BACKGROUND OF THE INVENTION

Methanol manufacture from methane via methane to synthesis gas (CO + H ₂ ), and then synthesis gas to methanol is the current good, efficient, commercial way to make methanol. It becomes quite economic when performed on abig scale and using natural gas which is relatively free from inert non-hydrocarbon components. Conventional, small plants cannot compete well for capitol which becomes relatively high per unit of methanol produced. System pressure and need for compressors to raise pressure to 700-2500 psig is costly on a small scale. Today, methanol plants of over abϋlion pounds per year are desired. Whereas, 500 million pounds per year from waste methanol generation is about a maximum. Further, solid waste landfill assay gas will be about 50% carbon dioxide and 5% inerts (mainly nitrogen but with sulfur components, etc.). Carbon dioxide maybe conveniently removed by one of several techniques which may also remove sulfur impurities. However, residual N ₂ in methane is expensive to remove, generally via cryogenic distillation. Thus, a way to use methane without removing nitrogen or doing major compression in making methanol on the scale of solid waste landfills is desirable. As more and more gas has been discovered in places removed from convenient pipelining, its conversion to methanol-a liquid easily shipped by tanker-has become amajor choice use for this Mghmethane natural gas. Three factors impact this product

This gas product must be imported affecting balance of trade for importing country.

It comes to ports by tanker and requires trans-shipping to inland sites thus adding an additional cost

Natural gas is not a "regenerable" quantity.

Thus, the conversion of solid waste landfill methane to methanol has some advantage, but the problems of scale, inerts and compression exist

SUMMARY OF THE INVENTION

What is proposed herein is a technique to make methanol with less capitol per unit; methanol on a small scale while avoiding major compression and reacting methane away with simple cheap separations from nitrogen or other inerls.

The most advantageous method is to directly oxidize methane to methanol. The chemistry has long been recognized: CH ₄ + [O] -^ CH ₃ OH. But unfortunately, many hundreds of efforts to stop there have been unsatisfactory. Simply put, each step in the oxidation

_C H ₂ + [O3 ■» O _Ϊ2 OHi22_> CO ₂ . . _{+- +u}

^{2 1 2} iseasierthantiiestepbefore.No adequate stopping has been seen. Ih a multi-step rather expensive way, mercury complexes have worked. Economics for this have proved unattractive, but a second reaction preventing the oxidation pattern above functioned. This study ^J) has progressed to the system

⁰

CH ₄ + CF ₃ CO ₂ H + Pd ⁺² -» CH ₃ OCCH ₃ + Pd ⁰ These lnvesugators nave recognized tnat tne W acKer reaction:

C ₂ BU +H ₂ O ₊ Pcf ² ₊ Cu ⁺² + O ₂ •* CH ₃ CHO, _{provides awayto reoχidize the} p _d o madep _d +2 _{vja Cu} + ⁱ ₊ Q ₂ ^ _Cu + ² _{? 2} c _u ⁺² +Pd ⁰ ■» 2Cu ⁺¹ + Pd ⁺² - But although the high acidity of tri-fluoroacetic acid (CF ₃ CO ₂ H) allows esterification at rates (with ratios of components used) stopping oxidation toward formaldehyde, the ester must be very cheaply reconverted to methanol and recycle acid The trifluoroacetic acid is expensive however the methanol product being made is quite cheap. Very little of the trifluoroacetic acid loss can be afforded.

Clearly if a stopping agent is to be used for the methane reaction commercially, it needs to be cheap and its conversion to methanol and 1he stopping agent very easy and cheap.

Phthalic anhydride is the preferred stopping agent As a hot melt, phthalic anhydride reacts very readily and without catalyst to the half ester with methane.

Thus, the reaction,

Of course, we must add copper as in the Wacker reaction and air for copper oxidation:

CH ₄ +Pd ⁺² + Cu ⁺² + .5O ₂ +Pd ⁺² + CU ⁺²

So, the Pd ⁺² , Cu ⁺² becomes the catalyst and the reaction has only anhydride, methane and oxygen. The half ester is converted to phthalic anhydride and methanol by a temperature increase.

Phthalic anhydride is made by oxidizing naphthalene or o-xylene with vanadium catalyst at

~ 47O ⁰ C. Similar conditions oxidize benzene to maleic anhydride. A C-H bond in benzene and that of methane have similar bond strength. Ergo, phthalic anhydride is indeed more oxidation stable than methane.

Most useful is the fact that dicarboxylic acids upon distillation are converted to the cyclic anhydride if the number of carbon atoms plus one oxygen creates a 5 or 6 membered ring. Thus maleic acid is converted commercially to maleic anhydride in an azeotropic distillation with xylene (right boiling point):

Water is the leaving group. Methanol has been seen to serve equally well as the leaving group: Q

HC^ CO ₂ CH ₃ HC- ^\

H — > (I O ^■ + ^• CH ₃ OH

HC^CO ₂ H HC^-C-"

O

Likewise, phfealic acid and monomeuiyl phthalate will behave like maleic specie above.

Thus,

Now, the flow sheet may be understood,

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic of the preferred embodiment of the present process for deriving methanol from methane.

DETAILED DESCRIPTION OF THE DRAWINGS

In Fig. 1 there is shown an entrained reactor 1 with inert packing material. Methane gas is introduced to Hie reactor together with an anhydride of a dicarboxylic acid wherein the anhydride ring contains 4 or 5 carbon atoms. Preferably the diacid anhydride is phthalic anhydride. Air is also introducedinfo the reactor which is typically maintained at about 190 ⁰ C. Thereactionproduct, including the desired half ester methyl phthalate, is shown as leaving the reactor 1 via the bottom to a separator II wherein the unreacted methane and other gases are separated as top effluent and the liquid remainder leaving as abottoms product to a distillation column IE. The temperature of column HI is maintained above the decomposition temperature of the half ester methyl phthalate thereby releasing methanol as an overhead product. In the preferred embodiment, the unreacted methane from separator II is forwarded to a catalytic combustor IV wherein the methane is catalytically converted to methanol and returned to column HI via pipes and valves shown in Fig. 1. Also, the recovered phthalic anhydride from the bottom of column HI is returned to reactor I for reuse in the process. Also shown in Fig. 1 is piping through which a heat exchange media is conducted to the catalytic combustor IV thereby recovering heat from this unit for use in the other units of the process requiring added heat to maintain desired temperature.

DETAILED DESCRIPTION OF THE INVENTION

To gain the conversion level needed for this once through oxidation at modest pressure, an entrainment reactor is preferred. Thkentrainment carries bubbles ofgas down the reactor.

Linear velocity of melted (i.e. liquid) phthalic anhydride entrains both methane and air such that as this liquid phase reacts with dissolved oxygen and methane, these gases are replaced by dissolving bubbles. In order to work well, an inert packing is used in reactor to provide continuous mixing with a modest pressure drop. Re-dissolving entrained gases allows us to work at moderate pressure and yet supply as much reactant to catalyst as a considerably higher pressure in which all reactant is pre-dissolved. The effect is as if we utilized the much higher pressure, more capital intensive system. The process functions by switching our first reactor to one utilizing

oxidation to methanol and then very fast stabilization by the production of the half ester in excess, hot phthalic anhydride. The flow system with constant regeneration of Rf ² by Cu ⁺² reaction with Pd ⁰ provides a high ratio OfPd ⁺² to dissolved methane. Also, this reaction takes place at a fairly hot temperature. Thus methane oxidation is relatively fast and is not an equilibrium- regulatedreactionbypressure.

To decompose the monomethyl phthalate, simply raise the temperature above its decomposition point. By utilizing good heat exchange in the distillation column methanol is taken overhead while returning phthalic anhydride via column bottoms, including Pd ⁺² , Cu ⁺² phthalates to entrained oxidation. Total oxygen should always be less than enough for explosion, i.e. mixture remains hydrocarbon rich at all places. It may also be noted that this process causes nitrogen from the input gas stream to exit with unreacted methane and oxygen plus the nitrogen and small amounts of inerts from air inputs. Small levels of H ₂ S or low boiling sulfur compounds will exit as occurring or be oxidized with this stream in the catalytic oxidizer. Several versions of this unit are possibilities including commercial waste oxidizers. A likely choice would be a Pt or alumina catalyst operating at about 600-700°C. This unit would provide the heat for the reactive distillation column. Generally speaking, entrained oxidation reactors will leave more B.T.U. value than reheat needs. However, if optimum conversion does not leave enough B.T.U. in entrained oxidation reactor vent gas and at high enough temperature, one can intentionally increase methane to waste burner by air decrease to entrainment reactor or by decreasing contact time.

We have an unusual economic situation. Methane cost in gas will be M> to ¹ A or less than the offshore big volume natural gas to competitive conventional facilities for methanol. Thus, balance on capitol and raw material will be more focused on capital. It will not be advantageous to waste gas, yet, in balance, capital restraint will have a larger role. It is essential, however, that we eliminate hydrocarbons from the environment via the catalytic combustor.

Given this overall picture, we can see lack ofhigh pressure and simple capital systems allow a methanol reactor of relatively small size to be of good economics in the waste generated case.

Noble metals are intended to mean herein palladium, platinum, gold, silver, iridium, rhenium, mercury, ruthenium, and osmium. Preferred noble metals are palladium and platinum.

Although discussion has focused on methane generated within solid waste landfills after they are sealed as feed to modest methanol facilities, it should be recognized that bacterial

decomposition in sewage disposal plants can also generate sizable methane. These facilities may also be raw material source for methane generation with this process. Yet another source of bacterial generation of methane for this process maybe animal feces where large quantities of chicken or other fowl or livestock such as pigs or cattle are collectively raised for food supplies. Although assay of methane will vary with each source, generally apractical sized bacterial unit will regionally supply regenerable methane in quantities that are small compared to natural gas sources. Such small methane sources will basically fit the methanol system defined herein.

EXAMPLE l

Utilizing the principles described in the summary, a waste methane input stream previously depleted of CO ₂ and sulfur containing gases is oxidized in an entrainment reactor utilizing molten phthalic anhydride as the solvent/reactant. Air is the source of oxygen for the system with nitrogen, carbon dioxide, and its minor components present. The waste methane input stream is derived from solid waste landfill bacterial decomposition and, as stated, has had carbon dioxide, hydrogen sulfide, methyl and ethyl mercaptan removed along with traces of higher mercaptans. The stream contains an average assay of 5% nitrogen. Oxidation takes place in the presence of 2% palladium and 2% copper phthalate in the phthalic anhydride solution.

Flow rates involve about 85% molten phthalic solution and the remainder entrained and dissolved air and methane. Air quantity is such that methane to oxygen ratio is maintained at 0.3 mol oxygen/mol methane. Contact time for the total mix of liquid and gases is about one minute, temperature is 180-190 ⁰ C and pressure is about 150 psig inlet. Reactor is packed with non porous alpha alundum spheres of approximately 1/8" diameter.

Reactor effluent is fed to a separator of two theoretical trays which are also packed with alundum spheres as is the reactor. Separator bottoms are retained as an all liquid phase with maintenance of reactor exit temperature. The liquid phase from separator bottom is charged about mid way to a distillation column. Column bottoms are split and about half recycled to column entry about 60% up column as reboiler via heat exchanger such that entry liquid from reboiler raises full charge to about 210-220°C. That portion of column bottoms not sent in column recycle is sent back to entrainment reactor to pick up gases again after pumping it back to 150 psig.

Reaction distillation column tops contain primarily methanol. This methanol may be redistilled to separate trace impurities, e.g. water from small over-oxidation.

The once through tops stripped from the half ester, anhydride catalyst bottoms are composed of methane, nitrogen and miscellaneous small components from air and the waste methane input stream. They are sent to a bed of two percent platinum metal dispersed on an active alumina of about 250 sq.m./g, surface area. Air is preheated in stainless steel coils immersed in the oxidation catalyst bed, then sent back to enter the bed with vent gases from the entrained oxidation reactor. Preheated air is used in a quantity to make the ratio of about 3 mols oxygen to 1 mol of methane. Mixed gas temperature entering this catalytic combustor will be 400-450°C. Terphenyl mixture heat exchange fluid also is passed through its catalytic combustor in tubes. It's velocity and quantity will be adequate to keep its tube temperature less than 350°C and exiting fluid about 275-300°C. This terphenyl is used to heat exchange with reboiler of the reaction/distillation system before the latter is recharged to that system's column.

Total reaction system is continuous and will be on stream around the clock until maintenance is needed. For the example we will utilize a ten minute period after system conditions are in balance. In that time we make methanol as defined above. A flow diagram delineating the process described in EXAMPLE 1 is provided in

Figure 1. The diagram traces the flow of waste methane process gas and catalysts through the entrained packed bed reactor (T) and into a packed bed separator (H). Liquid bottoms from the separator are fed to the distillation column (ID), while the gas stream is fed to the catalytic combustor/heat exchanger (JV). Bottoms from the distillation column (ED) are split, with approximately 50% reintroduced to the entrained packed bed reactor (T), and 50% reintroduced to the distillation column (EQ) after first being brought to temperature in the waste heat exchanger (TV). EXAMPLE 2

Essentially, the same as EXAMPLE 1, but with ³ A mullite inert ceramic spheres and super heated steam used as the heat exchange medium in the catalytic combustion of effluent from ethane oxidation in the phthalate system. Again, methanol is made as the product. EXAMPLE 3

Same as EXAMPLE 1, except methane is not pre-treated to remove CO ₂ and any sulrur-contaiπing components. Effluent will contain trace SO ₂ from the catalytic combustor and the feed gas CO ₂ as well as CO ₂ , H ₂ , N ₂ , etc., from air plus effluent at ~600°C. Product methanol will be essentially the same as EXAMPLE 1. EXAMPLE 4

Same as EXAMPLE 3, except the waste methanol stream is derived from animal waste. This feed has less N ₂ and CO ₂ in it than EXAMPLE 3, hence more methane.

Variations or modifications to the subject matter of the formula and process, in addition to the compound formed, namely, methanol, may occur to those skilled in the art upon review of the invention as described herein. Such variations, if within the spirit of this development, are intended to be encompassed within the scope of the invention as defined. The description of the preferred embodiment, and its summarization within the application, are set forth for illustrative purposes only.