FIELD OF THE INVENTION

Embodiments of the invention generally relate to a method and a system for upgrad ing methane rich gas to methanol.

BACKGROUND

The classical approach to methanol production involves steam reforming of hydrocar- bons and a major associated C02 emission. As the highly endothermic steam reform ing reaction is facilitated in fired reformers using large furnaces operating at tempera tures in the vicinity of 1000°C, the process economy is heavily favored by economy of scale to enable high process efficiency and integrated waste heat management. Such plants are therefore difficult to scale down economically due to the integrated design and high upfront capital investment. Consequently, the typical methanol plants exceed production capacities of 2000 MT/day.

It is an object of the invention to provide a method and system for converting methane rich gas to methanol. It is a further object of the invention to provide a sustainable method and system for converting methane rich gas to methanol.

SUMMARY OF THE INVENTION

The invention relates to sustainable production of methanol from a hydrocarbon feed gas by applying the electrically heated steam methane reformer (eSMR) technology that will allow for a practical zero-emission chemical plant with complete or substan tially complete carbon utilization.

Embodiments of the invention generally relate to a method and system for upgrading a hydrocarbon feed gas to methanol. This hydrocarbon feed gas could be natural gas, town gas, shale gas or biogas. In the following biogas will be used as example, which has a natural content of CO2. The term "biogas" in connection with the present invention means a gas with the fol lowing composition:

Compound Formula %

Methane CH4 50-75

Carbon dioxide C02 25-50

Nitrogen N2 0-10

Hydrogen H2 0-1

Oxygen 02 0-1

A first aspect of the invention relates to a method for upgrading hydrocarbon feed gas to methanol, comprising the steps of:

a) providing a hydrocarbon feed gas,

bl) optionally, providing CO2 to the process

b2) optionally, purifying the hydrocarbon feed gas in a gas purification unit, bB) optionally, prereforming the hydrocarbon feed gas together with a steam feed- stock in a prereforming unit,

c) carrying out steam methane reforming in a reforming reactor with a comprising a pressure shell housing a structured catalyst arranged to catalyze steam reforming of said hydrocarbon feed gas, said structured catalyst comprising a macroscopic structure of an electrically conductive material, said macroscopic structure supporting a ceramic coating, where said ceramic coating supports a catalytically active material; said steam methane reforming comprising the following steps:

cl) supplying said hydrocarbon feed gas to the reforming reactor,

c2) allowing the hydrocarbon feed gas to undergo steam reforming reaction over the structured catalyst and outletting a synthesis gas from the reforming reactor, and c3) supplying electrical power via electrical conductors connecting an electrical power supply placed outside said pressure shell to said structured catalyst, al lowing an electrical current to run through said macroscopic structure material, thereby heating at least part of the structured catalyst to a temperature of at least 500°C,

d) providing at least part of the synthesis gas of step c2) to a methanol synthesis unit to provide a product comprising methanol and an off-gas.

The step bl) of providing CO2 to the process is also understood to cover the cases where CO2 is present in the hydrocarbon feed gas. Moreover, step d) of providing at least part of the synthesis gas to the methanol synthesis unit also covers the case, where water is removed from the synthesis gas prior to leading the synthesis gas, in this case a dry or drier synthesis gas, to the methanol synthesis unit. The synthesis gas obtained in step c) may e.g. be cooled to a temperature below the dew point of the gas and be separated to a liquid phase comprising water and a gas phase comprising the dry synthesis gas, upstream the methanol synthesis unit.

The traditional methanol production involves steam reforming of hydrocarbons fol lowed by a methanol synthesis unit; this provides for a major associated CO2 emission.

Moreover, this traditional methanol production gives little opportunity for energy stor age and no debottlenecking of the energy fluctuations associated with renewable elec tricity. As the highly endothermic steam reforming reaction is facilitated in fired re formers using large furnaces operating at temperatures in the vicinity of 1000°C, the process economy is heavily favored by economy of scale to enable high process effi ciency and integrated waste heat management. Such plants are therefore difficult to scale down economically due to the integrated design and high upfront capital invest ment. Consequently, the typical methanol plants exceed production capacities of 2000 MT/day. An alternative route to methanol production is electrolysis of water for hydrogen pro duction mixed with CO2 for methanol production. This concept is proven and large- scale operation has already been performed with a capacity of 11 MT/day in Iceland, using alkaline electrolysis for hydrogen production. However, such plants are limited to locations with high availability of electricity, low electricity prices, and/or readily avail able high-grade CO2. Especially CO2 is a sparse resource and is typically financially unat tractive to utilize. Overall, the process economy of the electrolysis-driven frontend to a methanol plant remains very expensive compared with the classical steam reforming approach, because C0 ₂ -separation/purification combined with water electrolysis and subsequent compression has a very high net energy use, overall giving methanol pro duction prices 4-6 higher than equivalent fossil fuels. The use of only CO2 and hydro gen as make-up gas to the methanol synthesis also requires more catalyst inventory and reactor size, etc. due to the low reactivity of the gas. The application of co-elec- trolysis by solid oxide electrolysis cells (SOEC) could produce a more efficient and smaller methanol synthesis, but this approach is currently only at laboratory scale. In addition, electrolysis in general also has a high upfront capital investment presently, which only makes the process economy more challenged.

By the term "methanol synthesis unit" is understood one or several reactors config- ured to convert a synthesis gas into methanol. Such reactors can for example be a boil ing water reactor, an adiabatic reactor, a condensing methanol reactor or a gas-cooled reactor. Moreover, these reactors could be many parallel reactor shells and sequential reactor shells with intermediate heat exchange and/or product condensation. It is un derstood that the methanol synthesis unit also contains equipment for recycling and pressurizing feed to the methanol reactor(s). The term "hydrocarbon feed gas" is meant to cover both the hydrocarbon feed gas as well as a purified hydrocarbon feed gas, a prereformed hydrocarbon feed gas and a hydrocarbon feed gas with added steam and/or with added hydrogen and/or with added off-gas from the methanol syn thesis unit. All constituents of the hydrocarbon feed gas are pressurized, either sepa- rately or jointly, upstream the reforming reactor. Typically, steam is pressurized sepa rately; whilst the other constituents of the hydrocarbon feed gas may be pressurized jointly. The pressure(s) of the constituents of the hydrocarbon feed gas is/are chosen so that the pressure within the reforming reactor lies between 5 to 100 bar, preferably between 20 and 40 bar, or preferably between 70 and 90 bar.

In an embodiment, the electrical power supplied has been generated at least partly by means of renewable energy sources. Full utilization of methanol as an energy vector cannot be realized unless a more optimal production route is introduced. For this pur- pose, the method and plant of the invention uses renewable electricity to increase the energy value of hydrocarbon feed gas (such as methane) into methanol. The electri cally heated steam methane reformer (eSMR) is a very compact steam reforming reac tor, resulting in a lower capital investment than classical steam reforming equipment. The hydrocarbons in the hydrocarbon feed gas are preferably mainly methane; how- ever, the hydrocarbon feed gas may also comprise small amounts of higher hydrocar bons. The hydrocarbon feed gas can come from any methane-containing source such as biogas or natural gas, but because heating is facilitated by electricity, it will be an improvement over the existing fired reformer by saving the direct CO2 emissions. In addition, an excellent synergy exists with a biogas feedstock that will allow for practi- cally full conversion of all carbon in the biogas to methanol.

In an embodiment, wherein an electrolysis unit is used to generate a hydrogen rich stream from a water feedstock and where the hydrogen rich stream is added to the synthesis gas to balance the module M of the synthesis gas to be in the range of 1.5 to 2.5. Preferably, the module M of the synthesis gas is balanced to be in the range of

1.95 to 2.1. The module M of a synthesis gas is M = ^{Hz C} ° ² .

In an embodiment, the electrolysis unit is a solid oxide electrolysis cell unit and the wa ter feedstock is in the form of steam produced from other processes of the method. Steam is e.g. generated in the methanol synthesis unit or waste heat boiler of the sys tem for upgrading hydrocarbon feed gas to methanol.

In an embodiment, a membrane unit is included in the methanol synthesis unit to ex- tract at least part of the carbon containing molecules, such as CO and CO2, from the off-gas and return the at least part of the carbon containing molecules of the off-gas to the synthesis gas to balance the module M of the synthesis gas to be in the range of 1.5 to 2.5. Preferably, the module M of the synthesis gas is balanced to be in the range of 1.95 to 2.1. Again, the module M is defined as: M = ^{Hz C} ° ² .

⁰ co+co ₂

In an embodiment, a combination of steam superheating and steam generation is inte grated in the waste heat recovery of the hot synthesis gas product from the reforming reactor, and the superheated steam is used as steam feedstock in step c) of the method for upgrading a hydrocarbon feed gas to methanol.

In an embodiment, the pressure of the gas inside the reforming reactor is between 20 and 100 bar, preferably between 50 and 90 bar.

In an embodiment, the temperature of the gas exiting the reforming reactor is be- tween 900 and 1150°C.

In an embodiment, the space velocity evaluated as flow of gas relative to the geomet ric surface area of the structured catalyst is between 0.6 and 60 Nm ³ /m ² /h and/or the flow of gas relative to the occupied volume of the structured catalyst is between 700 Nm ³ /m ³ /h and 70000 Nm ³ /m ³ /h. Preferably, the flow of gas relative to the occupied volume of the structured catalyst is between 7000 Nm ³ /m ³ /h and 10000 Nm ³ /m ³ /h.

In an embodiment, the plot area of the reforming reactor is between 0.4 m ² and 4 m ² . Preferably, the plot area is between 0.5 and 1 m ² . Here the term "plot area" is meant to be equivalent to "ground area", viz. the area of land that the reforming reactor will take up when installed.

In an embodiment, the production of methanol is regulated according to availability of renewable energy.

In an embodiment, the method further comprises the step of upgrading the raw meth anol to fuel grade methanol. In an embodiment, the methanol is upgraded to chemical grade methanol.

In an embodiment, the method further comprises the step of using at least part of the methanol of step d) to a system for producing transportation fuel. In particular, the methanol is used as feedstock in a system for methanol to gasoline synthesis.

In an embodiment, between 80% and 100% of the carbon in the hydrocarbon feed gas is converted into methanol. This means than between 80% and 100% of the carbon at oms in the hydrocarbon feed gas are converted into carbon bounded in methanol mol ecules during the method of the invention.

In an embodiment, the hydrocarbon feed gas amounts to 500 Nm ³ /h to 8000 Nm ³ /h.

In an embodiment of the invention, the hydrocarbon feed gas is biogas. In a particular embodiment, wherein the hydrocarbon feed gas is biogas, a part of the off-gas pro- duced in step d) is recycled to a biogas production facility for producing the biogas to be upgraded in the method of the invention. As said off-gas typically has a high con tent of hydrogen, this hydrogen can be used in a biogas production facility, i.e. a fer mentation plant, where it can react with carbon oxides to produce methane. Effec tively, this means that in a process constellation where an amount of hydrogen rich off-gas is recycled to the biogas production facility, the produced biogas will have higher CH ₄ /CO ₂ ratio than a biogas produced in a biogas production facility with no re cycling of said hydrogen-rich off-gas.

Another aspect of the invention, relates to a system for upgrading a hydrocarbon feed gas to methanol, comprising:

- an optional gas purification unit,

- an optional prereforming unit,

- a reforming reactor with a comprising a pressure shell housing a structured catalyst arranged to catalyse steam reforming of said hydrocarbon feed gas , said structured catalyst comprising a macroscopic structure of an electrically conductive material, said macroscopic structure supporting a ceramic coating, where said ceramic coating sup ports a catalytically active material; wherein the reforming reactor moreover com prises an electrical power supply placed outside said pressure shell and electrical con ductors connecting said electrical power supply to said structured catalyst, allowing an electrical current to run through said macroscopic structure material to thereby heat at least part of the structured catalyst to a temperature of at least 500°C,

- a methanol synthesis unit arranged to receive a synthesis gas from said reforming re actor and produce a product comprising methanol and an off-gas. The structured catalyst of the reforming reactor of the system is configured for steam reforming. This reaction takes place according to the following reactions:

CH4 + H2O CO + BH2

CH4 + 2H2O CO2 + 4H2

CH4 + CO2 2CO + 2H2

The structured catalyst is composed a metallic structure, a ceramic phase, and an ac tive phase. The metallic structure may be FeCrAlloy, Alnico, or similar alloys. The ce ramic phase may be AI ₂ O ₃ , MgA^Os, CaA^Os, ZrC>2, or a combination thereof. The cata lytically active material may be Ni, Ru, Rh, Ir, or a combination thereof.

In an embodiment, catalyst pellets are loaded on top of, around, inside, or below the structured catalyst of the reforming reactor. The catalyst material for the reaction may be Ni/Al2C>3, Ni/MgAhOs, Ni/CaA^Os, Ru/MgAhC^, or Rh/MgAhOs. The cata lytica lly ac tive material may be Ni, Ru, Rh, Ir, or a combination thereof. This can improve the overall gas conversion inside the reforming reactor.

In an embodiment, the macroscopic structure(s) has/have a plurality of parallel chan nels, a plurality of non-parallel channels and/or a plurality of labyrinthic channels. The channels have walls defining the channels. Several different forms and shapes of the macroscopic structure can be used as long as the surface area of the structured cata- lyst exposed to the gas is as large as possible. In a preferred embodiment, the macro scopic structure has parallel channels, since such parallel channels render a structured catalyst with a very small pressure drop. In a preferred embodiment, parallel longitudi nal channels are skewed in the longitudinal direction of the macroscopic structure. In this way, molecules of the gas flowing through the macroscopic structure will mostly tend to hit a wall inside the channels instead of just flowing straight through a channel without necessarily getting into contact with a wall. The dimension of the channels should be appropriate in order to provide a macroscopic structure with a sufficient re sistivity. For example, the channels could be quadratic (as seen in cross section perpen dicular to the channels) and have a side length of the squares of between 1 and 3 mm; however, channels having a maximum extent in the cross section of up to about 4 cm are conceivable. Moreover, the thickness of the walls should be small enough to pro vide a relatively large electrical resistance and large enough to provide sufficient me chanical strength. The walls may e.g. have a thickness of between 0.2 and 2 mm, such as about 0.5 mm, and the ceramic coating supported by the walls has a thickness of between 10 pm and 500 pm, such as between 50 pm and 200 pm, such as 100 pm. In another embodiment, the macroscopic structure of the structured catalyst is cross-cor rugated. In general, when the macroscopic structure has parallel channels, the pres sure drop from the inlet to the outlet of the reforming reactor system may be reduced considerably compared to a reactor where the catalyst material is in the form of pel lets such as a standard SMR. In an embodiment, the macroscopic structure(s) is/are extruded and sintered struc tures. Alternatively, the macroscopic structure(s) is/are 3D printed structure(s). A 3D printed structure can be provided with or without subsequent sintering. Extruding or 3D printing a macroscopic structure, and optional subsequent sintering thereof results in a uniformly and coherently shaped macroscopic structure, which can afterwards be coated with the ceramic coating.

Preferably, the macroscopic structure has been manufactured by 3D printing or extru- sion of a mixture of powdered metallic particles and a binder to an extruded structure and subsequent sintering of the extruded structure, thereby providing a material with a high geometric surface area per volume. Preferably, the 3D printed extruded struc ture is sintered in a reducing atmosphere to provide the macroscopic structure. Alter natively, the macroscopic structure is 3D printed a metal additive manufacturing melt- ing process, viz. a 3D printing processes, which do not require subsequent sintering, such as powder bed fusion or direct energy deposition processes. Examples of such powder bed fusion or direct energy deposition processes are laser beam, electron beam or plasma 3D printing processes. As another alternative, the macroscopic struc ture may have been manufactured as a 3D metal structure by means of a binder-based metal additive manufacturing process, and subsequent sintered in a non-oxidizing at mosphere at a first temperature Ti, where Ti > lOOCfC, in order to provide the macro scopic structure.

A ceramic coating, which may contain the catalytically active material, is provided onto the macroscopic structure before a second sintering in an oxidizing atmosphere, in or der to form chemical bonds between the ceramic coating and the macroscopic struc ture. Alternatively, the catalytically active material may be impregnated onto the ce ramic coating after the second sintering. When chemical bonds are formed between the ceramic coating and the macroscopic structure, an especially high heat conductiv ity between the electrically heated macroscopic structure and the catalytically active material supported by the ceramic coating is possible, offering close and nearly direct contact between the heat source and the catalytically active material of the structured catalyst. Due to close proximity between the heat source and the catalytically active material, the heat transfer is effective, so that the structured catalyst can be very effi- ciently heated. A compact reforming reactor system in terms of gas processing per re forming reactor system volume is thus possible, and therefore the reforming reactor system housing the structured catalyst may be compact. The reforming reactor system of the invention does not need a furnace and this reduces the overall reactor size con siderably. Moreover, it is an advantage that the amount of synthesis gas produced in a single pressure shell is increased considerably compared to known tubular steam re formers. In a standard tubular steam reformer, the amount of synthesis gas produced in a single tube of the tubular steam reformer is up to 500 Nm ³ /h. In comparison, the reforming reactor of the invention is arranged to produce up to or more than 2000 Nm ³ /h, e.g. even up to or more than 10000 Nm ³ /h, within a single pressure shell. This can be done without the presence of O2 in the feed gas and with less than 10% me thane in the synthesis gas produced. When a single pressure shell houses catalyst for producing up to 10000 Nm ³ /h synthesis gas, it is no longer necessary to provide a plu rality of pressure shells or means for distributing feed gas to a plurality of such sepa rate pressure shells.

As used herein, the terms "3D print" and "3D printing" is meant to denote a metal ad ditive manufacturing process. Such metal additive manufacturing processes cover 3D printing processes in which material is joined to a structure under computer control to create a three-dimensional object, where the structure is to be solidified, e.g. by sin- tering, to provide the macroscopic structure. Moreover, such metal additive manufac turing processes cover 3D printing processes, which do not require subsequent sinter ing, such as powder bed fusion or direct energy deposition processes. Examples of such powder bed fusion or direct energy deposition processes are laser beam, electron beam or plasma 3D printing processes. Preferably, the catalytically active material is particles having a size from 5 nm to 250 nm. The ceramic coating may for example be an oxide comprising Al, Zr, Mg, Ce and/or Ca. Exemplary coatings are calcium aluminate or a magnesium aluminum spinel. Such a ceramic coating may comprise further elements, such as La, Y, Ti, K or combinations thereof. Preferably, the conductors are made of different materials than the macro scopic structure. The conductors may for example be of iron, nickel, aluminum, cop per, silver or an alloy thereof. The ceramic coating is an electrically insulating material and will typically have a thickness in the range of around 100 pm, e.g. about 10-500 pm.

The macroscopic structure is advantageously a coherent or consistently intra-con- nected material in order to achieve electrical conductivity throughout the macroscopic structure, and thereby achieve thermal conductivity throughout the structured catalyst and in particular providing heating of the a catalytically active material supported by the macroscopic structure. By using the coherent or consistently intra-connected ma terial, it is possible to ensure uniform distribution of current within the macroscopic structure and thus uniform distribution of heat within the structured catalyst.

Throughout this text, the term "coherent" is meant to be synonymous to cohesive and thus refer to a material that is consistently intra-connected or consistently coupled. The effect of the structured catalyst being a coherent or consistently intra-connected material is that a control over the connectivity within the material of the structured catalyst and thus the conductivity of the macroscopic structure is obtained. It is to be noted that even if further modifications of the macroscopic structure are carried out, such as provision of slits within parts of the macroscopic structure or the implementa- tion of insulating material within the macroscopic structure, the macroscopic structure is still denoted a coherent or consistently intra-connected material.

In an embodiment, the structured catalyst has electrically insulating parts arranged to increase the current path between the conductors to a length larger than the largest dimension of the structured catalyst. The provision of a current path between the con ductors larger than the largest dimension of the structured catalyst may be by provi sion of electrically insulating parts positioned between the conductors and preventing the current running through some part of the structured catalyst. Such electrically in- sulating parts are arranged to increase the current path and thus increase the re sistance through the structured catalyst. In an embodiment, the at least one electri cally insulating part has a length arranged to ensure that the minimum current path between the conductors is larger than the largest dimension of the macroscopic struc ture.

Non-limiting examples of such insulating parts are cuts, slits, or holes in the structure. Optionally, a solid insulating material such as ceramics in cuts or slits in the structure can be used. In a case where the solid insulating material is a porous ceramic material, the catalytically active material may advantageously be incorporated in the pores, by e.g. impregnation. A solid insulating material within a cut or slit assists in keeping the parts of the structured catalyst on the sides of the cut or slit from each other. As used herein, the term "largest dimension of the structured catalyst" is meant to denote the largest inner dimension of the geometrical form taken up by the structured catalyst. If the structured catalyst is box-formed, the largest dimension would be the diagonal from one corner to the farthest corner, also denoted the space diagonal.

It should be noted that even though the current through the structured catalyst may be arranged to twist or wind its way through the structured catalyst due to the electri cally insulating parts arranged to increase the current path, the gas passing through the reforming reactor system is inlet at one end of the reforming reactor system, passes through the structured catalyst once before being outlet from the reforming re actor system. Inert material is advantageously present in relevant gaps between the structured catalyst and the rest of the reforming reactor system to ensure that the gas within the reforming reactor system passes through the structured catalyst and the catalytically active material supported thereby. In an embodiment, the length of the gas passage through the structured catalyst is less than the length of the passage of current from one conductor through the structured catalyst and to the next conductor. The ratio of the length of the gas passage to the length of the current passage may be less than 0.6, or 0.3, 0.1, or even down to 0.002.

In an embodiment, the structured catalyst has electrically insulating parts arranged to make the current path through the structured catalyst a zigzag path. Here, the terms "zigzag path" and "zigzag route" is meant to denote a path that has corners at variable angles tracing a path from one conductor to another. A zigzag path is for example a path going upwards, turning, and subsequently going downwards. A zigzag path may have many turns, going upwards and subsequently downwards many times through the structured catalyst, even though one turn is enough to make the path a zigzag path. The following is a detailed description of embodiments of the invention depicted in the accompanying drawings. The embodiments are examples and are in such detail as to clearly communicate the invention. However, the amount of detail offered is not in tended to limit the anticipated variations of embodiments; but on the contrary, the in tention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the present invention as defined by the appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS

Figure 1 is a schematic drawing of a system for upgrading a hydrocarbon feed gas to methanol;

Figures 2a-2c show comparative cases for methanol plants based on a fired reformer versus an electric reformer versus alkaline electrolysis;

Figure 3 shows CO2 equivalent emissions (C0 ₂ e) associated with production of MeOH as the combined contribution from: Plant emissions + Emissions from electricity gener ation; and Figure 4 is a graph of technologies with lowest operating expenses as a function of nat ural gas price and electricity price.

DETAILED DESCRIPTION OF THE DRAWINGS

Figure 1 is a schematic drawing of a system 100 for upgrading of hydrocarbon feed gas to methanol. The system is a methanol plant comprising an electrically heated steam methane reformer (eSMR) 50.

The system 100 for upgrading a hydrocarbon feed gas to methanol comprises a re- forming section 10 and a methanol section 60. The reforming section 10 comprises a preheating section 20, a purification unit SO, e.g. a desulfurization unit, a prereformer 40 and an eSMR 50. The methanol section comprises a first separator 85, a compressor unit 70, a methanol synthesis unit 80, a second separator 90 as well as heat exchang ers. The first and second separators 65 and 90 may e.g. be flash separators.

A hydrocarbon feed gas 1 is preheated in the preheating section 20 and becomes a preheated hydrocarbon feed gas 2, which is led to the purification unit 30. A purified preheated hydrocarbon feed gas 3 is sent from the purification unit 30 to the preheat ing section 20 for further heating. Moreover, steam 4 is added to the purified pre- heated hydrocarbon feed gas, resulting in feed gas 5 sent to a prereformer 40. Prere formed gas 6 exits the prereformer 40 and is heated in the preheating section 20, re sulting in gas 7. In the embodiment of figure 1, hydrogen 14 is added to the gas 7, re sulting in a feed gas 8 sent to the eSMR 50. The feed gas 8 undergoes steam methane reforming in the eSMR 50, resulting in a reformed gas 9 which is led from the eSMR 50 and from the reforming section 10 to the methanol section 60.

In the methanol section 60, the reformed gas 9 heats water 12 to steam 13 in a heat exchanger. In a first separator 85 water is separated from the synthesis gas 9 to pro vide a dry synthesis gas 11, which is sent to a compressor 70 arranged to compress the dry synthesis gas before it is mixed with recycle gas from a second separator 90 enters the methanol synthesis unit 80. Most of the produced methanol from the methanol synthesis unit 80 is condensed and separated in the second separator 90 and exits the methanol section as methanol 25. The gaseous component from the second separator 90 is split into a first part that is recycled to the methanol synthesis unit 80 and a sec- ond part that is recycled as an offgas 17 to be used as fuel 18 to the preheating section 20 of the reforming section 10 and/or recycled as feed 16 to the eSMR 50. An addi tional compressor is typically used for recycling the first part of the gaseous compo nent from the second separator 95 to the methanol synthesis unit 80. Water 12 is heated to steam within heat exchangers of the system 100 and in the given embodi- ment inside the cooling side of the methanol synthesis unit 80.

In the case, where a second hydrocarbon feed gas is added to or mixed with the hydro carbon feed gas upstream the reforming reactor, the second hydrocarbon feed gas is typically added to the hydrocarbon feed gas upstream the prereforming unit and the purification unit. In figure 1, this would correspond to adding the second hydrocarbon feed gas to the preheated hydrocarbon feed gas 2. The second hydrocarbon feed gas may be a stream of natural gas having a higher H/C ratio than the H/C ratio of the hy drocarbon feed gas of stream 1. Such a system 100 according to the invention, comprising an electrically heated steam methane reformer and a methanol synthesis unit is also abbreviated eSMR-MeOH. Such an eSMR-MeOH system resembles a plant used in classical industrial process (SMR-MeOH) to a large extent, but deviates on some essential aspects. The use of the eSMR 50 removes the requirement for the intensive firing in the fired steam reformer of a classical SMR-MeOH system and thereby leaves only a small CO2 emission from the eSMR-MeOH layout associated with purge gas handling. Moreover, in the case where the hydrocarbon feed gas is biogas, the use of biogas rather than natural gas as feedstock removes the requirement for oxygen addition to the synthesis gas as the natural high CO2 content of biogas allows for the module adjustment inherently, as de scribed below. From an overall plant stoichiometry where methane (as natural gas) is used as feed stock, the reaction scheme can be expressed as:

CH ₄ + 0.50 ₂ ® CO + 2H ₂ ® CH ₃ OH

Alternatively, if a CO ₂ feedstock is available, this can be used as oxygen source, giving an overall plant stoichiometry of:

0.75CH ₄ + 0.25CO ₂ + O.5H ₂ O ® CO + 2H ₂ ® CH ₃ OH. Higher temperatures can be reached in an eSMR compared with a fired reformer, which gives a better conversion of methane in this layout; in the end, this provides for less off-gas handling. It should be noted, that the CO ₂ content in process gas can vary, and therefore, an addition CO ₂ and/or CO, e.g. from the off-gas, to the synthesis gas can be advantageous.

The same methanol synthesis technology as in the classical approach can be used and the methanol reactor will in this layout have a CO/CO ₂ ratio corresponding to that of a typical methanol plant and therefore have a similar activity and stability. To some extent, at least part of the off-gas from the methanol synthesis unit can be re cycled to the reforming section as feedstock to increase the carbon efficiency and re cover unconverted methane. In the same way, it is also possible to recover the off-gas from a potential methanol distillation and return this as feedstock, if this is com pressed to operating pressure. At least to some extent, preheating can be done by the excess steam, because high preheating. Electrically heated reforming can e.g. use a monolithic-type catalyst heated directly by Joule heating to supply the heat for the re action. In its essence, the eSMR 50 is envisioned as a pressure shell having a centrally placed catalytic monolith, which is connected to an externally placed power supply by a conductor threaded through a dielectric fitting in the shell. The shell of the eSMR is refractory lined to confine the high-temperature zone to the center of the eSMR. From a reforming reactor point of view, the eSMR has several advantages over a con ventional fired reformer. One of the most apparent is the ability to make a significantly more compact reactor design when using electrically heated technology, as the re- forming reactor no longer is confined to a system of high external heat transfer area. A size reduction of two orders of magnitudes is conceivable. This translates into a signifi cantly lower capital investment of this technology. The combined preheating and re forming section of an eSMR (including power supply) configuration was estimated to have a significant lower capital investment. As the synthesis gas preparation section of a methanol plant accounts for more than 60% of the capital investment in a classical fired reformer based methanol plant, a drastic saving on the reformer equipment will translate into a significant reduction in the cost of a methanol plant based on eSMR.

Figure 2a-2c show comparative cases for methanol plants based on a fired reformer versus (figure 2a) an electric reformer (figure 2b) versus alkaline electrolysis (figure 2c). A major advantage of the eSMR of figure 2b is that it does not require burning hydro carbons to provide the heat for the reaction, and consequently direct CO2 emissions of this technology is significantly decreased. This is exemplified in Figures 2a-2c, showing how the consumables and CO ₂ emissions can be markedly changed when using the eSMR-MeOH technology compared with both the fired reformer approach and elec trolysis. The consumption figures of the fired reformer layout (figure 2a) and the eSMR-MeOH layout (figure 2b) are both based on Haldor Topsoe developed flow sheets for chemical-grade methanol production (i.e., including product distillation), while electrolysis layout (figure 2c) is an overall best-case stoichiometric analysis cou- pled with published consumption figures for alkaline electrolysis (AEL) based H2 pro duction and CO ₂ purification. It should be noted, that the consumables are, from a chemical standpoint, divided in substantially pure CH ₄ and CO ₂ to not disadvantage the SMR-MeOH layout by requiring firing with hydrocarbon feed gas, which would have in creased the CO ₂ emissions from this plant considerably. In the given case, 30% reduc tion in methane consumption and 80% reduction in CO ₂ emissions are achieved by the eSMR-MeOH compared to the fired reformer (SMR-MeOH). It is emphasized that pro cess improvement may be considered for all presented cases, and should therefore not be considered limiting. When no units are given, the presented figures represent rela tive molar flow of components in figure 2a-2c.

The overview of the consumables of Figures 2a-2c illustrates a markedly lower electric ity use for methanol production when using eSMR-MeOH over electrolysis. By use of SOEC instead of AEL in the electrolysis layout, the electricity use could potentially de crease to 11-13 kWh/Nm ³ MeOH (depending on availability of steam), which would be an improvement for this technology, but still markedly higher than eSMR-MeOH. No tice that the concept development still can be done on the electrolysis approach to im prove the performance of this technology, but this is all at research stage and only es tablished electrolysis technology, as AEL, combined with classical methanol synthesis technology can be considered ready for industrial application presently, why this is also the focus of the comparison.

Energy consumption of methanol production by AEL ("AEL-MeOH") is calculated as: E _t o _t ai = E _AEL + E _CO2 + E _compress - E _steam . Here, E _AEL is energy use of alkaline elec trolysis with an energy efficiency of 71%. E _co is the energy use of CO2 purification es- timated as 2.6 MJ/Nm ³ CO2 when using flue gas as feedstock. E _compress is the com pression power calculated at an efficiency of 75%, without including energy for cooling water, to be 0.7 kWh/Nm ³ Methanol. E _steam is the potential energy recovery from steam production calculated as 75% recovery of the exothermic energy removed in the methanol synthesis estimated to be 0.7 kWh/Nm ³ Methanol. The calculation does not include any considerations on byproduct formation in the methanol synthesis unit or their integration in the plant layout.

Figure 3 shows CO2 equivalent emissions (CC^e) associated with production of metha nol for SMR, eSMR and AEM, respectively. For each of these production technologies, the black box represent overall equivalent emissions (CC^e) if the methanol was pro duced by renewable energy and the white box represent overall equivalent emissions (CChe) if the methanol was produced with electricity from the Danish electricity net work in 2019. When calculating the overall CO2 emissions from a chemical plant, the electricity consumption must be evaluated as well, as this could potentially also have a large CO2 emission footprint. The exact emissions will be dependent on the source of the electricity. Looking at the associated equivalent CO2 emissions (CC^e) when elec tricity is provided either by fully sustainable resources or as an example the Danish en ergy grid in 2019, in which more than 60% of the annual electricity use is covered by sustainable sources as solar cells, wind power, and biomass. The actual CC^e for pro duction of methanol by the eSMR-MeOH technology was on this basis calculated as shown in Figure 3 and benchmarked against the conventional fired technologies and AEL-MeOH. Irrespective of the source of electricity, eSMR-MeOH will markedly better the CO2 footprint of the methanol product over the conventional approach, viz. SMR- MeOH. While, based on the energy grid in Denmark in 2019, the electrolysis approach will not have a positive effect on the CC^e. Only when the electricity is fully renewable, the electrolysis approach will have an C0 ₂ e comparable to the eSMR-MeOH route, but AEL-MeOH will still be 35% higher Figure 4 is an overview of technologies with lowest operating expenses as a function of natural gas price and electricity price.

To make sustainable technology attractive, it must be cost-competitive compared to the established production routes. Figure 4 shows an overview of which technology gives the lowest operating expenses as a function of gas and electricity price. It should be noted, that the overview only shows operating expenses. If expenses to plant de preciation is included in the production costs, the size of the area indicated "eSMR- MeOH" would markedly increase into the areas denoted "AEL-MeOH" and "SMR- MeOH", because the eSMR-MeOH technology has a significantly lower capital invest ment compared with the two other technologies. From this overview it can be seen that the fired technology (SMR-MeOH) has been the cheapest production route for the last century because it is favoured by the low gas prices. However, the decreasing elec tricity prices opens for an incentive toward the electrically driven technologies. An eSMR driven frontend is proposed as a next step for a cost-competitive route for meth- anol production. To exemplify the opportunity, competitive cases can be found when comparing with natural gas prices of ca. 6-8 $/MMBTU in Europe. The operating ex penses of the eSMR-MeOH technology will be further favoured in cases with CO2 taxa tion, which will increase the operating expenses of the fired reformer approach signifi cantly. This is indicated by the dashed line in Figure 4, with a representative CO2 tax of the Nordic countries today. It is emphasized that Figure 4 is only indicative, as the de velopment within the eSMR-MeOH layout is still in a relatively early phase. It is fore seen that development within eSMR-MeOH will improve the consumption figures fur ther, and thereby the operating expenses. While the invention has been illustrated by a description of various embodiments and while these embodiments have been described in considerable detail, it is not the in tention of the applicant to restrict or in any way limit the scope of the appended claims to such detail. Additional advantages and modifications will readily appear to those skilled in the art. The invention in its broader aspects is therefore not limited to the specific details, representative methods, and illustrative examples shown and de scribed. Accordingly, departures may be made from such details without departing from the spirit or scope of applicant's general inventive concept.

EXAMPLE 1

Example 1 relates to an embodiment of the invention where a biogas is converted into methanol, cf. Fig. 1 for reference. A feed gas (1) is mixed with a CO2 feed to adjust the synthesis gas module and a recycle gas from a methanol loop to provide hydrogen for the subsequent desulfurization (30) and prereforming (40) steps. Using an electrically heated reformer (50), the gas is converted with steam (4) into a synthesis gas. This is cooled and separated into a condensate and dry synthesis gas (11), where the dry syn thesis gas is compressed and fed to a methanol loop using a boiling water type metha nol reactor (80). The compressed make-up synthesis gas is mixed with recycled gas (95) in the loop and sent to the methanol reactor (80) to produce methanol. By cooling and condensing this methanol is separated to produce the final product (25). Most of the off-gasses from this separation are recycled (95) directly to the methanol reactor, an other fraction (16) is recycled to the feed, while the last fraction is exported as a fuel rich off-gas.

Overall, this embodiment of the process allows for converting 95.4% of the carbon feedstock (CO ₂ + CH ₄ ) into methanol.