PROCESS FOR ELECTROCHEMICAL OXIDATION OF HYDROCARBONS BACKGROUND CROSS-REFERENCE TO RELATED APPLICATIONS [0001] This application claims the benefit of U.S. Provisional Application No. 63/032,149 filed on May 29, 2020 and entitled, “PROCESS FOR ELECTROCHEMICAL OXIDATION OF HYDROCARBONS,” which is incorporated herein by reference in its entirety for all purposes. STATEMENT REGARDING GOVERNMENTALLY SPONSORED RESEARCH OR DEVELOPMENT [0002] None. [0003] The oxygenation of hydrocarbons with dioxygen from air, especially hydrocarbons such as low molecular weight gaseous alkanes and alkenes, is still a major challenge in oxidation catalysis that could have significant economic and industrial importance. (Arakawa, H. et al. Catalysis research of relevance to carbon management: progress, challenges, and opportunities. Chem. Rev. 101, 953–996 (2001); and Bergman, R. G. Organometallic chemistry: C–H activation. Nature 446, 391–393 (2007)). Some desirous transformations include alkane hydroxylation and further oxidation to aldehydes and carboxylic acids as well as alkene epoxidation and further carbon-carbon bond cleavage reactions. The incorporation of copper and iron into zeolites and metal organic framework materials has led to demonstrated carbon-hydrogen bond activation of methane to form methanol via proposed active metal-oxo species, but catalytic cycles have only been perpetuated using nitrous oxide as an oxygen donor or carried out in a three-step reaction requiring high temperature activation, typically at 450°C, of O ₂ and use of steam at elevated temperatures to remove methanol from the catalysts (Tomkins, P.; Ranocchiari, M.; van Bolchoven, J. A. Direct conversion of methane to methanol under mild conditions over Cu-Zeolites and beyond. Acc. Chem. Res. 50, 418-425 (2017); Narsimhan, K.; Iyoki, K.; Dinh, K.; Román-Leshkov, Y. Catalytic Oxidation of Methane into Methanol over Copper-Exchanged Zeolites with Oxygen at Low Temperature. ACS Cent. Sci. 2, 424−429 (2016); Panov, G. I.; Sobolev, V. I.; Kharitonov, A. S. The role of iron in N2O decomposition on ZSM-5 zeolite and reactivity of the surface oxygen formed. J. Mol. Catal. 61, 85−97 (1990); Snyder, B. E. R.; Vanelderen, P.; Bols, M. L.; Hallaert, S. D.; Böttger, L. H.; Ungur, L.; Pierloot, K.; Schoonheydt, R. A.; Sels, B. F.; Solomon, E. I. The active site of low-temperature methane hydroxylation in iron-containing zeolites. Nature 536, 317−321 (2016); Alayon, E. M. C.; Nachtegaal, M.; Bodi, A.; van Bokhoven, J. A. Reaction Conditions of Methane-to-Methanol Conversion Affect the Structure of Active Copper P-570163-IL2 Sites. ACS Catal. 4, 16−22 (2104); and Tomkins, P.; Mansouri, A.; Bozbag, S. E.; Krumeich, F.; Park, M. B.; Alayon, E. M. C.; Ranocchiari, M.; van Bokhoven, J. A. Isothermal Cyclic Conversion of Methane into Methanol over Copper-Exchanged Zeolite at Low Temperature. Angew. Chem.128, 5557−5561 (2016)). SUMMARY [0004] In some embodiments, a reactor for converting hydrocarbon gases comprises a reactor vessel, an anode disposed within the reactor vessel, a cathode disposed within the reactor vessel, and a catalyst disposed within the reactor vessel. The reactor vessel is configured to receive liquid phase and a gas phase, and the gas phase comprises reactants. [0005] In some embodiments, a method for converting hydrocarbon gases comprises providing a gas stream comprising a hydrocarbon to a reactor, providing a liquid stream to the reactor, contacting the gas stream with the liquid stream within the reactor, and converting at least a portion of the hydrocarbon to a product within the reactor based on contacting the gas stream with the liquid stream in the presence of the cathode and the anode. The reactor comprises an anode and a cathode. [0006] In some embodiments, a method of producing acetic acid comprises providing a gas comprising a hydrocarbon gas and oxygen/air to a reactor, contacting the gas with a liquid phase comprising a catalyst in the presence of a potential difference applied across a cathode and an anode, producing acetic acid based on the contacting, wherein the acetic acid is dissolved in the liquid phase, and separating the acetic acid from the liquid phase to produce an acetic acid product stream. BRIEF DESCRIPTION OF THE DRAWINGS [0007] For a detailed description of the preferred embodiments of the invention, reference will now be made to the accompanying drawings in which: [0008] Figure 1 illustrates a process flow diagram showing an overall process according to some embodiments. [0009] Figure 2 illustrates a schematic reactor layout according to some embodiments. [0010] Figure 3 illustrates another schematic reactor layout according to some embodiments. [0011] Figure 4 illustrates still another schematic reactor layout according to some embodiments. [0012] Figure 5 illustrates yet another schematic reactor layout according to some embodiments. [0013] Figures 6A and 6B illustrate embodiments of a membrane reactor. [0014] Figure 7A illustrates a layered stack assembly of a membrane reactor according to some embodiments. [0015] Figure 7B illustrates another layered stack assembly of a membrane reactor according to some embodiments. [0016] Figure 8 illustrates a process flow for a separation process for the products of the reaction according to some embodiments. [0017] Figure 9 illustrates an overall process flow diagram for a reaction and separation scheme according to some embodiments. [0018] Figure 10 illustrates a schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0019] Figure 11 illustrates another schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0020] Figure 12 illustrates still another schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0021] Figures 13A and 13B illustrate schematic process flow diagrams for separation columns for the liquid product stream from the reactor in some embodiments. [0022] Figure 14 illustrates another schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0023] Figure 15 illustrates still another schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0024] Figure 16 illustrates yet another schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0025] Figure 17 illustrates a schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0026] Figure 18 illustrates another schematic process flow diagram for a reaction and separation scheme according to some embodiments. [0027] Figure 19 illustrates a process flow diagram for a simulation of the overall process according to some embodiments. [0028] Figure 20 is a chart showing the stream properties for the streams illustrated in Figure 19. [0029] Figure 21 illustrates a process flow diagram for a simulation of the overall process according to some embodiments. [0030] Figure 22 is a chart showing the stream properties for the streams illustrated in Figure 21. DESCRIPTION [0031] This disclosure is directed to the process of electrochemical oxidation of hydrocarbons, using catalytic compounds such as polyoxometalate compounds, noble metals, and the like as catalysts and molecular oxygen, O ₂ , as an oxidant under electrochemical reducing conditions along with separation techniques to enable continuous production of oxidation products. This disclosure includes electrochemical reactor alternatives, catalyst alternatives, catalyst separation and recovery, and reactants and products separation process alternatives. [0032] The gap between dioxygen activation, that is formation of reactive intermediates, and actual catalytic transformations, especially of light hydrocarbons and alkanes under convenient aerobic conditions, using intrinsically stable inorganic catalysts, has not been effectively bridged. For example, using Mo-V-O system for aerobic oxidation of ethane to ethylene and acetic acid leads to formation of undesired CO ₂ . Polyoxometalates can be used in very high temperature oxygenation of alkanes, although selectivity and yields are low with significant formation of combustion products. In recent years, polyoxometalate capsules consisting of 132 molybdenum atoms, {Mo132} have shown very high activity for acid catalysis such as the hydrolysis of ethers. This disclosure provides a method of oxygenating hydrocarbons using various catalysts such as catalytic polyoxometalate compounds such as Na6(NH4)20(Fe ^III (H2O)6)2[{(WVI)WVI5O21(SO4)}12{(Fe(H2O))30}(SO4)13(H2O )34].nH2O and molecular oxygen under electrochemical reducing conditions. Some reactor configurations may use alternative catalysts such as noble metals instead of, or in addition to, the polyoxometalate compounds. [0033] Disclosed herein are reaction systems and processes for converting hydrocarbons to products. Within the reaction system, the reactor can be used to perform electrochemical reactions to convert the hydrocarbons to products. For example, hydrocarbons can be combined with oxygen from a variety of sources in an aqueous media to produce products. A catalyst that is soluble and/or sufficiently small to form a slurry can be used in the aqueous media to perform the reaction. Electrodes can be used in the reactor to aid in carrying out the reaction. [0034] As an example, the hydrocarbon can be a gas such as methane, ethane, propane, butane(s), and/or ethylene that can be introduced into an aqueous media within the reactor. The gas can dissolve in the reaction media and/or react at a gas-liquid interface to form the products. A micro or nanoscale catalyst can be used in the liquid to carry out the reaction. The electrodes can be placed in the reactor so that they contact the gas and liquid in order to carry out the reaction. While various reaction products are possible, an exemplary reaction can include the conversion of ethane to acetic acid within the reactor. Subsequent processes can then be used to remove the aqueous phase and separate the products from the reaction media. [0035] Due to the limited solubility of hydrocarbon gases in water or other aqueous media, various configurations can be used to increase the amount of hydrocarbon gases that solvate into the reaction media. For example, co-solvents can be used to help increase the solubility of the hydrocarbons in the aqueous media. Further, temperature control (e.g., retaining the reaction mixture cool) and/or increased pressures can be used to further increase the solubility of the hydrocarbon gases. While not intending to be limited by theory, it is believed that higher solubilities may contribute to higher reaction rates within the reactor. [0036] Overall, the disclosed reactor systems and methods allow for the electrochemical reactions of hydrocarbons with air and water. The systems also provide for the simultaneous reactions using a soluble or micro or nanoscale catalyst. The catalyst can be captures within the reactor and/or recovered and reused within the reactor. In addition, various methods to improve the solubility of the hydrocarbons in the water can also be used such as the use of cosolvents, solvating agents, temperature control, and higher pressures. Each of these can contribute to the ability to efficiently convert the hydrocarbons to products within the disclosed reactor system. [0037] As used herein, the term “upper portion” can refer to a top half or a top third of a column. Similarly, the term “lower portion” can refer to the bottom half or the bottom third of a column. The term “central portion” or “middle portion” can refer to the central third of a column.An exemplary overall process flow diagram is shown in Figure 1. The process is composed to four sections: (i) a feed pretreatment section 102, (ii) a reaction system 104, (iii) an optional catalyst recovery and recycle section 106, and (iv) a purification system 108 to produce on-spec products 136 and recycling reactants 138. In the feed pretreatment section 102, a hydrocarbon gas stream 122 can be passed through the feed pretreatment system 102 to remove impurities such as carbon dioxide, hydrogen sulfide, helium, and particulate matter as an impurities stream 124. In some embodiments, certain hydrocarbon components can be considered a feed impurity and removed in the feed pretreatment section 102 to provide a pure or substantially pure hydrocarbon stream. The feed pre-treatment section 102 can comprise any number of units such as acid gas removal units, filtration units, dehydrators, separators, absorbers, and the like to separate the impurities from the components desired in the remaining sections of the process. [0038] After the feed pretreatment section 102, the treated hydrocarbon gas in stream 126 can be fed to the reaction system 104, which can include an electrochemical reactor, along with an oxygen source such as air, oxygen enriched air, pure oxygen, etc. in stream 128. As used herein, oxygen enriched air can refer to a stream comprising greater than 21% oxygen by volume. The reaction system 104 can comprise any of the reactors as described herein with respect to Figures 2-7 below. In some aspects, the reaction system 104 can comprise a reactor. The reactor can contain one or more catalysts, which in some embodiments can be in an aqueous medium. Recycled catalyst in stream 132 from the recovery/regeneration section 106 can also be added to the reactor. The reactor can be divided into two sections and can be equipped with electrodes include at least one anode and at least one cathode. The cathode space can contain an electrically conductive solution. Electrolysis can be carried out at a potential of from about 1 to about 4 volts. In some embodiments, the electrochemical reactor system 104 can use gaseous hydrocarbon reactants to react with oxygen from air or oxygen generated in the electrochemical reactor in the presence of a catalyst in the aqueous medium. The reaction conditions can vary. In some embodiments, the reactor can operate at a pressure between about 1 to 100 bar, and at a temperature at about 15 ^◦ C to 300 ^◦ C. [0039] While not intending to be limited by theory, it is expected that the reaction rate can be affected by the contact area available at the electrodes (e.g., the cathode surface area), the amount of gaseous reactants dissolved in the liquid, and an amount of the gas that can be mixed with the liquid medium to provide for the reaction. It is expected that improved reaction rates may be possible by increasing the cathode surface area, improving contact between hydrocarbons and oxygen, as well as improving solubility of reactants in the reaction mixture. It is expected that the catalyst type and amounts can affect the reaction rates as well as product selectivities. [0040] Because the electrochemical oxidation of hydrocarbon gases takes place in the aqueous medium, it may be beneficial for the reactants to have improved solubility. In addition to higher pressure and lower temperature in the reactor, certain organic species can be added to the reaction media to enhance the solubility of the reactant gases and hence improve reaction conditions. Since water is a structured solvent, hydrocarbon gases with very low polarity such as the reactant methane, ethane, propane, butane(s), and/or ethylene, and other non-polar gases such as oxygen have poor solubility in water. The addition of an organic solvent to the liquid media (e.g., an aqueous media) can make the water less structured and allow for significantly improved solubility of oxygen several fold and even more for hydrocarbons such as methane, ethane, propane, butane(s), or ethylene. Organic compounds that are not oxidized easily, such as diethyl ether and tertiary butanol are also favorable species to be added. In addition, by adding a species already part of the reaction scheme, such as butyl acetate, ethyl acetate, formic acid, and/or acetic acid, the solubility of reactant hydrocarbon gases and oxygen into the aqueous phase can be improved without compromising on higher energy of separation. In some embodiments, organic solvents such as diethyl ether, 1,4-dioxane, ethyl acetate, methanol, tertiary butanol, and/or acetone can be added to the liquid reaction media to serve as enhancers to the reactant gas solubility into the aqueous reaction medium. [0041] Additional solubility enhancements can be achieved by improving mass transfer limitations using physical devices that improve the gas-liquid contacting area and hence solubility. For example, any device or configuration that allows for a greater contact area between the reactant gases and the liquid media can be used to improve the mass transfer. For example, sintered spargers, or fritted glass tips can be used to introduce gases into liquids through tiny pores, creating bubbles far smaller and more numerous than with other conventional methods. Nozzles can also be used to form a jet of gas into the liquid that can create shear effects to form small bubbles of the reactant gases, thereby increasing the gas- liquid contact area. Mechanical mixers or agitators can also be used to increase the contact area. Any other suitable mixing devices can also be used. The result is a greater gas-liquid contact area, which reduces both the time and volume required to dissolve gas into the liquid medium (e.g., an aqueous media such as water). [0042] Within the reactor system 100, the catalyst can be a heterogeneous catalyst that can be separated from the reaction mixture in some embodiments. The catalyst can be separated from within the reaction mixture during the reaction and passed in stream 130 to the catalyst recovery and recycle section 106. A portion of the reaction media and/or reaction products can be used as a carrier fluid for the catalyst as part of the recovery and separation process. Within the catalyst recovery and recycle section 106, the catalyst can be separated, processed, and returned to the reaction system 104 in stream 132. An amount of make-up catalyst can be added within the catalyst recovery and recycle section 106 to maintain the desired amount of catalyst within the reaction system 104. [0043] The products from the reaction system 104 can pass out of the reaction system 104 in stream 134 and pass to a separation and purification system 108. The reaction products in stream 134 can comprise end products such as acetic acid, acetates, and the like, the reaction media such as an aqueous fluid, unreacted reactants dissolved within the reaction media, possibly some amount of free gas entrained in the reaction media, and possibly some amount of catalyst entrained within the reaction media. Within the purification system, an aqueous stream can be taken out of the purification system as stream 142. The aqueous fluid, or any portion thereof, can be recycled for use within the system, used in another process within the system, or removed from the system for other downstream uses or disposal. Any free gases can be passed through a vent as stream 140. The gases, or a portion thereof, can be recycled to the inlet of the reactor when the vent stream 140 comprises unreacted hydrocarbons, oxygen, and/or nitrogen. Alternatively or when the vent stream 140 comprises other gases, the vent stream 140 can be passed out of the system for other uses. The purification system 108 can also produce a recycle stream 138 comprising any unreacted reactants and reaction intermediates, water, some portion of the products, and potentially small amount of catalysts, depending on the composition to the inlet of and separation efficiency of the purification system 108. [0044] Within the purification system 108, the products produced in the reaction section 104 can be separated from water and/or byproducts and removed from the system as purified product stream 136. Any water produced during the reaction can be removed from the purification system and the remaining water can be recycled back to the reaction system. Also, the purification system 108 can separate unreacted hydrocarbons from other gases coming out of the reaction system such as nitrogen, oxygen, and/or carbon dioxide. [0045] A variety of reactor configurations can be used within the reactor section 104. Figure 2 shows an embodiment of a reactor configuration 200 as a way to improve the cathode surface area and improve production of the products. The reactor configuration 200 can comprise a reactor vessel 201 comprising one or more cathodes 214 and one or more anodes 216. The cathodes 214 can be connected in parallel to a cathode power sources with intervening anodes 216, also connected in parallel to an electrode power source. [0046] In order to provide a large surface area, the cathode 214 can be coupled to a conductive (e.g., metallic, metal coated, conductive carbon, etc.) structured filling with a large surface area. For example, the structured filling can be a mesh, gauze, screen, perforated foil, structured packing, or the like to provide a relatively large surface area. In some embodiments, the structured filling can have a surface area ranging from about 100 to about 1000 m ² /m ³ . The anode(s) 216 can be conductive plates or screens in contact with the reaction media. [0047] The liquid reaction media 202 can be introduced near a top of the reactor vessel 201 through a distributor and flow downward through the reactor vessel 201 in countercurrent fashion with the gas 204 introduced in a lower portion of the reactor vessel 201. As dissolved gas is converted to products in the reactor, the gas can be replaced with additional dissolved gas striving to keep the gas at its solubility limit throughout the reactor vessel 201. [0048] The reaction media can be removed from the lower portion of the reactor vessel 201 as stream 206. Any make-up solution can be combined with this stream, and the combined stream can be passed through a heat exchanger 208 to control the temperature of the reaction media in the reactor. The temperature can rise within the reactor based on the reaction, and the generated heat can be removed externally using, for example, the cooler 208. Other suitable heat transfer configurations such as a cooling jacket around the reactor can also be used. [0049] In some aspects, the catalyst can be a heterogeneous catalyst present in the liquid reaction media. In order to retain the catalyst in the reaction media, a filtration system or other element designed to filter the product stream from the reaction media can be used within the reactor. In some embodiments, the reactor design can include a filtration membrane 210 (e.g., a nanofiltration membrane) prior to the product outlet 212. This filtration membrane 210 serves to separate the catalyst from the liquid outlet and retain the catalyst in the reactor vessel 201 through the recycle loop 206. Various membranes such a polymer based membranes, ceramic filters, screens, and the like can be used to separate the catalyst from the product solution. Figure 2 shows a simple flat membrane. Other shapes are also possible. For example, Figure 3 shows the use of a hollow tube membrane system 310 inserted directly into the reactor vessel 201. While shown as a single tube, a plurality of tubes can also be used. For example, a tube bundle can be present within the reactor and have a common outlet to collect the product stream 310 permeating through the membrane. Other suitable membrane configurations such as pleated, vertically arranged tubes, plates, screens, and the like can also be used to form the membrane 310. [0050] Figure 4 shows a schematic representation of another reactor configuration. The reactor system 400 shown in Figure 4 addresses certain design criteria for the electrochemical reactor system. First, a higher cathode surface area is desired for improving reaction rates and a shell/tube configuration allows cathode surface area to be increased. Second, a shell/tube configuration allows heat transfer for removal of the heat of reaction within the reactor vessel 401. [0051] As shown in Figure 4, the reactant gases can enter the reactor in stream 408, and any unreacted gases can pass out of the reactor as stream 413. The reaction media can be introduced counter-currently as stream 412 and pass out of the reactor vessel 401 as outlet stream 410. Heat transfer fluid (e.g., water, an aqueous fluid, glycol, an oil, etc.) can be used to maintain the temperature in the reactor at a desired temperature. The heat transfer fluid can be introduced in stream 402 and pass out of the reactor vessel 401 as stream 403. The reactor vessel 401 can have insulation 406 disposed on a portion or all of the reactor to maintain the temperature at a desired set point. While shown in Figure 4 as having the reactants on the tube side and the heat transfer fluid on the shell side of the exchanger, the reactants can also be introduced on the shell side and the heat transfer fluid can be within the tubes in some embodiments. [0052] The tube sheet bundle in this case can be the cathode 414 and appropriate materials of construction can be utilized. Other conductive components can then serve as electrodes 416. Shell and tube configuration using a conductive material (e.g., metal, conductive carbon such as graphite, etc.) can be used as a material of construction since conductive materials such as graphite can act as the electrode material. In case a non-conductive shell and tube configuration is used, the tubes can be coated with conductive materials (such as Pt, C) that can act as electrode. [0053] Another reactor configuration is shown in Figure 5. As shown, a jet loop reactor configuration 500 can include a nozzle 502 used to form a jet and a loop which recycles part of the reaction media passing through the reactor. The media can pass out of the reactor 501 through stream 506, pass through a pump 509, and back into the reactor 501 as stream 504 to form the loop. A product stream 511 can be taken out of the reactor 501 and/or from the outlet stream 506. The reactant gases can enter the lower portion of the reactor 501 as inlet gas stream 508. The outlet gases can pass out of the reactor 501 as outlet gas stream 513. [0054] The circulation through the reactor 501 can be achieved in three basic modes of operation: hydrodynamic (1), hydromechanics (2), and/or hydrostatic loop (3). The flux in (2) and (3) can be generated using agitators or density differences while (1) is powered by a jet stream. This jet stream can be created using the reaction medium that is drawn from the reactor 501 in stream 506 and reinjected through a nozzle 502 in a second external loop. In some aspects, the stream 506 can form bubbles that pass between the cathode 514 before rising an in outer portion of the reactor vessel 501. An anode 516 can also be disposed in the reactor vessel 501. It is therefore a double loop configuration by design. This mode of operation offers the advantage of non-moving reactor internals unlike other options that use agitators that need good sealing at high pressure and or temperature. Moving parts also are affected by abrasion and may require higher maintenance cost compared to equipment with non-moving parts. In some aspects a mechanical agitator such as a magnetically coupled stirrer can be used so that there are no mechanical connections passing through the reactor vessel walls, which can avoid the sealing issues but may still have wear due to the movement of the mixers. In gas-liquid catalytic reactions, it is favorable to insert the liquid medium from the top of the reactor where the jet stream sucks in or entrains the gaseous components in the nozzle 502 via impulse transfer. The captured gas is then dispersed into small bubbles 505 by the shear stress in the jets and forms bigger bubbles as it moves through the draft tube. At the end of the tube, the bubbles are deflected using an impact plate to form large macro shapes 507 that rise in the outer reactor ring and induce additional circulation similar to an airlift pump. Interaction of the internal and external loop and the shear forces of the nozzle 502 results in intense mixing achieving high interfacial surface between the reaction phases. Therefore, a jet loop reactor provides fast mass transfer enhancing electrochemical reaction rates. [0055] Heat exchange can be achieved through the addition of cooling coils in the reactor or by using external heat transfer using a heat exchanger (e.g., upstream or downstream of the pump 509, in a separate loop, etc.) will enable removal of exothermic heat of reaction in a jet loop reactor configuration. [0056] The catalyst used in any of the systems described herein can comprise any suitable catalyst for converting a hydrocarbon to a product, such as acetic acid. In some embodiments, the catalyst can comprise a polyoxometalate catalyst as described in WO2018/225066, entitled “Electrochemical Oxygenates of Hydrocarbons” by Ronny Neumann, et al., which is incorporated herein in its entirety for all purposes. [0057] For example, the reactions described herein can be used to contact a hydrocarbon with a polyoxometalate catalyst or a solvate thereof with oxygen (e.g., molecular oxygen, oxygen from air, etc.). As described herein, the contacting can occur in an electrochemical cell to generate or produce an oxidized hydrocarbon product such as acetic acid, acetaldehyde, formic acid, formaldehyde and/or the optional hydrate thereof. When a polyoxometalate catalyst, is used, the catalyst can be of the general formula (1): Q1[{(M)M5021(X')0}J{(M'(H20))k}(X)i(H20)m] ^ (1) or a solvate thereof; In this formula, i is between 0-50; j is between 5-20; k is between 0-50; 1 is between 5-50; m is between 0-50; o is between 0-10; each of Q is independently absent or the same or a different metal or NH4 ⁺ cation; each of X is independently H20 or the same or a different anion; each of X' is independently H20 or the same or a different anion; each of M is independently Mo or W; and each of M' is independently Fe, V, Cr, Mn, Co, Ni or Cu. [0058] In some embodiments, the polyoxometalate catalyst can be of the general formula (2): Q ₁ [{(M)M ₅ 0 ₂ i(X')o} _J {(M'(H ₂ O)) _k }(X)i(H ₂ O) _m ]-n-H ₂ O- (2); where: i is between 0-50; j is between 5-20; k is between 0-50; 1 is between 5-50; m is between 0-50; n is between 0-1000; o is between 0-10; each of Q is independently absent or the same or a different metal or NH4 ⁺ cation; each of X is independently H20 or the same or a different anion; each of X' is independently H20 or the same or a different anion; each of M is independently Mo or W; and each of M' is independently Fe, V, Cr, Mn, Co, Ni, or Cu. [0059] In some embodiments, the polyoxometalate catalyst can be of the general formula (3): Q1[{(W ^VI )W ^VI 5021(X')0}J{(Fe(H ₂ 0))k}(X)i(H20)m] . n H20 (3); where Q, X, X' i, j, k, 1, m, n and o are as defined for formula (1). [0060] In some embodiments, the polyoxometalate catalyst can be of the general formula (4) referred also as "{Fe ⁱⁿ 3o W ^VI 72}" or as "{Fe30W72}": Na6(NH4)2o(Fe ^III (H ₂ 0)6)2[{(W ^VI )W ^VI ₅ 0 ₂ i(S0 ₄ )}i ₂ {(Fe(H ₂ 0)) ₃ o}(S0 ₄ )i ₃ (H ₂ O) ₃₄ ] . nH ₂ O, (4) where n is as defined for formula (1). [0061] In some embodiments, the polyoxometalate catalyst can be of the general formula (5): Na6(NH4)2o(Fe ^III (H20)6)2[{(W ^VI )W ^VI 502i(S04)}i2{(Fe(H20))3o}(S04)i3(H20)34] ^ 200 H20, (5). [0062] In some embodiments, the polyoxometalate catalyst can be of the general formula (6), referred also as "{Fe ⁱⁿ ₃ o Mo ^VI ₇₂ }" or as "{Fe ₃ oMo ₇₂ }": [{(Mo ^VI )Mo ^VI 5021)(X'1)6}12{Fe ^III (H20)(X1)}3o]- n H20, (6), where n is between 0 and 1000; X' i and X1 are each independently selected from H20, Mo208 2- ^" , Mo ₂ 0 ₉ 2- ^" and CH ₃ COO ^" (acetate); the compound (formula (6)) comprises 12 CH ₃ COO ^" (acetate) anions and 3 (three) dimolybdate anions; and each dimolybdate anion is Mo2082- ^" or Mo ₂ 0 ₉ 2 anion. [0063] Within the reactor systems as described herein (e.g., within any of the systems as described with respect to Figures 1-7), the reaction can be carried out in the presence of a reaction media comprising a catalyst. The catalyst can be a heterogeneous catalyst disposed within a liquid reaction media, or as part of the reactor structure. As part of the reaction, the catalyst can be separated from the reaction media to retain the catalyst within the reaction media while allowing a product stream to be extracted from the reactor. In some embodiments, the catalyst can be separated from the reaction mixture using semi-permeable membranes, crystallization, electrostatic precipitation, dissolved gas flotation, hydrocyclones, centrifuges, or any combination there. [0064] In some embodiments, semi-permeable membranes can be used to separate one or more cathodes from one or more anodes and also to filter catalyst. For example, an inorganic membrane can comprise a mesoporous ^-alumina supported ^-alumina membrane with a pore size appropriate to separate catalyst from the reaction mixture. Membranes made from mesoporous oxides of silicon, niobium, tantalum, titanium, zirconium, cerium, and/or tin can also be used for the nanofiltration. Activated carbon, which typically comprises a carbon framework with micro as well as meso porosity, can be used as a nanofiltration material for catalyst separation and recycle. Typical pore sizes for such membranes can range from about 2 to about 50 nm. [0065] In some embodiments, crystallization can be used to recover the catalyst from the reaction mixture. The crystallization process can be carried out by removing at least a portion of the aqueous phase to leave the non-volatile catalyst, which can form a slurry and/or crystalize out of solution to allow the catalyst to be reused. [0066] In some embodiments, electrostatic precipitation can be used to separate the catalyst. For example, one or more high voltage plates can used to concentrate the catalyst and remove the catalyst from the reaction mixture. The catalyst can be charged and can then be electrostatically attracted to the plate. Once concentrated on the plate, the plate and the associated catalyst can be removed from the reaction solution. [0067] In some embodiments, dissolved gas flotation can be used to separate the catalyst. In this process, the catalyst can be aggregated and separated in particle form using a dissolved gas that can be liberated by a pressure reduction. Tiny bubbles can then form to capture agglomerated catalyst particles, and the agglomerations can rise to the surface where they can be removed by physical or mechanical means. [0068] In some embodiments, hydrocyclones and/or centrifuges can be used to separate the catalyst. A hydrocyclone is a cono-cylindrical mechanical device used to separate a solid dispersed phase from a liquid or slurry by means of centrifugal forces within a vortex. The mixture can be injected into the hydrocyclone in such a way as to create the vortex and, due to difference in densities of the two phases, the centrifugal acceleration causes the dispersed phase to move away from or towards the central core of the vortex. A tangential feed inlet is connected to the cylindrical section and an outlet at each axis. The outlet at the cylindrical section is called the vortex finder and extends into the cyclone to reduce short-circuit flow directly from the inlet. At the conical end is the second outlet, called spigot. Hydrocyclones are operated vertically with the spigot at the lower end. Liquid outlet from the reactor carrying suspended catalyst particles can enter the cyclone tangentially, spiral downward, and produce a centrifugal field in free vortex flow. Larger particles move through the fluid to the outside of the cyclone in a spiral motion, and exit through the spigot with a fraction of the liquid. Hydrocyclones are relatively inexpensive with diameters ranging from 10 mm up to 2.5 m. Centrifugal separation uses similar principle, however, unlike hydrocyclones, centrifuges consist of moving parts. A rapidly rotating container applies centrifugal force to its contents, typically to separate the catalyst (which has higher density) from the fluid. [0069] An additional reactor configuration is shown in Figures 6A and 6B. As shown, a reactor design can include an electrolyzer-type reactor 600 with a proton exchange membrane 602 separating the anode 604 and the cathode 606. The membrane 602 can be gas impermeable, such that no gasesous products such as ethane, oxygen or hydrogen are transferred to the opposite side. Protons can be transferred from the anode 604 to the cathode 606 through the membrane. Protons can be generated from the dissociation of water by means of electricity on the anode side. One or more electrocatalyst(s) can be attached on both sides of the membrane. These catalysts can be heterogeneous, and may not dissolve into the solution. In various embodiments, electrodes formed from Ir, Pt, Pd, and/or Ru, with and without Fe, Co, Ni, and/or Cu as promoters, can be used and inserted on either side of the membrane 602. In some embodiments, the catalyst(s) used with the reactor can comprise any of the polyoxometalate catalysts described herein. [0070] As shown in Figure 6B, the structure of the reactor 600 can be similar to a membrane electrode assembly (MEA) with a membrane 602 in the center, catalyst (e.g., anode catalyst 608, cathode catalyst 610, etc.) on either side of the membrane 602, a gas diffusion layer (e.g., anode gas diffusion layer 612, cathode gas diffusion layer 614, etc.) adjacent to the catalyst, and finally flow plates (e.g., anode flow plate 618, cathode flow plate 620, etc.) on either side. The flow plates 618, 620 can have a channel for fluid (e.g., liquids, water, reaction media, etc.) distribution. Each layer can have a thickness of at least 10 μm, for example between about 10 μm and about 10 mm. [0071] The catalyst layers 608, 610 can comprise one or more of the catalysts. The catalyst can be affixed to a support layer to allow the reactants to contact the catalyst to form intermediates and reaction products. The gas diffusion layer (e.g., anode gas diffusion layer 612, cathode gas diffusion layer 614, etc.) can be formed from a material selected to allow the gas to pass through the gas diffusion layer and contact the catalyst. In some aspects, the gas diffusion layer(s) can be formed from hydrophobic materials such as fluoropolymers to allow the gaseous reactants to diffuse to and react at the catalyst. Various forms such as a mesh, gauze, screen, or other structure can be used to form the gas diffusion layer(s). The flow plates may be used to define flow channels and retain the reactants, intermediates, reaction media, and products within the reactor. The flow plates can be formed from any suitable materials such as plastics and/or metals. [0072] An overall reactor assembly using one or more MEA type cells 600 can consist of a cell stack in which multiple single cells each including a membrane electrode assembly are stacked in the stacking direction. The reactor cell stack can include appropriate electrical insulation members each connected to an outer peripheral portion of a corresponding one of the membrane electrode assemblies. The reactor cell stack can also include a first displacement absorbing member disposed between each insulation member and an adjacent insulation member to absorb displacement between the plurality of membrane electrode assemblies. [0073] In order to retain a good proton transfer across the membrane 602, wet conditions can be maintained in the cell by humidifying the anode gas and the cathode gas prior to or within the reactor cell stack. The anode electrode 604 can be a stack of layers including an anode catalyst 608 made of an alloy including platinum or the like, a water-repellent layer made of fluorocarbon resin or the like, and a gas diffusion layer made of a carbon cloth or the like, which can be stacked on the electrolyte membrane 602 in this order. As with the anode electrode 604, the cathode electrode 606 can be a stack of layers including a cathode catalyst 610, a water repellent layer, and a gas diffusion layer, which can be stacked on the electrolyte membrane 602 in this order. The anode electrode 604 and cathode electrode 606 can be followed by flow plates 618 and 620 respectively on their side. Appropriate insulation can be applied for the cell assembly. Cooling water can be introduced through a separate cooling channel 622 between the anode 604 and the cathode 606. Cooling channels 622 can be one per pair of anode 604 and cathode 606 or can be alternated. In some embodiments, air can be used as a coolant instead of water. [0074] Figures 7A and 7B schematically illustrates the assembly 700, which is a layered stack including a membrane electrolyzer assembly (MEA) 600, an anode electrode disposed on one surface of the electrolyte membrane, and a cathode disposed on the other surface of the electrolyte membrane. The electrolyte membrane can be a proton-conductive ion exchange membrane. Suitable membranes can be formed from various materials such as a fluorocarbon resin. In some aspects, the electrolyte membrane 602 can be larger than the adjacent electrodes, so that the electrolyte membrane 602 has an outer edge which extends past the outer edges of the electrodes. [0075] In some embodiments, cooling water can be introduced in the cell assembly by using stamped bipolar plates with cooling channels 622 as shown in Figures 7A and 7B. A coolant gasket 704 can be used between the faces of bipolar plates 620, 706 that form a coolant cell. One of more additional gaskets 708 can be used between the plates and an endplate 710 to form one or more cooling channels or cells. Stamped bipolar plates can be used for efficiency in manufacturing. [0076] This type of MEA reactor may address the low solubility issue of ethane and air in the water liquid phase as observed in other reactor designs. The use of the attached heterogeneous catalyst is able to overcome the catalyst recovery issue which in turn reduces the complexity of the process and operation cost. The modular nature of the design also has better scalability by stacking of the units similar to the system of a proton exchange membrane in water electrolysis and flexibility for maintenance. The system could be configured in a very compact size which would lead to a smaller footprint for the plant. [0077] Referring to Figures 6A-7B, the reactants (e.g., ethane and oxygen/air) can be fed to the cathode side 606, whereas water can be fed to the anode side 604. In order to keep good proton transfer of the membrane 602 in wet condition, the cathode gas can also be humidified. The reactants can react in the cathode side 606 to form reaction products. Unreacted feed gases, product acetic acid, intermediates ethanol and acetaldehyde, and byproduct formic acid can exit from the cathode side 606, either as a single vapor phase or a mixed vapor-liquid phase depending on the reaction conditions. This is illustrated in Figure 6A. For the production of acetic acid, the simplified reaction chemistry proceeds according to the follow reactions: Anode: 3H ₂ O → 3(2H ⁺ + 1/2 O ₂ + 2e-) Cathode: CH ₃ CH ₃ + 2H ⁺ + 2e- + O2 → CH ₃ CH ₂ OH + H ₂ O CH ₃ CH2OH + 2H ⁺ + 2e- + O2 → CH ₃ CHO + 2H ₂ O CH ₃ CHO + 2H ⁺ + 2e- + O2 → CH ₃ COOH + H ₂ O [0078] The resulting reaction products from the anode side 606 can be separated according to the separation scheme as shown in Figure 18 and described in more detail herein. [0079] Within the process, the gas portion of the product stream removed from the reactor (e.g., any of the reactors described with respect to Figures 2-7) can be subjected to separation in order to separate and recycle the unreacted reactants such as the hydrocarbon components. The separation and recycle can comprise a number of separation techniques such as membrane separation, molecular sieve separation, pressure swing adsorption, temperature swing adsorption, cryogenic distillation, and the like. [0080] In some embodiments, membrane separation can be used to separate the gas stream leaving the reactor. For example, any of the gas streams (e.g., stream 211, stream 413, stream 513, etc.) in Figures 2-7 can be sent to a separation system. The membranes can comprise organic or inorganic membranes that can be used to separate light hydrocarbons from nitrogen, hydrogen and oxygen. Separated light hydrocarbons can then be recycled back to the electrochemical reactor, with a small purge, as seen in Figures 9 and 10, which are described in more detail herein. [0081] In some embodiments, molecular sieves can be used to separate the components of the gas outlet streams. Pressure swing adsorption using molecular sieves can also be used as an effective method to separate light hydrocarbons from gases such as CO2, N2 and O2. The gas outlet streams from the separator that follows the electrochemical reactor can be passed through a bed of adsorbent media at high pressure. Under high pressure, the specific gasses can be selectively adsorbed on to the surface and pores of the adsorbent media. The adsorbed gases are removed from the molecular sieves by reducing the pressure. Commercial scale systems typically use multiple adsorbent beds so that one is always in the adsorption mode, while other beds are regenerated, thus enabling continuous operation. Molecular sieve media with the appropriate pore size is used such that it will preferably adsorb target molecules. Smaller molecules, such as CO2, O2, and N2 are able to fit into the pores and be strongly adsorbed, while the light hydrocarbons such as methane, ethane, etc., are too large to fit in the pore and move downstream of the adsorbent bed. This results in effective separation of light hydrocarbons from CO ₂ , O ₂ , and N ₂ . Separated light hydrocarbons can then be recycled back to the electrochemical reactor, with a small purge, as seen in Figures 9 and 10 and described in more detail herein.  [0082] Ethane oxidation to acetic acid is an exothermic reaction. In any of the reactor designs described with respect to Figures 2-7, the reactors can be configured to be cooled in situ or operate as an adiabatic reactor with external cooling. In-situ cooling may allow the reactor to operate as an isothermal reactor or a substantially isothermal reactor, though the reactor operating temperature may be controlled using an in-situ coolant without operating in an isothermal regime (e.g., by having a controlled or target temperature rise across the reactor). For in-situ cooling, heat effects of the reaction can also be removed by means of an embedded cooling or heat removal mechanism. The presence of the inert nitrogen gas also provides partial heat removal to maintain the reaction temperature. In some aspects, heat generated in any of the reactor configurations described with respect to Figures 2-7 can be removed in heat exchanger external to the reactor. For example, heat can be removed in a subsequent condenser cooled by cooling water. [0083] Reactor configurations in any of Figures 2-7 can have a reaction temperature of between about 35⁰C to about 100⁰C in each reactor unit. The reaction temperature in the reactor can be between about 35⁰C and about100⁰C and have a pressure of less than or equal to about 200 psi, though other reaction conditions are possible. As the reactions are generally exothermic, the inlet temperature of the reactants can be controlled to maintain the reactor temperature and/or reactor assemblies with internal cooling can enable heat removal to maintain the reaction temperature within a desired range. [0084] In any of the reactor configurations, including those described with respect to Figures 6A-7B, an alternate configuration of operating a reactor can be in the form of a cascade of adiabatic reactors (e.g., reactors arranged in series, or in some aspect, in parallel) cooled intermittently by coolers. In this configuration, the reactors can form reactor-cooler pairs such that the resulting pair can be used to control the reaction temperature. In some aspects, each reactor unit in a cascade could be operating at a temperature rise of, for example, from about 35⁰C to about 85⁰C, or a temperature change of about 50⁰C. Any suitable design temperature change can be used within the limits of the reactors. Multiple cascade units with coolers in between them for both the gas and liquid phases that flow from one unit to another, could be used to achieve a desired conversion. [0085] [0086] In some aspects, a reactor designed with a temperature rise of between about 35⁰C to about 85⁰C could have a relative low conversion (e.g., a 1% to 5% conversion or approximately a 2% conversion). The resulting series of reactor could then be designed to have a 10% to 50%, or about 20% overall conversion, thereby using a plurality of reactor units in series to achieve the desired overall conversion. Liquid exiting the reactor can be cooled from about 85⁰C to about 35⁰C to the next reactor’s inlet. Figure 7A illustrates each unit (e.g., an adiabatic reactor) is one or multiple stacks of cells in an assembly with feed in parallel. The products can be cooled using an external cooler before sending it to the next adiabatic unit of cells. The product from any of the electrochemical reactors can be processed in a separation or product purification section (e.g., purification system 108 of Figure 1). The purification system can serve to produce a product stream as well as one or more recycle streams to the reactor. In some aspects, separation systems are shown in the schematic flowsheets of Figures 8 and 9. When the product comprises acetic acid, the objective of the separation system is to separate the desired chemical, acetic acid, from the liquid mixture that contains water, dissolved gases, some catalyst, intermediates, and other by-products. [0087] As shown in Figure 8, the product stream 605 from the electrochemical reactor can first pass to a degassing unit 601. The product stream 605 can comprise any of the product streams described with respect to Figures 1-7. In general, the product stream may have had the catalyst filtered out using a variety of configurations such as a membrane separation. As a result, the product stream 605 may have a reduced amount of catalyst, if any, relative to the reaction media. The liquid entering the degassing unit 601 can be degassed by using a distillation column or a simple flash vessel. In general, a flash vessel may have a single stage of separation where as a distillation column can comprise two or more stages of separation. Additional vessels or columns can be optionally used to further de-gas the product stream to a desired level. The degassing unit 601 can be used to vent out any dissolved gases such as N ₂ , O ₂ , hydrocarbon gases, hydrogen, or the like in the off-gas stream 603. The pressure and other operating conditions (e.g., temperature, flow rates, residence time, etc.) can be adjusted to minimize the loss of products in the vapor phase. [0088] In some embodiments, the gas phase stream 603 vented from the product stream 605 in the degassing unit 601 can also comprise unreacted hydrocarbon gases exiting the reactor in the gas phase along with the non-condensable nitrogen and unreacted oxygen. The resulting gas phase stream can be processed in a number of ways. In some aspects, nitrogen can be separated from the unreacted hydrocarbon, and after an optional purge stream is taken from the recycle stream, the separated unreacted gas stream can then be compressed to the reactor pressure and recycled back to the reactor. In some aspects, a fraction of the unreacted hydrocarbon gas stream can be recycled to the reactor and the rest purged from the process gas without any type of membrane separation. Depending on the hydrocarbon content, composition, and heat value, the purged stream may be used as fuel gas for generating steam and/or electricity. In some aspects, all the unreacted gas stream can be sent for use as fuel in the process. The selection of the use of the recycle gas may depend on the economic of the system and can vary over time. [0089] In some aspects, the vented gas stream (e.g., stream 140 in Figure 1 or off gas stream 603 in Figure 8) can be further treated to recover product prior to recycling and/or sending the vent stream for use as fuel. In addition to nitrogen, unreacted reactants, and possibly some unreacted oxygen, the vent gas stream can also comprise acetic acid and other reaction intermediates. In addition to the separation techniques described herein, the vent gas stream, or a portion thereof, can pass through an absorber or absorption unit. An absorption unity can comprise any unit configured to contact a gas stream with a solvent and absorb at least a portion of one component in the gas stream into the solvent, thereby effecting a separation of the components. Absorption can be used to recover acetic acid and reaction intermediates from the gas stream. The absorber can be placed on the purged gas stream (to minimize acetic acid loss) and/or the entire gas stream (to maximize per pass acetic acid recovery). Water can be used as a solvent in the absorber. A fraction, or the entire, water recycle from the water separation column can be used as the solvent in the absorber. The acetic acid rich liquid leaving the absorber can be recycled to the reactor, or the liquid separation system or both. The conditions in the absorber can be approximately the same as the pressure and temperature of the reactor exit stream. The remaining purge gas stream can be used as a fuel gas within the system or leave the system. [0090] The liquid stream 607 leaving the degassing unit 601 can comprise the product in an aqueous fluid. The liquid stream 607 can then pass to a separation unit 611 to produce an acetic acid stream and a second stream comprising other components such as water, any remaining catalyst, any gas solvating agents, and the like. The separation unit 611 can use any suitable separation techniques to separate from the acetic acid from the remaining components. In some embodiments, the separation unit can utilize distillation, decantation, azeotropic distillation, extraction, extractive distillation, or the like, and the separation unit 611 can be formed from one or more vessels connected in parallel or in series. [0091] In some embodiments, distillation can be used to separate the acetic acid from the remaining components. However, the vapor-liquid behavior of acetic acid and water indicates the presence of a tangent pinch on the pure water side, which means that while it is possible to achieve a high purity acetic product using conventional distillation, it is difficult to simultaneously achieve a high purity water product. When some acetic acid is recycled along with the water back to the reactor, the desired separation can be achieved using conventional distillation [0092] In some embodiments, azeotropic distillation can be used in order to address the tangent pinch. Azeotropic distillation uses an entrainer to separate two components that are difficult to separate by conventional distillation, either due to the presence of an azeotrope or tangent pinch behavior. Entrainers in the separation of acetic acid and water can include components such as ethyl acetate, propyl acetate, butyl acetate, etc. The salient characteristic of an entrainer is that the entrainer forms a minimum boiling heterogeneous azeotrope. [0093] In some embodiments, decantation can be used to separate the acetic acid from the other components of the product stream. Decantation comprises the separation of acetic acid and water by introducing an entrainer that exhibits heterogeneous behavior with water. Acetic acid then distributes between the aqueous and organic phases. Decantation by itself is not able to obtain pure product purity desired. When an entrainer is used, the aqueous phase from the decanter can be further purified in a distillation column in which water is recovered as the bottom stream with the distillate recycled to the entrainer stream. The organic phase from the decanter can be further purified using distillation (e.g., in one or more columns) to recover high purity acetic acid, and the entrainer rich stream from the distillation may be recycled to the entrainer stream, after an optional purge. [0094] Extraction followed by distillation is similar to decantation followed by distillation, and involves a liquid/liquid extraction step where an appropriate solvent suitable to form a multi- phase solution (e.g., at least a partially immiscible solvent as an extractive agent which exhibits heterogeneous behavior with water) is contacted in a counter-current fashion with the water based product stream. The solvent can be selected based on its physical properties so that it effectively and selectively extracts the acetic acid. [0095] Figures 8 and 9 illustrate process flow configurations for the separation of the products from the reaction system. Figure 8 shows an example of an extraction process in which the liquid stream 607 can be provided to an extraction column 611. It can be noted that an extraction column can also serve as a decanter (e.g., a single-stage extraction column). An entrainer or solvent can be introduced in the lower portion of the extraction column 611 through stream 613, while the liquid stream 607 can be introduced in an upper portion of the column 611. The solvent can rise within the column to extract at least a portion of the acetic acid in the solvent phase, which forms a heterogeneous mixture with the aqueous phase liquid in the liquid stream 607. The rich solvent containing the extracted acetic acid can then pass out through stream 609, while the aqueous phase having the acetic acid at least partially removed can pass out through stream 615. The aqueous phase stream can contain the catalyst and can be recycled within the system to the reactor. While shown as having the liquid stream 607 entering the upper portion of the extraction column 611, the liquid stream 607 could enter a lower portion if the solvent has a higher density than the aqueous phase in the liquid stream 607, where the counter-current flow is established based on density differences between the two streams. [0096] As shown in Figure 9, the rich solvent in stream 609 can then be sent on to an acetic acid separation column 902 for separation of the acetic acid and the solvent. The selection of the solvent can be used to provide an easier separation than the separation of water and acetic acid. Once separated, the solvent phase from an extraction or decanter process can be partially recycled back to the solvent stream 613. A small purge can be taken out of the recycled solvent stream to avoid the build-up of impurities. [0097] Water can be recovered in a distillation column 904 with water being removed as the bottoms stream and the distillate recycled to the solvent product from the acetic acid separation column 902. Part of the water can be purged from the process, and subsequently treated, if necessary, before being discharged, and the rest can be recycled back to the reactor. [0098] The separation system may also take other components of the reaction mixture into account. Acetic acid production by electrochemical oxidation of hydrocarbons as described herein proceeds through the formation of intermediates including ethanol and acetaldehyde, and byproduct formic acid. Both ethanol and acetaldehyde are partially recycled with the unreacted gases back to the reactor whereas a fraction is purged with the gas or liquid purge. [0099] The reactions proceed according to the following equations: [00100] In some embodiments, no entrainer is used to separate acetic acid and water as in the embodiments of Figures 8 and 9, and the water recycle can include a small amount of acetic acid. An example of such a process flowsheet is shown in Figure 10 in which acetic acid is recovered without an entrainer. Feed streams, reactor, and lights separation portion are the same as or similar to those described above with respect to Figures 19 and 20. [00101] Stream 1002 goes to the water removal column. Typical operating pressures in the water column are between about 0.5 atm to about 12 atm, or about 7 atm. A water and acetic acid stream having mostly water is obtained in the distillate. A fraction of this stream is purged in splitter 1004 to avoid buildup of water and organic impurities in the process of this stream whereas the rest is recycled to the reactor. The pure acetic acid product can be 99.9 wt% or greater in the bottoms product of the water removal column. [00102] Another process flowsheet example is shown in Figure 11. The formation of formic acid from acetic acid follows the equation: [00103] Byproduct formic acid has a tangent pinch on the pure formic acid side as demonstrated in the vapor-liquid equilibrium behavior with acetic acid. This leads to loss of acetic acid product in the formic acid purge. Formic acid also has a maximum-boiling azeotrope with water. Additionally, the formic acid-water-acetic acid ternary mixture exhibits a saddle azeotrope which limits the overall acetic acid recovery. However, both the formic acid-water azeotrope and the formic acid-water-acetic acid ternary are sensitive to higher pressure. At higher pressures the ternary saddle azeotrope tends to disappear. The distillate will contain formic acid, in addition to the acetic acid, and this formic acid will be recycled to the reactor. This can be followed by a formic acid/acetic acid separation. In this column, pure acetic acid can be obtained as a bottom product whereas formic acid and acetic acid can be removed as distillate and purged. [00104] A schematic of the process flowsheet is shown in Figure 11 in which high purity acetic acid product can be recovered without the use of an entrainer, along with a small amount of formic acid byproduct impurity. The feed streams, reactor, and lights separation are the same as or similar to those described with respect to Figures 9 and 10. [00105] In this example, when the formic acid byproduct formation occurs, it can leads to a formic acid impurity in the acetic acid product if not separated. In some embodiments, no entrainer is used to separate the acetic acid and water as in the first example, and the water recycle can include a small amount of acetic acid. Typical operating pressures in the water column 1102 can be between about 0.5 atm to 12 atm, or about 7 atm. The acetic acid column 1104 can be operated at approximately atmospheric pressure. After separating water (with the rest being predominantly acetic acid with small amounts of formic acid and other impurities and/or reaction intermediates) in the distillate of the water column 1102 (as seen in Figure 11), formic acid can be purged in the distillate of the acetic acid column 1104 (along with a small loss of acetic acid). Pure acetic acid product can be obtained at the bottom of the acetic acid column 1104 at a purity of about 99.9wt% or greater. [00106] The order of the water and acetic acid separation columns shown in Figure 11 can also be reversed with the acetic acid being recovered as a bottom product in the first column 1102, the water-acetic acid recycle stream can be the distillate of the second column 1104, and the formic acid acetic acid purge can be taken as the bottom product of the second column 1104. In this case, the operating pressures of both the columns can be between about 0.5 atm to about 12 atm, or about 7 atm. In addition, both options can be combined into a single column with the water acetic acid stream as a distillate, acetic acid as a bottom product, and the formic acid acetic acid purge as a side-draw. A combined column’s operating pressure can be between about 0.5 atm to about 12 atm, or about 7 atm. [00107] Another schematic process flowsheet example is shown in Figure 12 in which high purity acetic acid product can be recovered with the use of an entrainer (e.g., ethyl acetate, etc.), along with a small amount of formic acid byproduct impurity. The feed streams, reactor, and lights separation are the same as described with respect to Figures 9 and 10. In this example with the formation of formic acid, when the entrainer is used to separate water and acetic acid, additional columns can be used to obtain high purity water (e.g., 99.9 wt% or greater water) and high purity acetic acid (e.g., 99.9 wt% or greater acetic acid) products. Formic acid, acetic acid, and water are removed in a side-draw from the acetic acid separation column 1202, which are further treated to remove a formic acid and acetic acid via a purge stream (with 1% loss of acetic acid) and pure acetic acid product. [00108] For separation sequences with or without entrainer, the lights column used for degassing can also be replaced, depending on the separation sequence, with various configurations. For example, a partial condenser followed by a flash vessel/reflux accumulator can be used instead of the lights column. Any dissolved gases can be removed in the vapor phase, while light reaction intermediates such as ethanol and acetaldehyde can be recovered in the liquid phase and recycled back to the reactor. Other options can include a three-phase decanter, a flash vessel, and/or a vent on the extraction column. [00109] Figures 13A and 13B illustrate alternate column configurations showing the gas vent addition to the water column. In Figure 13A, the light reaction intermediates can be recovered in the acetic acid-water distillate product, while in Figure 13B they can be recovered separately as the distillate (lights recycle), while the acetic-acid water recycle is recovered as a side stream from the column. [00110] Figure 14 illustrates an extension of Figure 13A to the entire separation sequence. The general sequence can include any of those shown in Figures 10-11, and the corresponding components can be the same or similar to those described above with respect to Figures 10 and 11. Figure 14 illustrates the separation of acetic acid product from water with no entrainer, without a degassing column, and without a separate lights recycle. The light reaction intermediates can be recovered in the water-acetic acid distillate and recycled to the reactor after an aqueous purge to remove the water generated in the reactor. [00111] More specifically, Figure 14 illustrates a process flowsheet for the separation of acetic acid and water (and containing formic acid by product impurity). The feed streams and reactor configurations can be the same or similar to the arrangement as described with respect to Figure 11. However, the degassing or lights column can be removed and a gas vent stream 1404 can be introduced on the water column 1402. In this case, the light reaction intermediates can be recycled to the reactor 1406 within the water-acetic acid recycle. Typical operating pressures within the water column 1402 can be between about 0.5 atm to 12 atm, or about 7 atm. The acetic acid column 1408 can be operated at or near atmospheric pressure. [00112] Figure 15 illustrates an extension of Figure 13B to the entire separation sequence. The general sequence can include any of those shown in Figures 10-11, and the corresponding components can be the same or similar to those described above with respect to Figures 10 and 11. Figure 15 shows the separation of acetic acid product from water with no entrainer, without a degassing column but with a lights recycle (comprising primarily light reaction intermediates) to the reactor and an optional organic purge to remove any light reaction by-products and impurities from the process. Figure 15 shows a configuration that is similar to that shown in Figure 14 (where like components can be the same or similar) but with a separate lights recycle in stream 1502 and an optional organic purge in stream 1504. Typical operating pressures within the water column 1506 can be between about 0.5 atm to 12 atm, or about 7 atm. The acetic acid column 1508 can be operated at about atmospheric pressure. [00113] When no entrainer is used (e.g., in any of the schemes in Figures 10-15), water can be recovered as the distillate of the water column 1506 and recycled back to the reactor after a purge. While it is theoretically possible to achieve a pure (>99%) water distillate, such recovery may not be practical or economical, and the distillate can contain some acetic acid, and possibly some amount of formic acid as well. Consequently, the aqueous purge can result in a small acetic acid loss, and may be further separated (e.g., using azeotropic distillation) in order to increase the overall acetic acid recovery. [00114] A schematic of a process flowsheet is shown in Figure 16. The feed streams and reactor can be the same or similar to those shown in the same as in Figure 12, and like components will not be re-described in the interest of brevity. The main difference in Figure 12 is that the degassing or lights column can be removed and a gas vent can be introduced on the extractor. In this embodiment, the bulk of the light reaction intermediates can be recycled to the reactor within the water recycle, while a small fraction may be lost with the ethyl acetate purge. Unlike the configuration in Figure 12, the formic acid and acetic acid can be removed as a bottom product from the ethyl acetate removal column 1602, whereas ethyl acetate and water can be removed as a distillate of the same. The formic acid can be purged from the distillate of the next column 1604 (with a small loss of acetic acid) and pure or nearly pure acetic acid product can be obtained as a bottom product. To reduce the energy consumption of the water separation column 1606, some of the water (saturated with ethyl acetate) can be recycled to the reactor before this distillation. [00115] In any of the embodiments described herein, products or byproducts having a heavier molecular mass than acetic acid may be produced when hydrocarbons heavier than ethane are present in the feed to the reaction. Any byproducts heavier than acetic acid can pass through the separation system and be present in the acetic acid product stream. Any suitable downstream separation can be used to produce high purity acetic acid by removing heavier byproducts from the acetic acid such as distillation, extraction, and the like. [00116] Another schematic of the process is shown in Figure 17. This flow sheet is similar to the flowsheet shown in Figure 10. Feed streams, reactor and separation columns are the same as Figure 10 but with an absorber 1702 on the gas exiting the reactor and a gas exit stream instead of a gas recycle. [00117] In some aspect, any of the separation schemes described herein can be used with the membrane reactor. Due to the presence of two separate stream flows from the cathode and anode sides of the membrane reactor and the specific water purity requirements on the anode side, some specific separation sequences can be used. [00118] As shown in Figure 18, water can be fed to the anode side 604 of the reactor, where it can be converted to oxygen via electrolysis. The stream 1802 exiting the anode side 604 can be separated in a gas-liquid separator 1804 to yield a water stream 1806 that is recycled to the anode side 604 of the reactor, and a gas stream 1808 comprising oxygen. The gas stream 1808 can be compressed and recycled to the cathode side 606 of the reactor (as shown in Figure 18), or alternatively, may be sold as a separate product. Ethane can be mixed with air and recycled oxygen, and then humidified using either a fraction of the liquid stream leaving the reactor and/or recycled water from the water separation column 1810. The humidified stream can then be fed to the cathode side 606 of the reactor where it can react to form acetic acid, water, reaction intermediates such as ethanol and acetaldehyde, and potentially by-products such as formic acid. [00119] The stream 1812 exiting the cathode side 606 of the reactor can be either a vapor or a mixed vapor liquid mixture. This stream 1812 can be cooled and separated in a gas liquid separator 1814 to yield a vapor stream 1816 and a liquid stream 1818. The vapor stream 1816 can comprise unreacted ethane, air saturated with water, reaction intermediates, and products. The vapor stream 1816 can be sent to the absorber 1820, where water can be used as an absorbent to recover acetic acid present in this stream 1816. A fraction of the gas as stream 1822 leaving the absorber 1820 can be compressed and recycled to the reactor, while the rest can be purged from the process and may be used as fuel for the process. [00120] The liquid stream 1818 leaving the vapor liquid separator 1814 can comprise water, acetic acid, reaction by-products, and intermediates. A fraction of this stream may be used to humidify the gas stream entering the cathode side 606 of the reactor in the humidifier 1824. Any liquid leaving the humidifier 1824 can be mixed with the liquid stream 1818 leaving the separator 1814 as well as the liquid stream 1826 from the absorber 1820, and the combined stream can be sent to a liquid-liquid extractor 1828. The extractor 1828 could be either a multiple stage column or a single stage decanter. In the extractor 1828, the acetic acid rich liquid stream can be combined with an entrainer rich stream to yield an organic stream comprising acetic acid and the entrainer, and an aqueous stream comprising water and the entrainer. The entrainer can be any of those described herein such as ethyl acetate. The organic stream can be sent to a distillation column 1830 (e.g., an acetic acid separation column), where acetic acid, along with formic acid and other heavy by-products/impurities can be recovered as the bottoms product. This stream may need to be further purified in an additional distillation column to achieve the desired product purity. The distillate from the acetic acid separation column can be recycled to the extractor 1828. The aqueous stream from the extractor 1828 can be sent to a different distillation column (e.g., a water separation column 1810) where high purity water can be recovered as the bottoms product. Since net water is produced in the reaction, a fraction of the water stream can exit the process and be sent to waste treatment. In addition, a fraction can also be recycled to the absorber 1820, and possibly the humidifier 1824. Finally, a fraction may be optionally further purified in a membrane unit or other water purification system 1832 such as a an RO (Reverse Osmosis) unit followed by optional ion exchange beds and then used as feed to the anode side of the reactor. The distillate from the water separation column 1810 can be recycled to the extractor 1828. EXAMPLES [00121] The subject matter having been generally described, the following examples are given as particular aspects of the disclosure and are included to demonstrate the practice and advantages thereof, as well as preferred aspects and features of the inventions. It is understood that the examples are given by way of illustration and are not intended to limit the specification of the claims to follow in any manner. EXAMPLE 1 [00122] As an example of the process, the process Flowsheet shown in Figure 19 shows a simulated process flow that was simulated using Aspen Plus process design software, version V11. The simulated process is similar to the schematic for the process shown in Figure 9. Feed streams are indicated as follows: GAS (with a composition of 5%v/v Methane, 90% v/v Ethane and 5% v/v Propane), AIR (79% N2, 21% O2), CAT (catalyst), and ETAC (entrainer Ethyl Acetate makeup stream). [00123] GAS and AIR streams are introduced in the REACTOR along with the dissolved catalyst stream. Gas outlet from the reactor is sent to GASMEMB, where the unreacted hydrocarbon gases are recycled back by S22 to the feed gas stream with a 1% purge in stream S21, and the air vent in stream S20. [00124] Feed streams are heated to the reaction temperature of 50 ^◦ C and pressurized to reaction pressure of 10atm. [00125] The liquid outlet from the reactor is first depressurized in valve V1 and is sent to CATSEP where the catalyst is separated from the stream and is sent further to separation system as stream S1. LIGHTS column separates dissolved gases in streams S2, S3. Stream S3 mostly contains light intermediates ethanol and acetaldehyde along with acetic acid product, which can be recycled back to the reactor. Bottom stream S4 has a composition of 55wt% Water and 44wt% acetic acid, remaining 1% being intermediates from the process. The column is operated at 1atm pressure and distillate and bottoms temperatures are 30 ^◦ C and 105 ^◦ C respectively. [00126] Stream S4 is cooled down to 30 ^◦ C in heat exchanger HE-5 before being fed to EXTRACT unit along with ethyl acetate, which is also cooled to 30 ^◦ C in HE-4. Recycled ethyl acetate stream S16 is mixed with makeup ethyl acetate in mixer M1. The extractor unit consists of 10 stages and is operated at 30 ^◦ C. [00127] The aqueous phase from the EXTRACT unit is stream S7 which then connects to the water purification column W-PUR, whereas the organic phase stream S11 from the extractor goes to the acetic acid purification column AA-SEP. Both columns are operated at atmospheric pressure. Pure water stream of composition 99.9wt% is obtained from the bottom of the column W-PUR in stream S10 at 123 ^◦ C. The pure acetic acid product is 99.9wt% is the bottoms product of AA-SEP in S13 at 126 ^◦ C. Distillate of both the W-PUR (stream S9 at 92 ^◦ C) and of AA-SEP (stream S10 at 30 ^◦ C) are ethyl acetate/water streams of composition 91wt% ethyl acetate approx. which are recycled back to mixer M4 with a 1% purge out in unit RCY2. Water purge ratio is adjusted in unit RCY3. [00128] The overall mass balance with the inlet and outlet streams is shown in Figure 20 for the flowsheet described above and in Figure 19. EXAMPLE 2 [00129] As an example of the process, the process flowsheet shown in Figure 21 shows a simulated process flow that was simulated using Aspen Plus process design software, version V11. The simulated process is similar to the schematic for the process shown in Figure 18. [00130] Feed streams are indicated as follows: GAS (with a composition of 99.5% v/v Ethane and 0.5% v/v Propane), AIR (79% N2, 21% O2), CAT (catalyst), and W-IN (Water makeup stream). [00131] GAS and AIR streams are introduced in the REACTOR along with the dissolved catalyst stream. Gas outlet from the reactor is sent to flash drum F1, where the gas and liquid phases are separated. The unreacted hydrocarbon gases are sent to the absorber ABS, where they contact with the recycled water stream S3-RCY from the AA-SEP1 and exit from the process as GAS-OUT1, which comprises of 27 % Ethane, 64% N2, 5% O2 and 1% Water. Acetic acid to the feed of the absorber is scrubbed out from 118 kg/h to 5 kg/h. [00132] Feed streams are pre-heated to the reaction temperature of 50⁰C and pressurized to reaction pressure of 10atm. [00133] The liquid outlet from the reactor is sent to CATSEP where the catalyst is separated from the stream and is sent further to separation system as S1. STO-V1 is a storage unit with a vent. [00134] Stream S1 is the feed to the water removal column AA-SEP1, wherein 92wt% water (containing 5wt% acetic acid, 1% acetaldehyde) is removed in the distillate S3 at 50⁰C and formic Acid-acetic acid mixture is the bottoms product at 195⁰C is sent to second column AA-SEP2. Distillate S3 is sent to splitter R2 where 62% water is recycled and the rest purged out in stream S3-OUT. Stream S3-RCY is recycled to the absorber ABS. Column AA-SEP1 is operated at 7atm, whereas column AA-SEP2 is operated at atmospheric pressure. The pure acetic acid product is 99.96wt% is the bottoms product of AA-SEP2 in S9 at 118⁰C. Distillate of AA-SEP2 (stream S8 at 30⁰C) is the formic acid and acetic acid, with a flow of 300kg/h and a composition of 56wt% formic acid and 39wt% acetic acid approx. which are purged out. [00135] The overall mass balance with the inlet and outlet streams is shown in Figure 22 for the flowsheet described above and in Figure 21. [00136] Having described various processes and systems, certain aspects can include, but are not limited to: [00137] In a first aspect, a reactor for converting hydrocarbon gases comprises: a reactor vessel; a structured filling disposed within the reactor, wherein the structured filling is electrically coupled to a current source and configured to serve as a cathode within the reactor vessel; and at least one anode disposed within the reactor vessel. [00138] A second aspect can include the reactor of the first aspect, wherein the structured filling is formed from a metal. [00139] A third aspect can include the reactor of the first or second aspect, wherein the structured filling is a mesh, a gauze, a screen, a structured packing, or any combination thereof. [00140] A fourth aspect can include the reactor of any one of the first to third aspects, wherein the structured filling has a surface area ranging from about 100 to about 1000 m2/m3. [00141] A fifth aspect can include the reactor of any one of the first to fourth aspects, further comprising: a filtration media disposed within the reactor vessel, wherein the filtration media is disposed between an interior of the reactor vessel and a fluid outlet. [00142] A sixth aspect can include the reactor of the fifth aspect, wherein the filtration media comprises a membrane, a filter, a screen, or any combination thereof. [00143] A seventh aspect can include the reactor of the fifth or sixth aspect, wherein the filtration media comprises a sheet or tube of the filtration media. [00144] An eighth aspect can include the reactor of any one of the first to seventh aspects, wherein the reactor is configured to accept a gas in a lower portion of the reactor and a liquid in the upper portion of the reactor, and wherein the reactor is configured to contact the gas with the liquid in a countercurrent flow within the reactor vessel. [00145] A ninth aspect can include the reactor of any one of the first to seventh aspects, 9further comprising: a mixer disposed in the reactor vessel, wherein the mixer is configured to circulate the fluid in the reactor vessel. [00146] In a tenth aspect, a method for converting hydrocarbon gases comprises: providing a gas stream comprising a hydrocarbon to a lower portion of a reactor, wherein the reactor comprises a reactor vessel, a structured filling disposed within the reactor, wherein the structured filling is electrically coupled to a current source and configured to serve as a cathode within the reactor vessel; and at least one anode disposed within the reactor vessel; providing a liquid stream to an upper portion of the reactor; contacting the gas stream with the liquid stream in a countercurrent flow within the reactor vessel; and converting at least a portion of the hydrocarbon to a product within the reactor based on contacting the gas stream with the liquid stream. [00147] An eleventh aspect can include the method of the tenth aspect, wherein the structured filling is formed from a metal. [00148] A twelfth aspect can include the method of the tenth or eleventh aspect, wherein the structured filling is a mesh, a gauze, a screen, a structured packing, or any combination thereof. [00149] A thirteenth aspect can include the method of any one of the tenth to twelfth aspects, wherein the structured filling has a surface area ranging from about 100 to about 1000 m2/m3. [00150] A fourteenth aspect can include the method of any one of the tenth to thirteenth aspects, wherein the reactor is configured to accept a gas in a lower portion of the reactor and a liquid in the upper portion of the reactor, and wherein the reactor is configured to contact the gas with the liquid in a countercurrent flow within the reactor vessel. [00151] A fifteenth aspect can include the method of any one of the tenth to fourteenth aspects, wherein the gas stream comprises the hydrocarbon and oxygen, and wherein the product comprises acetic acid. [00152] A sixteenth aspect can include the method of any one of the tenth to fourteenth aspects, further comprising: providing a second gas stream comprising oxygen to the reactor. [00153] A seventeenth aspect can include the method of any one of the tenth to sixteenth aspects, wherein the liquid stream comprises a catalyst. [00154] An eighteenth aspect can include the method of the seventeenth aspect, wherein the catalyst is a heterogeneous catalyst that forms a slurry with the liquid. [00155] A nineteenth aspect can include the method of any one of the tenth to eighteenth aspects, wherein the liquid stream comprises a solvent configured to increase the solubility of the hydrocarbon in the liquid. [00156] A twentieth aspect can include the method of the nineteenth aspect, wherein the solvent comprises acetic acid, formic acid, diethyl ether, 1,4-dioxane, ethyl acetate, methanol, tertiary butanol, acetone, or any combination thereof. [00157] A twenty first aspect can include the method of any one of the tenth to twentieth aspects, further comprising: maintaining a pressure, temperature, or both of the reactor to increase a solubility of the hydrocarbon in the liquid. [00158] A twenty second aspect can include the method of any one of the tenth to twenty first aspects, further comprising: filtering at least a portion of the liquid within the reaction vessel; and removing the portion of the liquid that is filtered from the reaction vessel as a product stream. [00159] A twenty third aspect can include the method of any one of the tenth to twenty second aspects, further comprising: mixing the gas stream and the liquid stream within the reactor. [00160] A twenty fourth aspect can include the method of any one of the tenth to twenty third aspects, wherein the reactor is operated at a pressure between about 1 to 100 bar, and at a temperature at about 15⁰C to 300⁰C. [00161] In a twenty fifth aspect, a reactor for converting hydrocarbon gases comprises: a reactor vessel comprising a plurality of tubes disposed within a shell; wherein at least a portion of the tubes of the plurality of tubes are electrically coupled to a current source and configured to serve as a cathode within the reactor vessel; at least one anode disposed within the shell; wherein the reactor vessel is configured to accept one or more gas streams comprising a hydrocarbon gas and oxygen and a liquid stream. [00162] A twenty sixth aspect can include the reactor of the twenty fifth aspect, wherein the shell is configured to accept a heat exchange fluid within the reactor, and wherein the plurality of tubes is configured to accept the gas stream and the liquid stream. [00163] A twenty seventh aspect can include the reactor of the twenty fifth aspect, wherein the plurality of tubes is configured to accept a heat exchange fluid within the reactor, and wherein the tubes are configured to accept a heat exchange fluid. [00164] A twenty eighth aspect can include the reactor of any one of the twenty fifth to twenty seventh aspects, wherein the plurality of tubes are formed from carbon. [00165] A twenty ninth aspect can include the reactor of the twenty eighth aspect, wherein the carbon comprises graphite. [00166] A thirtieth aspect can include the reactor of any one of the twenty fifth to twenty ninth aspects, wherein at least a portion of the tubes of the plurality of tubes are coated with platinum, carbon, or a combination thereof. [00167] A thirty first aspect can include the reactor of any one of the twenty fifth to thirtieth aspects, further comprising: insulation disposed about at least a portion of the reactor vessel. [00168] A thirty second aspect can include the reactor of any one of the twenty fifth to thirty first aspects, wherein the reactor is operated at a pressure between about 1 to 100 bar, and at a temperature at about 15⁰C to 300⁰C. [00169] In a thirty third aspect, a method for converting hydrocarbon gases comprises: providing a gas stream comprising a hydrocarbon to a lower portion of a reactor, wherein the reactor comprises a reactor vessel comprising a plurality of tubes disposed within a shell; wherein at least a portion of the tubes of the plurality of tubes are electrically coupled to a current source and configured to serve as a cathode within the reactor vessel; and at least one anode disposed within the reactor vessel; providing a liquid stream to an upper portion of the reactor; contacting the gas stream with the liquid stream in a countercurrent flow within the reactor vessel; and converting at least a portion of the hydrocarbon to a product within the reactor based on contacting the gas stream with the liquid stream. [00170] A thirty fourth aspect can include the method of the thirty third aspect, wherein the shell is configured to accept a heat exchange fluid within the reactor, and wherein the plurality of tubes is configured to accept the gas stream and the liquid stream. [00171] A thirty fifth aspect can include the method of the thirty third aspect, wherein the plurality of tubes is configured to accept a heat exchange fluid within the reactor, and wherein the tubes are configured to accept a heat exchange fluid. [00172] A thirty sixth aspect can include the method of any one of the thirty third to thirty fifth aspects, wherein the plurality of tubes are formed from carbon. [00173] A thirty seventh aspect can include the method of the thirty sixth aspect, wherein the carbon comprises graphite. [00174] A thirty eighth aspect can include the method of any one of the thirty third to thirty seventh aspects, wherein the gas stream comprises the hydrocarbon and oxygen, and wherein the product comprises acetic acid. [00175] A thirty ninth aspect can include the method of any one of the thirty third to thirty eighth aspects, further comprising: providing a second gas stream comprising oxygen to the reactor. [00176] A fortieth aspect can include the method of any one of the thirty third to thirty ninth aspects, wherein the liquid stream comprises a catalyst. [00177] A forty first aspect can include the method of the fortieth aspect, wherein the catalyst is a heterogeneous catalyst that forms a slurry with the liquid. [00178] A forty second aspect can include the method of any one of the thirty third to forty first aspects, wherein the liquid stream comprises a solvent configured to increase the solubility of the hydrocarbon in the liquid. [00179] A forty third aspect can include the method of the forty second aspect, wherein the solvent comprises acetic acid, formic acid, diethyl ether, 1,4-dioxane, ethyl acetate, methanol, tertiary butanol, acetone, or any combination thereof. [00180] A forty fourth aspect can include the method of any one of the thirty third to forty third aspects, further comprising: filtering at least a portion of the liquid within the reaction vessel; and removing the portion of the liquid that is filtered from the reaction vessel as a product stream. [00181] A forty fifth aspect can include the method of any one of the thirty third to forty fourth aspects, further comprising: mixing the gas stream and the liquid stream within the reactor. [00182] A forty sixth aspect can include the method of any one of the thirty third to forty fifth aspects, wherein the reactor is operated at a pressure between about 1 to 100 bar, and at a temperature at about 15⁰C to 300⁰C. [00183] In a forty seventh aspect, a reactor system for converting hydrocarbon gases comprises: a reactor vessel comprising at least one cathode and at least one anode; a nozzle configured to inject a fluid into the reactor vessel; and a pump in fluid communication with and configured to supply the fluid to the nozzle; wherein the reactor vessel is configured to accept one or more gas streams comprising a hydrocarbon gas and oxygen and a liquid stream. [00184] A forty eighth aspect can include the reactor system of the forty seventh aspect, wherein the nozzle is configured to inject a liquid through a gas phase in the reactor vessel and entrain the gas phase into the liquid stream within the reactor vessel. [00185] A forty ninth aspect can include the reactor system of the forty eighth aspect, further comprising: internal baffles disposed within the reactor vessel, wherein the internal baffles are configured to direct the entrained gas to a lower portion of the reactor vessel and allow the entrained gas to rise through a separate flow path. [00186] A fiftieth aspect can include the reactor system of any one of the forty seventh to forty ninth aspects, further comprising a fluid outlet in the reactor vessel, wherein the fluid outlet is in fluid communication with an inlet of the pump. [00187] In a fifty first aspect, a method for converting hydrocarbon gases comprises: providing a gas stream comprising a hydrocarbon to a reactor vessel, wherein the reactor comprises a reactor vessel comprising at least one cathode and at least one anode; injecting a liquid stream into the reactor through a gas phase, wherein the gas phase is formed by at least a portion of the gas stream; entraining at least a portion of the gas phase into a liquid phase in the reactor, wherein the liquid phase is formed by the liquid stream within the reactor; contacting the gas phase with the liquid phase within the reactor based on the entraining; and converting at least a portion of the hydrocarbon to a product within the reactor based on contacting the gas phase with the liquid phase in the reactor. [00188] A fifty second aspect can include the method of the fifty first aspect, wherein the nozzle is configured to inject a liquid through a gas phase in the reactor vessel and entrain the gas phase into the liquid stream within the reactor vessel. [00189] A fifty third aspect can include the method of the fifty second aspect, further comprising: internal baffles disposed within the reactor vessel, wherein the internal baffles are configured to direct the entrained gas to a lower portion of the reactor vessel and allow the entrained gas to rise through a separate flow path. [00190] A fifty fourth aspect can include the method of any one of the fifty first to fifty third aspects, further comprising a fluid outlet in the reactor vessel, wherein the fluid outlet is in fluid communication with an inlet of the pump. [00191] A fifty fifth aspect can include the method of any one of the fifty first to fifty fourth aspects, wherein the gas stream comprises the hydrocarbon and oxygen or air, and wherein the product comprises acetic acid. [00192] A fifty sixth aspect can include the method of any one of the fifty first to fifty fifth aspects, further comprising: providing a second gas stream comprising oxygen to the reactor. [00193] A fifty seventh aspect can include the method of any one of the fifty first to fifty sixth aspects, wherein the liquid stream comprises a catalyst. [00194] A fifty eighth aspect can include the method of the fifty seventh aspect, wherein the catalyst is a heterogeneous catalyst that forms a slurry with the liquid. [00195] A fifty ninth aspect can include the method of any one of the fifty first to fifty eighth aspects, wherein the liquid stream comprises a solvent configured to increase the solubility of the hydrocarbon in the liquid. [00196] A sixtieth aspect can include the method of the fifty ninth aspect, wherein the solvent comprises acetic acid, formic acid, diethyl ether, 1,4-dioxane, ethyl acetate, methanol, tertiary butanol, acetone, or any combination thereof. [00197] A sixty first aspect can include the method of any one of the fifty first to sixtieth aspects, further comprising: filtering at least a portion of the liquid within the reaction vessel; and removing the portion of the liquid that is filtered from the reaction vessel as a product stream. [00198] A sixty second aspect can include the method of any one of the fifty first to sixtieth aspects, further comprising: removing at least a portion of the liquid phase from the reactor; and separating a catalyst from the portion of the liquid phase removed from the reactor. [00199] A sixty third aspect can include the method of the sixth second aspect, wherein separating the catalyst from the portion of the liquid phase uses an ion-exchange resin bed, crystallization, electrostatic precipitation, dissolved gas flotation, a hydrocyclones, or a centrifuge. [00200] A sixty fourth aspect can include the method of any one of the fifty first to sixty third aspects, wherein the reactor is operated at a pressure between about 1 to 100 bar, and at a temperature at about 15⁰C to 300⁰C. [00201] In a sixty fifth aspect, a method of producing acetic acid comprises: providing a gas comprising a hydrocarbon gas and oxygen/air to a reactor; contacting the gas with a liquid phase comprising a catalyst in the presence of a potential difference applied across a cathode and an anode; producing acetic acid based on the contacting, wherein the acetic acid is dissolved in the liquid phase; and separating the acetic acid from the liquid phase to produce an acetic acid product stream. [00202] A sixty sixth aspect can include the method of the sixty fifth aspect, wherein the hydrocarbon gas comprises methane, ethane, propane, butane(s), ethylene, or combinations thereof. [00203] A sixty seventh aspect can include the method of the sixty fifth or sixty sixth aspect, further comprising: separating any dissolved gaseous components and the catalyst from the acetic acid product stream to produce a liquid stream. [00204] A sixty eighth aspect can include the method of the sixty seventh aspect, wherein separating the acetic acid from the liquid phase comprises: distilling the liquid stream to remove at least a portion of the liquid phase from the acetic acid and produce an acetic acid product. [00205] A sixty ninth aspect can include the method of the sixty seventh aspect, wherein separating the acetic acid from the liquid phase comprises: distilling the liquid stream using azeotropic distillation to remove at least a portion of the liquid phase from the acetic acid and produce an acetic acid product. [00206] A seventieth aspect can include the method of the sixty ninth aspect, wherein distilling the liquid stream using azeotropic distillation comprises: introducing the liquid stream to a first distillation column; providing an entrainer within the first distillation column or to a separate decanter during the distillation; separating the acetic acid product during the distillation; recovering the entrainer from a second distillation column; and recycling at least a portion of the entrainer to the first distillation column or the decanter during the distillation. [00207] A seventy first aspect can include the method of the sixty seventh aspect, wherein separating the acetic acid from the liquid phase comprises: contacting the liquid stream with an extractant; solvating at least a portion of the acetic acid in the liquid stream in the extractant to produce a rich extractant; and distilling the rich extractant to produce an acetic acid product. [00208] A seventy second aspect can include the method of the sixty seventh aspect, wherein separating the acetic acid from the liquid phase comprises: distilling the liquid stream using liquid-liquid extraction followed by distillation to remove at least a portion of the liquid phase from the acetic acid and produce an acetic acid product. [00209] A seventy third aspect can include the method of any one of the sixty seventh to seventy second aspects, further comprising: producing a water stream from the liquid phase during the separating; and recycling a first portion of the water stream to the reactor, where a second portion of the water stream is removed from the process. [00210] A seventy fourth aspect can include the method of the seventy third aspect, wherein the water stream comprises acetic acid, wherein producing the water stream comprises: distilling the water stream in a distillation column without the use of an entrainer. [00211] A seventy fifth aspect can include the method of any one of the sixty seventh to seventy fourth aspects, further comprising: separating a hydrocarbon recycle stream from the separation of the dissolved gaseous components from the acetic acid product stream; and recycling at least a portion of the hydrocarbon recycle stream to the reactor. [00212] A seventy sixth aspect can include the method of any one of the sixty fifth to sixty seventh aspects, wherein the liquid phase comprises formic acid, water, and the acetic acid, and wherein separating the acetic acid from the liquid phase comprises: distilling the liquid phase to separate the water from an intermediate stream, wherein the intermediate stream comprises acetic acid and formic acid; and distilling the intermediate stream to produce a first stream comprising acetic acid, and a second stream comprising a majority of the formic acid and acetic acid. [00213] A seventy seventh aspect can include the method of the seventy sixth aspect, wherein distilling the liquid phase occurs at a pressure above atmospheric pressure. [00214] A seventy eighth aspect can include the method of any one of the sixty fifth to sixty seventh aspects, wherein the liquid phase comprises formic acid, water, and the acetic acid, and wherein separating the acetic acid from the liquid phase comprises: separating the liquid stream to remove a first overhead stream and a first bottoms stream in a first column, wherein the first overhead stream comprises a majority of the water, and wherein the first bottoms stream comprises a majority of the acetic acid and formic acid; separating the first bottoms stream in a second column to produce a second overhead product and a second bottoms stream, wherein the second overhead stream comprises the formic acid and a portion of the acetic acid, and wherein the second bottoms stream comprises a majority of the acetic acid in the first bottoms stream. [00215] A seventy ninth aspect can include the method of the seventy eighth aspect, wherein the second bottoms stream is at least 99 wt.% acetic acid. [00216] An eightieth aspect can include the method of any one of the sixty fifth to sixty seventh aspects, wherein the liquid phase comprises formic acid, water, and the acetic acid, and wherein separating the acetic acid from the liquid phase comprises: separating the liquid stream to remove a first overhead stream and a first bottoms stream in a first column, wherein the first overhead stream comprises a majority of the water and formic acid, and wherein the first bottoms stream comprises a majority of the acetic acid; separating the first overhead stream in a second column to produce a second overhead product and a second bottoms stream, wherein the second overhead stream comprises the water and a portion of the acetic acid, and wherein the second bottoms stream comprises a majority of the formic acid in the first overhead stream. [00217] An eighty first aspect can include the method of any one of the sixty fifth to sixty seventh aspects, wherein the liquid phase comprises formic acid, water, and the acetic acid, and wherein separating the acetic acid from the liquid phase comprises: separating the liquid stream to remove a first overhead stream, a first side stream, and a first bottoms stream in a first column, wherein the first overhead stream comprises a majority of the water, wherein the first bottoms stream comprises a majority of the acetic acid, and wherein the first side draw stream comprises a majority of the formic acid. [00218] An eighty second aspect can include the method of the seventy seventh aspect, further comprising: contacting the liquid stream with an extractant; solvating at least a portion of the acetic acid in the liquid stream in the extractant to produce a rich extractant and a lean liquid stream; distilling the rich extractant to produce a product stream and a first extractant stream; distilling the lean liquid stream to produce a water stream and a second extractant stream; combining the first extractant stream with the second extractant stream; and distilling the product stream to produce an acetic acid stream and a formic acid stream, where the formic acid stream comprises primarily formic acid and a minor amount of acetic acid. [00219] An eighty third aspect can include the method of the seventy seventh aspect, further comprising: contacting the liquid stream with an extractant; solvating at least a portion of the acetic acid in the liquid stream in the extractant to produce a rich extractant and a lean liquid stream; distilling the rich extractant to produce a product stream as a bottoms stream, a formic acid stream as a side draw stream, and a first extractant stream as an overhead stream; distilling the lean liquid stream to produce a water stream and a second extractant stream; distilling the side draw stream to produce a second formic acid stream as a bottoms stream and a third extractant stream as an overhead stream; combining the first extractant stream, the second extractant stream, and the third extractant stream; distilling second formic acid stream to produce a second product stream as a bottom stream and a third formic acid stream; and combining the first product stream and the second product stream. [00220] An eighty fourth aspect can include the method of the sixty fifth or sixty sixth aspect, further comprising: separating the catalyst from the acetic acid product stream to produce a liquid stream. [00221] An eighty fifth aspect can include the method of the eighty fourth aspect, further comprising: separating the liquid stream into an overhead stream and a bottoms stream, wherein the bottoms stream comprises a majority of the acetic acid in the liquid stream; and at least partially condensing the overhead stream to produce a liquid stream and a gas stream, wherein the liquid stream comprises a majority of the water in the liquid stream. [00222] An eighty sixth aspect can include the method of the eighty fourth aspect, further comprising: separating the liquid stream into an overhead stream, a bottoms stream, and a side draw stream, wherein the bottoms stream comprises a majority of the acetic acid in the liquid stream, and wherein the side draw stream comprises a majority of the water in the liquid stream; and separating the overhead stream to produce a lights recycle stream and a gas stream. [00223] An eighty seventh aspect can include the method of the eighty fifth or eighty sixth aspect, further comprising: recycling the gas stream to the reactor. [00224] An eighty eighth aspect can include the method of the eighty sixth aspect, further comprising: recycling the light recycle stream to the reactor. [00225] An eighty ninth aspect can include the method of any one of the eighty fifth to eighty eighth aspects, further comprising: separating the bottoms stream into an acetic acid product stream and a formic acid product stream, wherein the acetic acid product stream comprises the majority of the acetic acid in the liquid stream. [00226] A ninetieth aspect can include the method of the eighty ninth aspect, wherein separating the bottoms stream into the acetic acid product stream and the formic acid product stream occurs at a lower pressure than separating the liquid stream into the overhead stream and the bottoms stream. [00227] A ninety first aspect can include the method of the eighty ninth aspect, wherein separating the bottoms stream into the acetic acid product stream and the formic acid product stream occurs at a pressure at or about atmospheric pressure. [00228] A ninety second aspect can include the method of any one of the eighty ninth to ninety first aspects, wherein separating the liquid stream into the overhead stream and the bottoms stream occurs at a pressure between about 0.5 atm and about 12 atm. [00229] A ninety third aspect can include the method of the eighty fourth aspect, further comprising: contacting the liquid stream with an extractant in an extraction column or a decanter; solvating at least a portion of the acetic acid in the liquid stream in the extractant to produce a rich extractant and a lean liquid stream; separating a gas stream from the extraction column; distilling the rich extractant to produce a product stream and a first extractant stream; distilling a first portion of the lean liquid stream to produce a water stream and a second extractant stream; combining the first extractant stream with the second extractant stream; and distilling the product stream to produce an acetic acid stream and a formic acid stream, where the formic acid stream comprises primarily formic acid and a minor amount of acetic acid. [00230] A ninety fourth aspect can include the method of the ninety first aspect, further comprising: recycling a second portion of the lean liquid to the reactor. [00231] In a ninety fifth aspect, an electrochemical reactor comprises: an ion exchange membrane; an anode; and a cathode, wherein the anode and the cathode are on opposite sides of the ion exchange membrane, wherein the anode comprises a first catalyst in contact with an anode gas diffusion layer, and wherein the cathode comprises a second catalyst in contact with a cathode gas diffusion layer; an anode flow plate, wherein the anode is disposed between the anode flow plate and the ion exchange membrane; and a cathode flow plate, wherein the cathode is disposed between the cathode flow plate and the ion exchange membrane. [00232] A ninety sixth aspect can include the reactor of the ninety fifth aspect, wherein the ion exchange membrane is gas impermeable. [00233] A ninety seventh aspect can include the reactor of the ninety fifth or ninety sixth aspect, wherein the anode flow plate and the cathode flow plate each comprise one or more channels for liquid distribution. [00234] A ninety eighth aspect can include the reactor of any one of the ninety fifth to ninety seventh aspects, wherein the second catalyst is affixed to a catalyst support layer, and wherein the catalyst support layer is in contact with the cathode gas diffusion layer. [00235] A ninety ninth aspect can include the reactor of any one of the ninety fifth to ninety eighth aspects, wherein at least one of the anode gas diffusion layer or the cathode gas diffusion layer is formed from a hydrophobic material. [00236] A one hundredth aspect can include the reactor of any one of the ninety fifth to ninety ninth aspects, further comprising: a cathode end plate disposed in contact with the cathode flow plate, wherein the cathode end plate defines a cooling media flowpath configured to cool the reactor. [00237] A one hundred first aspect can include the reactor of any one of the ninety fifth to one hundredth aspects, wherein the ion exchange membrane has large dimensions than the anode or the cathode, and wherein a seal is formed between the anode, the cathode, and the ion exchange membrane at the surface of the ion exchange membrane. [00238] In a one hundred second aspect, a method for converting hydrocarbon gases comprises: providing a gas stream comprising a hydrocarbon to a cathode in a reactor, wherein the reactor comprises the cathode and an anode, where the cathode and the anode are separated by an ion exchange membrane; generating protons at the anode; passing the protons through the ion exchange membrane to the cathode; converting at least a portion of the hydrocarbon to a product within the cathode to for a product stream, wherein the converting is based on contacting the hydrocarbon with a first catalyst and the protons at the cathode; and passing the product stream out of the cathode. [00239] A one hundred third aspect can include the method of the one hundred second aspect, where generating protons at the anode comprises: [00240] passing a water stream to the anode; and [00241] dissociating the water at the anode to form the protons and oxygen. [00242] A one hundred fourth aspect can include the method of the one hundred second or one hundred third aspect, where the cathode comprises the first catalyst in contact with a cathode gas diffusion layer, and wherein providing the gas stream to the cathode comprises passing the gas stream through the cathode gas diffusion layer to contact the first catalyst. [00243] A one hundred fifth aspect can include the method of any one of the one hundred second to one hundred fourth aspects, further comprising: applying between 1 V to 4 V across the anode and cathode during the converting. [00244] A one hundred sixth aspect can include the method of any one of the one hundred second to one hundred fifth aspects, further comprising: [00245] humidifying the gas stream prior to providing the gas stream to the cathode. [00246] A one hundred seventh aspect can include the method of any one of the one hundred second to one hundred sixth aspects, further comprising: cooling the reactor during the converting. [00247] A one hundred eighth aspect can include the method of any one of the one hundred second to one hundred seventh aspects, wherein the hydrocarbon comprises ethane, and wherein the product comprises acetic acid. [00248] In a one hundred ninth aspect, a method of producing acetic acid comprises: providing a gas stream comprising a hydrocarbon to a cathode in a reactor, wherein the reactor comprises the cathode and an anode, where the cathode and the anode are separated by an ion exchange membrane; producing acetic acid in the cathode to generate a product stream, wherein the product stream comprises the acetic acid; condensing at least a portion of the product stream to form a liquid stream and a gas stream; contacting the liquid stream with an extractant in an extraction column; solvating at least a portion of the acetic acid in the liquid stream in the extractant to produce a rich extractant and a lean liquid stream; separating the rich extractant to produce an acetic acid product stream and a first extractant stream; distilling a first portion of the lean liquid stream to produce a water stream and a second extractant stream; and combining the first extractant stream with the second extractant stream. [00249] A one hundred tenth aspect can include the method of the one hundred ninth aspect, wherein the product stream further comprises formic acid, and where the method further comprises: [00250] distilling the acetic acid product stream to produce an acetic acid stream and a formic acid stream, where the formic acid stream comprises primarily formic acid and a minor amount of acetic acid. [00251] A one hundred eleventh aspect can include the method of the one hundred ninth or one hundred tenth aspect, further comprising: feeding water to the anode; electrolyzing the water to produce protons and oxygen; passing the protons through the ion exchange membrane to the cathode; and passing the oxygen and water out of the anode. [00252] A one hundred twelfth aspect can include the method of the one hundred eleventh aspect, further comprising: separating the water from the oxygen; and combining at least a portion of the oxygen with the gas stream provided to the cathode. [00253] A one hundred thirteenth aspect can include the method of the one hundred twelfth aspect, further comprising: recycling at least a portion of the water separated from the oxygen to the anode. [00254] A one hundred fourteenth aspect can include the method of any one of the one hundred ninth to one hundred thirteenth aspects, further comprising: recycling at least a portion of the water stream to the anode. [00255] A one hundred fifteenth aspect can include the method of any one of the one hundred ninth to one hundred fourteenth aspects, further comprising: humidifying the gas stream prior to providing the gas stream to the cathode using at least one of a portion of the water separated from the oxygen or a portion of the water stream. [00256] A one hundred sixteenth aspect can include the method of any one of the one hundred ninth to one hundred fifteenth aspects, further comprising: passing the gas stream to an absorber; contacting the gas stream with a liquid in the absorber; absorbing at least a portion of any acetic acid in the gas stream in the liquid; passing the gas stream out of the absorber; and passing the liquid stream to the extraction column. [00257] While various embodiments in accordance with the principles disclosed herein have been shown and described above, modifications thereof may be made by one skilled in the art without departing from the spirit and the teachings of the disclosure. The embodiments described herein are representative only and are not intended to be limiting. Many variations, combinations, and modifications are possible and are within the scope of the disclosure. Alternative embodiments that result from combining, integrating, and/or omitting features of the embodiment(s) are also within the scope of the disclosure. For example, features described as method steps may have corresponding elements in the system embodiments described above, and vice versa. Accordingly, the scope of protection is not limited by the description set out above, but is defined by the claims which follow, that scope including all equivalents of the subject matter of the claims. Each and every claim is incorporated as further disclosure into the specification and the claims are embodiment(s) of the present invention(s). Furthermore, any advantages and features described above may relate to specific embodiments, but shall not limit the application of such issued claims to processes and structures accomplishing any or all of the above advantages or having any or all of the above features. [00258] Additionally, the section headings used herein are provided for consistency with the suggestions under 37 C.F.R. 1.77 or to otherwise provide organizational cues. These headings shall not limit or characterize the invention(s) set out in any claims that may issue from this disclosure. Specifically and by way of example, although the headings might refer to a “Field,” the claims should not be limited by the language chosen under this heading to describe the so-called field. Further, a description of a technology in the “Background” is not to be construed as an admission that certain technology is prior art to any invention(s) in this disclosure. Neither is the “Summary” to be considered as a limiting characterization of the invention(s) set forth in issued claims. Furthermore, any reference in this disclosure to “invention” in the singular should not be used to argue that there is only a single point of novelty in this disclosure. Multiple inventions may be set forth according to the limitations of the multiple claims issuing from this disclosure, and such claims accordingly define the invention(s), and their equivalents, that are protected thereby. In all instances, the scope of the claims shall be considered on their own merits in light of this disclosure, but should not be constrained by the headings set forth herein. [00259] Use of broader terms such as comprises, includes, and having should be understood to provide support for narrower terms such as consisting of, consisting essentially of, and comprised substantially of. Use of the term “optionally,” “may,” “might,” “possibly,” and the like with respect to any element of an embodiment means that the element is not required, or alternatively, the element is required, both alternatives being within the scope of the embodiment(s). Also, references to examples are merely provided for illustrative purposes, and are not intended to be exclusive. [00260] While preferred embodiments have been shown and described, modifications thereof can be made by one skilled in the art without departing from the scope or teachings herein. The embodiments described herein are exemplary only and are not limiting. Many variations and modifications of the systems, apparatus, and processes described herein are possible and are within the scope of the disclosure. For example, the relative dimensions of various parts, the materials from which the various parts are made, and other parameters can be varied. Accordingly, the scope of protection is not limited to the embodiments described herein, but is only limited by the claims that follow, the scope of which shall include all equivalents of the subject matter of the claims. Unless expressly stated otherwise, the steps in a method claim may be performed in any order. The recitation of identifiers such as (a), (b), (c) or (1), (2), (3) before steps in a method claim are not intended to and do not specify a particular order to the steps, but rather are used to simplify subsequent reference to such steps. [00261] Also, techniques, systems, subsystems, and methods described and illustrated in the various embodiments as discrete or separate may be combined or integrated with other systems, modules, techniques, or methods without departing from the scope of the present disclosure. Other items shown or discussed as directly coupled or communicating with each other may be indirectly coupled or communicating through some interface, device, or intermediate component, whether electrically, mechanically, or otherwise. Other examples of changes, substitutions, and alterations are ascertainable by one skilled in the art and could be made without departing from the spirit and scope disclosed herein.