METHOD AND SYSTEM FOR PRODUCING HYDROCARBON PRODUCTS

METHOD AND SYSTEM FOR PRODUCING HYDROCARBON PRODUCTS

DESCRIPTION OF THE INVENTION

This invention in general relates to methods for production of products, in particular, hydrocarbon products, for example, alcohols, by microbiological fermentation. In particular, invention relates to methods of producing products of fermentation from industrial gases, connected with processes reforming S02.

BACKGROUND OF THE INVENTION

In the entire world ethanol quickly becomes main rich of hydrogen liquid engine fuel. Consumption of ethanol in the entire world in 2005 g. by estimates was 12.2 billion, gallons. By Projections, production of ethanol fuel also will continue to grow in the future due to diffusion nnoi interest in ethanol Europe, Japan, SShA and in several developing countries.

For example, in SShA ethanol of mixtures therewith, representing 10% mixture of ethanol in gasoline. In mixtures of it an ethanol component acts as has enriched oxygen agent, improves efficiency of combustion and reducing isolation of atmospheric polluting substances. In Brazilii ethanol on 30% meets demand in engine fuel, as enriches oxygen agent in mixture with gasoline, and as pure fuel itself alone. In Europe ecological problems around consequences of emissions of gases, causing greenhouse effect (GHG , green house Gases), also steel stimulus for setting European Union (EC) for stranchlenov authorized purposes of consumption of ecologically rational types of motor fuel, such as ethanol, based on biomass.

Inhibiting the majority of ethanol fuel is obtained by means of traditional methods of fermentation based on yeast, which as a single source of carbon are used, obtained from cultured plants, such as sucrose, ekstragirovannaya from sugarcane, or starch, extracted from cereal crops. The fact of not less than, on cost of this initial carbohydrate raw material effect its value as products of power supply for people and feeds for animals, and growing crops, providing starch or sucrose, for production of ethanol economically irrationally in all geographic zones. Therefore is of interest the development of technologies for converting more cheap and/or more abundant carbon sources to fuel ethanol.

With is main, free, rich energy by-side product of incomplete combustion of organic materials, such as coal or petroleum and petroleum products. For example, is, that ferrous production in australia produces and releases in atmosphere above 500000 tons with annually.

For converting gases, consisting, in the main, from co and/or with and hydrogen (h2), in different types of fuel and chemical substances can be used catalytic processes. For converting these gases fuel and chemical substances may also be to use microorganisms. These biological processes, at they in whole slower, than chemical reactions, have several the following advantages as compared with catalytic process, including high specificity, higher outputs, lower energy consumption and more high resistance to to contamination.

Ability of microorganisms to grow on with as a single source of carbon is newly is open in 1903 g. Later identified, that this ability is property of organisms, using for avtotrofnogo growth biochemical path atsetilkoenzima and (acetyl CoA) (known also as biochemical path Vuda - Lyungdalya and biochemical path dehydro genazy carbon monoxide/synthase acetyl CoA (CODH/ACS)). Shown, that large number of anaerobic microorganisms, including karboksidotrofnye , fotosinteziruyushchie , mathanogenic and atsetogennye organisms, seabirds with to different final products, in other words S02 , h2, methane, n-butanol, acetate and ethanol. All such organisms, using with as a single source of carbon, produce at least two of these final products.

Shown, that anaerobic bacteria, such as bacterium of genus clostridium, produce ethanol from co, S02 and h2 by means of biochemical track acetyl CoA.

For example, various strains of clostridium ljungdahlii , producing ethanol from gases, are described in the following documents: WO 00/68407, ep 117309, Patent US 5173429, US 5593886 and US 6368819, WO 98/00558 and WO 02/08438. Also is known, that bacterium clostridium autoethanogenum sp produces ethanol from gases (Abrini et al ., archives care Microbiology 161, pp 345-351 (1994)).

At methods of fermentation of microorganisms of substrates, containing co and h2, are known, potential scaling and integration of these processes in industrial context is mastered weakly. Petrochemical works and nefteochistitelnye works is big amount of with as by-products, and potential use of this "spent" gas for production of of valuable products. Besides, at the present time considerable proportion of exhaust gases is sent in tongues developed (is burned), or alternatively is used as fuel source, where both variants is undesirable gas S02 , possessing hotbed effect.

Respectively, exists potential for updating of industrial processes due to the use of exhaust gases and produced by them energy for use in the fermentation with produce required products, simultaneously reducing the emission of the gaseous carbon from industrial enterprises.

By Projections, hydrogen becomes main starting material for use in hydrogen fuel elements, in development of for application in technologies in the range from automobiles to domestic electronic equipment. Besides, its can be used as fuel. Hydrogen also required conducted in refineries, in other words for large number of processes hydro cleaning and hydro cracking in purposes of removing sulfur, nitrogen and other impurities from raw hydro cleaning of, and also for hydro cracking more heavy gas oils to products of distillation. Since production of hydrogen is input-intensive, preferably to develop methods, enhancing efficiency of production of and regeneration of hydrogen, especially from contaminated flows. In absence of hydrogen such streams of end fuel gas or are fed to tongues developed, and hydrogen component, showing high value, effectively is lost.

Carbon dioxide (carbon dioxide; S02) at the present time is the most significant gas, by calling greenhouse effect, formed as a result of economic activity (Treacy and Ross. Prepr. pap. am. Chem.

Soc., 49 (1), 126, 2004). On industry is considerable pressure in with respect to reducing emission of carbon (including S02), and in the present time applied force to trapping carbon before ejection. Trying induce industry to limit emission of the carbon, in some jurisdictions defined economic stimulation on Your lu emissions of carbon and quotas on emission of greenhouse gases.

To promote reduced emissions S02 , exists possibility of fixation S02 in the form of chemical substance. Advantages of the fixation S02 compared with removal of S02 (for example, by sequestering in the deep ocean) lies in possibility of production of chemical substances, with economic value. At reforming S02 (sometimes called "dry" reforming) is used S02 and methane (SN4) for producing carbon monoxide and gaseous hydrogen in the form of products the following reaction:

S02 + SN4 -> 2SO + 2N2

Product of this reaction often called synthetic gas, and it represents the equimolar mixture of co and h2. Synthetic gas can be used for the production of products, possessing high value, most specifically diesel fuel, not containing sulfur, with the help of synthesis of FisheraTropsha , represented by the following equation:

pSO + (2n + 1) h2-► SpN (2n + 2) + pN20 and methanol, as shown below:

With + 2N2 -> SNzON the fact of not less than, for both of these reactions in gas line synthetic gazareagenta necessary to add h2, installation of correct ratio of reagents. Hydrogen usually delivered with the help of steam reforming SN4 , shown below:

SN4 + N20 -> ZN2 + WITH

As S02 , and SN4 represent relative to stable compound, with low potential energies. As a result of reaction of dry reforming is highly endothermic, and therefore, to direct its in correct direction, required supply of energy. Steam reforming of SN4 is also endothermic reaction. The most likely energy source, guides these reaction, is burning of natural gas, and this process itself alone forms S02.

Purpose of the of the present invention consists in development of method, overcoming or decreasing at least one of the drawbacks of previous level of technology, or at least in development of its useful for human alternative.

DESCRIPTION OF THE INVENTION

According to first aspect, invention production method hydrocarbon product, including the following stages:

i) supply of substrate, containing with and/or h2, bioreactor, containing culture of one or more microorganisms; n) fermentation culture in bioreactor to produce one or more hydrocarbon products; where substrate, containing with and/or h2, is produced from reforming process S02 , in whole certain the following equation: S02 + SN4 -► 2SO + 2N2.

Preferably a process of reforming S02 additionally includes regeneration of catalyst, as a result of which substrate, containing with and/or h2.

Preferably substrate, obtained from reforming process S02 , is passed in the module by heating of adsorption to or after receiving a bioreactor.

Preferably gaseous substrate after fermentation, coming from bioreactor, containing any one or more of the following substances: S02 , SN4 , with, N2 or h2, is received membrane module, adapted to separation of one or more gases from one or more other gases.

Preferably h2 and S02 is separated from gaseous substrate, coming from bioreactor, with the help of membrane module and passed in the module by heating of adsorption.

Preferably gaseous substrate, coming from bioreactor or membrane module, containing h2, is received modulus by heating of adsorption.

Preferably module by heating of adsorption is used for isolating h2 from gaseous substrate, coming from bioreactor or membrane module.

Preferably gaseous substrate, coming from bioreactor, membrane module or module by heating of adsorption (psa, from Eng, "pressure swing adsorption "), containing any one or more of the following gases: S02 , SN4 , with or h2, used again in the process of reforming S02.

Preferably gaseous substrate, coming from membrane module, containing any one or more of the following gases: with, SN4 and/or N2, used again in the process of reforming S02 or as gas blowing.

Preferably hydrocarbon, obtained in bioreactor, used again in the process of reforming S02.

Preferably part SN4 , used for the reforming process S02 , obtained as a result of gasification of raw material refining, for example, coal or vacuum gas oil. More preferably SN4 is component of substitute of natural gas (so-called "synthetic natural gas", spores g).

Preferably gaseous substrate, containing with and/or h2, received a bioreactor, includes additional component, representing synthetic gas or ugs, obtained from other source of, than process of reforming S02. Preferably other source, than process of reforming S02 , is gasification raw material refining, for example, coal or vacuum gas oil, at invention is not limited by this source.

Preferably hydrocarbon reagent is passed through installation of preliminary reforming before application in the process of reforming S02.

Preferably hydrocarbon reagent represents hydrocarbon, produced from bioreactor.

Preferably hydrocarbon product or hydrocarbon reagent represents either ethanol, or propanol, or butanol.

Preferably hydrocarbon product or hydrocarbon reagent represents diol, more preferably 2.3-butanediol.

Preferably 2.3-butanediol is used for of gasoline mixtures.

Preferably made hydrocarbon represents butyrate, propionate, caproate, propylene, butadiene, isobutylene or ethylene.

Preferably made hydrocarbon is component of gasoline (approximately 8 carbon atoms), jet fuel (approximately 12 carbon atoms) or diesel fuel (approximately 12 carbon atoms).

Preferably biomass is collected from the bioreactor, and this biomass undergoes anaerobic enzymatic hydro lys to obtain product biomass, preferably methane.

Preferably product biomass is used as reagent for reforming process S02.

Preferably product biomass is used for producing additional of heat for conducting one or more reactions, certain in the given invention.

According to the second aspect, a process of reforming S02 , in whole certain the following equation:

S02 + SN4 -> 2SO + 2N2

where S02 and/or SN4 and/or components for producing S02 and/or SN4 is produced from bioreactor, containing culture of one or more microorganisms, adapted to producing one or more hydrocarbon products by fermentation gaseous substrate, containing with and/or h2.

Preferably a process of reforming S02 is used for treatment and/or for producing substrate, containing with and/or h2, for bioreactor.

Preferably gaseous substrate, containing with and/or h2, received a bioreactor, represents gas process of producing high-quality iron with use of non-coking coal without contamination of environment and preferably contains any one or more of the following gases: with, h2, S02 , 1 or SN4.

To avoid doubt, output from the bioreactor may undergo one or more stages of treatment before introduction into the process of reforming.

Other signs of the method of the second aspect are similar to features of the method of the first aspect.

The third aspect, in present invention provides a system for production of hydrocarbon product, comprising the following elements:

bioreactor, containing culture of one or more microorganisms, adapted to producing hydrocarbon product by fermentation substrate, containing with and/or h2, where this substrate is obtained from module reforming S02 , suitable made reforming process S02 , in whole certain the following equation:

S02 + SN4 -> 2SO + 2N2.

Preferably module reforming S02 additionally includes regenerator, adapted to catalyst regeneration by burning carbon-containing deposits on a catalyst.

Preferably system includes module of gasification, adapted to gasification of raw material refining to produce synthetic gas, which can be used as component of co-containing substrate, received a bioreactor.

Preferably synthetic gas is received modulus substitute of natural gas (ugs), rim adapted to conversion of synthetic gas in ugs. Preferably module reforming S02 is adapted to receive signal ugs for use in the process of reforming S02.

Preferably bioreactor is adapted to receive signal substrate, containing with and/or h2, from module psa or to passage of this substrate in the module psa.

Preferably system additionally includes membrane module, adapted to receive signal gaseous substrate, containing any one or more of the following gases: S02 , SN4 , with, 1 or h2, from the bioreactor and to separation of one or more gases from one or more other gases. More preferably membrane module is adapted to separation of h2 and/or S02 from gaseous substrate.

Preferably module psa is adapted to receive signal gaseous substrate from bioreactor or from membrane module.

Preferably module psa is adapted to separation of h2 from gaseous substrate.

Preferably module reforming S02 is adapted to receive signal gaseous substrate from bioreactor, membrane module or module psa, where gaseous substrate contains any one or more of the following gases: S02 , h2, with and/or SN4.

Preferably module reforming S02 is adapted to receive signal of hydrocarbon, obtained in bioreactor.

Preferably module reforming S02 is adapted to receive signal of hydrocarbon from module preliminary reforming.

Preferably module preliminary reforming is adapted to receive signal of hydrocarbon, obtained in bioreactor.

Preferably hydrocarbon represents either ethanol, or propanol, or butanol.

Preferably hydrocarbon represents diol, more preferably 2.3-butanediol.

Preferably 2, 3-butanediol is used for of gasoline mixtures.

Preferably made hydrocarbon represents butyrate, propionate, caproate, propylene, butadiene, isobutylene or ethylene.

Preferably made hydrocarbon represents gasoline (approximately 8 carbon atoms), jet fuel (approximately 12 carbon atoms) or diesel fuel (approximately 12 carbon atoms)..

As understandable, any of above mentioned hydrocarbon products can be obtained directly or indirectly, i.e. for producing desired final products can be used additional processing modules.

Preferably module enzymatic hydro lipolysis is adapted to receive signal biomass from the bioreactor and to production of product biomass, preferably methane.

Preferably module reforming S02 is adapted to receive signal product biomass, used as reagent for reforming process S02.

Preferably module enzymatic hydro lipolysis is adapted to production of additional of heat for feeding in one or more other modules, described in the given invention.

According to fourth aspect, in-module reforming S02 , adapted to of process, in whole certain the following equation:

S02 + SN4 -> 2SO + 2N2

where S02 and/or SN4 and/or components for synthesis of these compounds is produced from bioreactor, suitable to production of one or more hydrocarbon products by microbiological fermentation of gaseous substrate, containing with and/or h2.

Preferably module reforming S02 is adapted to the treatment and/or supply of substrate, containing with and/or h2, into bioreactor.

Preferably bioreactor is adapted to receive signal gas process of producing high-quality iron with use of non-coking coal without contamination of environment, preferably containing any one or more than one of the following gases: with, h2, S02 , N2 or SN4.

Other signs of system of the fourth aspect are similar to features system of the third aspect.

According to fifth aspect, in-method of catching carbon from substrate, containing with, including the following stages:

(a) supply of substrate, containing with and/or h2, bioreactor, containing culture of one or more microorganisms ; (b) fermentation culture in bioreactor to produce one or more hydrocarbon products; where substrate, containing with, is obtained from module reforming S02 , suitable made reforming process S02 , in whole certain the following equation:

S02 + SN4 -> 2SO + 2N2.

Preferably substrate, containing with, is obtained from the device by heating of adsorption.

Preferably substrate, containing with, additionally contains h2.

According to sixth aspect, in-method of catching carbon from substrate, containing with, at which:

substrate, containing with and/or h2, is fed into a bioreactor, containing culture of one or more microorganisms, and is fermented in bioreactor with produce one or more hydrocarbon products; where said method includes the following stages:

feeding one or more products and/or by-products and/or wastes of bioreactor and/or their derivatives in the module reforming S02 , adapted to of reforming process S02 , in whole certain the following equation:

C02 + CH4-> 2C0 + 2H2.

According to seventh aspect, in-hydrocarbon product, produced by the first, or second, or fifth, or sixth aspect, or with the help of system of third or fourth aspect.

Preferably hydrocarbon product represents alcohol, acid or diol.

Preferably made hydrocarbon represents butyrate, propionate, caproate, propylene, butadiene, isobutylene or ethylene.

Preferably made hydrocarbon is component of gasoline (approximately 8 carbon atoms), jet fuel (approximately 12 carbon atoms) or diesel fuel (approximately 12 carbon atoms).

According to seventh aspect, in-hydrogen, obtained in reforming S02 , where hydrogen are obtained from bioreactor, containing culture of one or more microorganisms.

Professionals in this engineering understandable, process reforming S02 , in whole certain the following equation:

S02 + SN4 -> 2SO + 2N2

may include additional stage or reaction, which are made to, after above described reaction or simultaneously with it. Aspects of the invention, certain in the description, in equal degree of are used to these through additional or reactions.

Invention also involves part, members and signs, on which present in this operation, and part of, members and signs, specified in the description given of operation, separately or all together, in any combination or in all combinations of two or more parts, elements or features, and also, if are given certain integers, having known equivalents in engineering, to which-this invention, such known equivalents is considered to be connected in this invention as indicated individually.

DESCRIPTION OF GRAPHIC MATERIALS

Data aspects, and other aspects of the present invention, which should be viewed in all its new aspects, , as apparent from subsequent description, which is put only in one, with a reference to the accompanying graphic materials, in which:

On Figure 1 is indicated illustrative system and method in accordance with one form of realization.

On Figure 2 is illustrative system and method in accordance with one form of realization, in which modules of the system are combined for producing diffusion nnoi efficiency and diffusion nnogo catching carbon.

On Figure 3 is illustrative system, including gasification system, functionally connected with system reforming S02.

Should be mentioned, that blocks at Figure 1 are presented as stage of the method, so and components of physical system. Besides, understandable, that given of system are only preferable, and the alternative one order and combination of stages and of modules process are connected in volume-.

OF CONVERGENCE. CONFIRMING POSSIBILITY OF

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Definitions if not determined other, described below terms, used during the whole of this description, are determined, as described below:

Term "substrate, containing carbon monoxide and/or hydrogen" and the like terms should be understand as including any substrate, in which carbon monoxide and/or hydrogen are accessible for growth and/or fermentation, for example, one or more strains of bacteria.

"Gaseous substrate, containing carbon monoxide and/or hydrogen" includes any gas, containing carbon monoxide and/or hydrogen. Gaseous substrate can contain significant share with, preferably at least approximately from 2% to approximately 100% with volume and/or preferably approximately from 0% to approximately 95% of hydrogen by volume.

In a context of products of fermentation term "acid", used in this description, includes as carboxylic acids, and associated carboxylate anion, for example, mixture of free acetic acid and acetate, in enzyme broth, as described in this operation. Ratio of molecular of acid to carboxylate in enzyme broth depends on ph system. Term "acetate" includes as exclusively salt acetate, so and mixture of molecular or free acetic acid and salt acetate, such as mixture of salt acetate and free of acetic acid, in enzyme broth, as can be described in this operation. Ratio of molecular to acetic acid wherein in enzyme broth depends on ph system.

Term "hydrocarbon" includes any compound, including hydrogen atoms and carbon. Term "hydrocarbon" includes as pure hydrocarbons, consisting of hydrogen atoms and carbon, and mixed hydrocarbons and substituted hydrocarbons. Mixed hydrocarbons contain atoms of carbon and hydrogen, connected with other atoms of. Substituted hydrocarbons are formed by substituting at least one hydrogen atom atom of other element. Term "hydrocarbon", used in this operation, includes compounds, including hydrogen atoms and carbon, and optionally one or more other atoms. One or more other atoms includes, but not is limited by them, oxygen atoms, nitrogen and sulfur. Compound, enclosed by term "hydrocarbon", used in this operation, include at least acetate/acetic acid; ethanol, propanol, butanol, 2.3-butanediol, butyrate, propionate, caproate, propylene, butadiene, isobutylene, ethylene, gasoline, jet fuel or diesel fuel.

Term "bioreactor" includes device fermentation, consisting of one or more vessels and/or columns or piping systems, besides, this device includes chemical flow reactor with a stirrer (CSTR , continuous Stirred tank Reactor), reactor with immobilized cells (icr, Immobilized cell Reactor), reactor with watered layer (TBR , Trickle bed Reactor), the bubbling fermenter, gas-lift fermenter, membrane reactor, such as membrane bioreactor with system of hollow fibers (HFMBR , hollow fibre MembraneBioreactor), static mixing device, or another vessel or other device, suitable for gas-liquid stnogo contact.

If context does not require other, expression "fermentation", "fermentation process" or "reaction fermentation" and the like, as is used in this operation, imply as including as growth phase, and phase biosynthesis product this process. As described in this description below, in some forms of realization bioreactor may include first reactor for growing and second reactor for fermentation. Addition of metals or compositions in reaction fermentation, so, should be understand as including addition of in any of these reactions or in both these reaction.

"Enzymatic broth" is determined as culture medium, in which there is fermentation.

"Raw material for refining" is determined as product or combination of products, obtained from crude oil or coal and intended for further treatment in nefteochistitelnoi industry, except for preparing mixtures. These products are converted into one or more components and/or finished products and may include coal, heavy fuel oil, vacuum gas oil and severe residual raw material.

"Severe residual raw material" is determined as very high boiling fraction of oil, frequently formed in the form of the heavy fraction from the system of distillation of crude petroleum.

"Process of refining" includes any process, usually performed at cleaning oil or in similar industrial conditions, including, but not confining them, cracking on flyuidizirovannom catalyst, catalytic reforming of gasoline fractions with continuous regeneration, gasification, reforming of S02 , steam reforming of and short-cycle adsorption.

Process of reforming S02 in the process of reforming S02 is used S02 and hydrocarbon reagent (mainly, methane from natural gas), and this of the process as a whole is determined the following equation:

S02 + SN4 -> 2SO + 2N2.

If in this operation present into methane, professionals in this engineering understandable, in alternative forms of invention in the process of reforming S02 can be used other suitable hydrocarbon reagents, for example, the following reagents: ethanol, methanol, propane, gasoline, automobile propane-butane and diesel fuel, all of which may have different ratio of reagents and optimal conditions.

At characteristic the process of reforming S02 methane with S02 in molar ratio of methane: S02 , equal to 1:1, at pressure, from 1 to 20 atm, and at temperature, component approximately 900-1 100° with in the presence of catalyst. Suitable catalysts are known in this engineering.

Traditional reforming reactor S02 represents gas generator with loosened layer of coal, in which is fed gas and is passed through fixed bed of catalyst particles. Since reaction reforming S02 are formed deposition of carbon, which can to prevent catalyst activity, for suppressing this properties can be used alternative system of reactors. For example, system fluidized bed reactor well known in nefteochistitelnoi and petrochemical industry.

Catalyst particles form a fluidized layer at usage of flow of gas supply, which can comprise as from reaction compounds, and of inert compounds. Catalyst is transferred in regenerator, in which flow of gas, oxygen-containing, for example, air, for burning deposits of carbon. In a result of this burning is formed gaseous substrate, containing ranging lobe with and/or h2, which may approach for passing into bioreactor for fermentation gas to produce hydrocarbon product. Regenerated catalyst is recycled into reactor. Stage catalyst regeneration also provides of heat transfer in system reactors, since exothermal reaction, connected with by burning carbon, is heat. Catalyst particles serve as medium for transmission in system of reactors of this heat of, useful for endothermic reaction reforming S02. Alternatively system reactors could least consist of multiple gas generators with loosened layer of coal, in which in any given moment of time in one or more reactors of gas, containing methane and S02 , in conditions of, suitable for reaction of reforming S02 , and in one or more systems reactors of gas, containing oxygen, for burning carbon, Suspend to the catalyst particles.

Process reforming S02 in characteristic case are stage by heating of adsorption (PSA) for isolating flow of purified hydrogen.

Gas flow from the reforming process S02 goes to system molecular sieves, which adsorbs S02 , co and SN4 at high pressure. Hydrogen is able pass through a sieve, and its is isolated for other applications. As only sieve is saturated, the pressure is released, as a result of which desorbed gases, using minimum possible quantity of hydrogen product.

Degree of regeneration depends from pressure, since greater number of adsorbed molecules of released during more low pressure regeneration. This, in its turn, leads to yield hydrogen.

Consequently, pressure regeneration, approximation to atmospheric pressure, maximize storage hydrogen output. Then vessel again podkachivayut of hydrogen, and it is ready to the next period of as adsorbent. Available sale of system in characteristic case include three or four vessel, that provides uninterrupted operation.

Product of interaction of S02 frequently called synthetic gas, which represents a equimolar mixture of co and h2. Synthetic gas can be used for obtaining products, possessing high value, most specifically diesel fuel, not containing sulfur, with the help of synthesis of FisheraTropsha , as shown below:

pSO + (2n + 1) h2-► SpN (2n + 2) + pN20 and methanol, as shown below:

With + 2N2 -> SNzON the fact of not less than, for both of these reactions in gas line synthetic gazareagenta necessary to add h2, installation of correct ratio of reagents. Hydrogen usually delivered with the help of steam reforming SN4 , shown below:

SN4 + N20 -> ZN2 + WITH

In this invention method Your condensate content with gas, produced from reforming process S02. Among advantages of this method is then, that level of additional hydrogen, required for diesel fuel production, not containing sulfur, and methanol, reduced or eliminiruetsya. In-second, the present invention provides separation of hydrogen from gas, produced from reforming process S02 , which can be used as source of fuel, for example, for providing energy for reaction of reforming S02 , or used as chemical raw material, for example, required in the processes of refining for various purification processes. Third, the present invention provides conversion of by-product of fermentation process S02 in co and h2, boost, so, efficiency of fermentation. -Fourth, the present invention provides conversion of external sources S02 in hydrocarbon products.

According to one form of realization in this invention a bioreactor, which receives substrate, containing with and/or h2, from process reforming S02. This bioreactor contains culture of one or more microorganisms, able to fermentation of substrate, containing with and/or h2, with hydrocarbon product. So, process stages reforming S02 can be used for producing or improving composition gaseous substrate for fermentation process.

Preferably bioreactor is able to receive signal substrate, containing with and/or h2, and contains culture of one or more microorganisms, able to fermentation of substrate, containing with and/or h2, with hydrocarbon product.

According to alternative form of realization process of reforming S02 can be to modify the due to supply of of bioreactor in the process of reforming S02. Preferably this output represents gas, which can to increase efficiency of the process and/or total trapping of the desired product (for example, carbon or h2).

Invention is combined system modules and processes, showing diffusion nnoi efficiency and diffusion nnym trapping of carbon.

Illustrative system, showing this combining, is presented on Figure 2.

According to one more form of realization, presented on Figure 3, invention provides preparing part SN4 , used for the reforming process S02 , as a result of gasification of raw material refining, for example, coal or vacuum gas oil. Gasification may be made in accordance with methods, known in this engineering. The gasification process includes interaction of raw material refining, for example, coal or vacuum gas oil, with oxygen, preferably with air, to produce synthetic gas.

Synthetic gas can be optionally passed in the module substitute of natural gas (ugs), which converts synthetic gas in ugs. Ugs includes, mainly, SN4. Invention provides application ugs in addition or instead SN4 from natural gas for process of refining, preferably reforming process S02. Synthetic gas, obtained in gasification process, may also be delivered in bioreactor in combination with synthetic gas, obtained in the process of reforming S02 , for production of hydrocarbon product. Any with or S02 , coming from bioreactor, may be subjected to recirculation for use in the process of reforming S02 or in other the process of refining. Residual ugs may be export on the market delivery domestic gas or used in other processes refining. One of the advantages described above form of realization consists in the fact, that the gasification process, the process of production of ugs, process of reforming S02 and fermentation process gas are combined, as a result of which is increased efficiency of trapping of carbon and formation of hydrocarbon product as compared with known methods.

Preferably gaseous substrate, containing with and/or h2, received a bioreactor, has additional component, including synthetic gas or ugs, obtained from other source of, than process of reforming S02. Preferably other source, than process of reforming S02 , is gasification raw material refining, for example, coal or vacuum gas oil.

Bioreactor fermentation can be in any suitable bioreactor, such as chemical flow reactor with a stirrer (CSTR , continuous Stirred tank Reactor), reactor with immobilized cells (icr, Immobilized cell Reactor), gas-lift fermenter, the bubbling fermenter (of bcr, bubble column Reactor), membrane reactor, such as membrane bioreactor with system of hollow fibers (HFMBR , hollow fibre MembraneBioreactor) or the reactor with watered layer (TBR , trickle bed Reactor). In some forms of invention implementation bioreactor may also include first reactor for growing, in which bacteria are cultured, and second reactor fermentation, in which can be delivered enzymatic broth from reactor for growing, and in which can be to produce larger part of fermentation product (for example, ethanol and acetate).

Bioreactor according to the present invention is adapted to receive signal substrate, containing with and/or h2.

System reforming S02 bioreactor may be part of the system for producing hydrocarbon product, which in common form of is presented on Figure 1 and includes one or more modules, selected from the group, including the following modules:

module reforming S02 , adapted to production with and/or h2 according to process of reforming S02 , in whole definite the following equation:

S02 + SN4 -> 2SO + 2N2 ;

module by heating of adsorption (PSA), adapted separation from gaseous substrate; membrane module, adapted to separation of one or more gases from one or more other gases, more preferably for separating h2 and S02 from gaseous substrate, containing any one or more of the following gases: with, h2, S02 , 1 and SN4 ; module enzymatic hydro lipolysis, adapted to receive signal biomass from the bioreactor and production of product biomass, preferably methane.

Module psa may be adapted to receive signal substrate from any one or more modules or from the bioreactor. Module psa is adapted to separation of hydrogen from substrate. Substrate after fermentation from the bioreactor may contain with and/or h2, and this substrate can be optionally subjected to recirculation in the bioreactor with hydrocarbon product.

Alternatively hydrocarbon, produced by the bioreactor, can be used as raw material for reforming process S02.

System may optionally include module preliminary reforming, adapted to receive signal of hydrocarbon, which can be obtained from the bioreactor. Module preliminary reforming is able to cleave more heavy hydrocarbons with means of process of preliminary reforming to produce methane or other hydrocarbons, suitable for reforming process S02.

Professionals in this engineering understandable, that modules, certain in this description, may be functionally combined in any suitable system for performing production of the desired product.

Substrate, containing with and/or h2 substrate, containing with and/or h2, is trapped or is directed along channel from process, using any convenient method. Depending on composition of substrate, containing with and/or h2, before its introduction in fermentation can also be preferably treated with its for removing any-either unnecessary impurities, such as particles of dust. For example, this substrate can be filtered or subjected to scrubbing clearance by, using known methods.

In characteristic case with added into reaction fermentation in gaseous state. The fact of not less than, methods according to the invention are not limited by addition of substrate in said state. For example, carbon monoxide can be obtained in the form of liquid sti. For example, liquid st can be satiate gas, containing carbon monoxide, and add this liquid st into bioreactor. This action can be made with using standard methodologies. One, for this purpose can be used generator of dispersion of microbubbles (Hensirisak et. al. Scale-up care microbubbledispersion the generator for aerobicfermentation ; AppliedBiochemistry and biotechnology volume 101. Number 3/ October. 20021. At link on "gas flow" in present operation of this term also includes other forms of transportation of gaseous components of this flow, such as method of saturation liquid sti, described above.

Composition of gas with-containing substrate may contain any share with, for example, at least approximately from 20% to approximately 100% with by volume, from 40% to 95% with by volume, from 40% to 60% with by volume and from 45% to 55% with by volume. In specific forms of realization substrate contains approximately 25%, or approximately 30%, or approximately 35%, or approximately 40%, or approximately 45%, or approximately 50% with, or approximately 55% with, or approximately 60% with by volume. Substrates, having more low concentration of with, such as 2%, may also approach, in particular, when there are also h2 and S02.

In specific form of realization substrate, containing with and/or h2, represents gas process of producing high-quality iron with use of non-coking coal without contamination of environment.

Typical composition of gas process of producing high-quality cast iron includes the following gases: h2 (16.1%), with (43%), S02 (36.5%), N2 (2, 8%)and SN4 (1.6%). Invention a method of converting S02 and SN4 in gas process of producing high-quality cast iron in useful raw material for fermentation, providing, so, additional utilization of gas process of producing high-quality cast iron.

Presence of h2 must not harmful for formation of hydrocarbon product by fermentation. In specific forms of realization as a result of presence of hydrogen increased total efficiency of production of alcohol. For example, in specific forms of realization ratio of h2: with substrate may be 2:1, or 1:1, or 1:2. In other forms of realization substrate, containing with, contains less than approximately 30% of h2, or less 27% h2, or less 20% h2, or less 10% h2, or more low concentration of h2, for example, less than 5%, or less than 4%, or less than 3%, or less than 2%, or less than 1%, or has no hydrogen. In other forms of realization substrate, containing with, contains more than 50% of h2, or more than 60% of h2, or more than 70% of h2, or more than 80% of h2, or more than 90% of h2.

At stage psa hydrogen is isolated from substrate, produced from reforming process S02 , made from membrane module or from the bioreactor. In characteristic form of realization substrate, coming from stage psa, has approximately 10-35% h2. H2 may be passed through bioreactor and to separate from the substrate. In specific the form of-h2 is subjected to recirculation in stage psa for isolating from substrate. Substrate can also contain some amount of S02 , equal to, for example, approximately from 1% to approximately 80% S02 by volume, or from 1% to approximately 30% S02 by volume.

Fermentation methods of production of ethanol and other alcohols from gaseous substrates are known. Pictorial methods include, for example, methods, described in the following documents: W02007/117157, W02008/1 15080, W02009/022925, W02009/064200, US 6340581, US 6136577, US 5593886, US 5807722 and US 5821111, where each document is placed in the present description by references.

Microorganisms in various forms of realization fermentation is made, using culture of one or more strains of karboksidotrofnykh bacteria. In various forms realization karboksidotrofnaya bacterium is selected from the following delivery of bacteria: Moorella , clostridium, Ruminococcus , Acetobacterium , Eubacterium , Butyribacterium , Oxobacter , Methanosarcina , Methanosarcina and Desulfotomaculum.

Is known, that large number of anaerobic bacteria may fermentation with to alcohols, including n-butanol and ethanol, and acetic acid, and these bacteria are suitable for use in the method according to the present invention.

Examples of bacteria, suitable for use in invention, include bacteria of genus clostridium, such as strains of clostridium ljungdahlii , including strains, described in the following documents: WO 00/68407, ep 117309, Patent US 5173429, US 5593886 and US 6368819, WO 98/00558 and WO 02/08438, clostridium carboxydivorans (Liou et al ., international Journal care Systematic and EvolutionaryMicrobiology 33:pp 2085-2091), clostridium ragsdalei (WO/2008/028055) and clostridium autoethanogenum (Abrini et al, archives care Microbiology 161 : pp 345-351). Other suitable bacteria include bacteria of genus Moorella , including Moorella sp HUC22-1, (Sakai et al, biotechnology Letters 29:pp 1607-1612), and bacterium of genus Carboxydothermus (Svetlichny , V. a., Sokolova , T.G. et al (1991), Systematic and AppliedMicrobiology 14 : 254-260). Additional examples include the following bacteria:

Moorellathermoacetica , Moorellathermoautotrophica , Ruminococcusproductus , Acetobacteriumwoodii , Eubacteriumlimosum , Butyribacteriummethylotrophicum , Oxobacterpfennigii , Methanosarcinabarkeri , Methanosarcinaacetivorans , Desulfotomaculumkuznetsovii (Simpa et. al. Critical reviews in biotechnology, 2006 vol.

26. Pp41-65). Besides, understandable, that in present invention can be can be used other atsetogennye anaerobic bacteria, known professionals in this engineering. Also understandable, that this invention can be applied to mixed culture of two or more bacteria.

One of the illustrative microorganisms, suitable for use in this invention, is bacterium clostridium autoethanogenum. In one form of realization clostridium autoethanogenum represents bacterium clostridium autoethanogenum , possessing identification characteristics of strain, deposited in German collection of microorganisms and cell cultures (DSMZ) under identification deposit number 19630. In the other form of realization clostridium autoethanogenum represents bacterium clostridium autoethanogenum , possessing identification characteristics of strain DSMZ , escrow number DSMZ 10061. In the other form of realization clostridium autoethanogenum represents bacterium clostridium autoethanogenum , possessing identification characteristics of strain DSMZ , escrow number DSMZ 23693. These strains have special tolerance changes composition substrate, in particular, of h2 and with, and, so, they especially well are suitable for use in combination with process of reforming S02.

Culturing bacteria, used in methods according to the invention, may be made, using different methods, known engineering for culturing and fermentation substrates using anaerobic bacteria. One, can be used methods with use of gaseous substrates, in common described in the following articles : (i) to. T.

Klasson , et al. (1991). Bioreactors for synthesis gas fermentations resources.

Conservation and recycling, 5 ; 145-165 ; (ii) to. t. Klasson , et al. (1991). Bioreactor design for synthesis gas fermentations. Fuel. 70. 605-614 ; (iii) to. t. Klasson , et al. (1992).

Bioconversion care synthesis gas into liquid or gaseous fuels. Enzyme and Microbial technology. 14 ; 602-608 ; (iv) j. l. Vega , et al. (1989). Study care GaseousSubstrateFermentation : carbon MonoxideConversion to Acetate. 2. Continuous Culture. Biotech.

Bioeng. 34. 6. 785-793 ; (v) j. l. Vega , et al. (1989). Study care gaseoussubstratefermentations : carbon monoxideconversion to acetate. 1. Batch culture. Biotechnology and Bioengineering. 34. 6. 774-784 ; (vi) j. l. Vega , et al. (1990). Design care Bioreactors for Coal synthesis gas Fermentations. Resources, Conservation and recycling. 3. 149160 ; all these article are connected in the present description by references.

Conditions of fermentation understandable, that for growing bacteria for conducting fermentation from with to of hydrocarbon, in addition to co-containing substrate into bioreactor should be to supply suitable liquid nutrient medium. Nutrient medium has sufficient amount of vitamins and minerals, to give possibility for growth used microorganism. Anaerobic medium, suitable for production of hydrocarbon products by fermentation, using with as a single source of carbon, are known in this engineering.

For example, suitable medium are described in Patent US 5173429 and US 5593886, and also in the following documents: WO 02/08438, W02007/1 15157 and W02008/1 15080, on which present above.

Fermentation preferably in appropriate conditions for passage of desired fermentation (for example, from with to ethanol). Reaction conditions, which should be consider, include the following conditions: pressure, temperature, speed of gas flow, rate of flow liquid sti, ph medium, oxidation-reduction potential medium, rate of mixing (at usage of chemical flow reactor with mixer), level of inokuluma , maximum concentration of gaseous substrate, is, that concentration of with in liquid phase becomes limiting, and maximum concentration of product, to avoid inhibition of product. Suitable conditions are described in the following documents: W002/08438, WO07/1 17157 and WO08/1 15080.

Optimal conditions reaction partially depend on specific used microorganism. The fact of not less than, in whole preferable to conduct fermentation at pressure, exceeding pressure of environment. Operation at diffusion possible in the freely chosen pressures gives possibility of considerably increase the transfer rate with from gas phase in liquid phase, where it may cause absorption microorganism as the source of carbon for producing hydrocarbon products. This, in its turn, means, that residence time (determined as volume of liquid sti in bioreactor, divided on speed of incoming gas flow) can be reduced, if maintain bioreactors at diffusion nnom pressure of more likely, than at atmospheric pressure. Since this rate of conversion of with in hydrocarbon partially depends on residence time of substrate, and achievement of required residence time, in its turn, determines the required volume of bioreactor, use of systems under pressure can also considerably to reduce required volume of the bioreactor and, consequently, increase equipment for fermentation. In accordance with the examples, given in A US 5593886, volume of reactor can be to reduce in linear ratio to diffusion Exploration pressure of reactor operation, i.e. volume of bioreactors, operating at a pressure, equal to 10 atmospheres, should be only tenth part of bioreactors, operating at a pressure, equal to 1 atmosphere.

Advantages of the conducting fermentation gas to hydrocarbon at diffusion possible in the freely chosen pressures Described also in other documents. For example, in document WO 02/08438 described fermentation gas to ethanol, conducted at pressures, components 2.1 atm and 5.3 atm, to obtain efficiency, component 150 g/l/day and 369 g/l/day of ethanol, respectively. The fact of not less than, was recognized, that approximate fermentation, directed using such same medium and same compositions incoming gas at atmospheric pressure, is performed in 10-20 times smaller than ethanol on litre of a day.

Also preferably, to rate of introduction of co-containing gaseous substrate has such value, is, that concentration of with in liquid phase becomes limiting. This is connected with the fact, that due to SOogranichivayushchikh conditions hydrocarbon product may be consumed by culture.

Products of fermentation methods by invention can be used for production of any of various hydrocarbon products. These products include alcohols, acid and/or diols. More specifically, the invention can be applied to fermentation for production of butirata , propionate, kaproata , ethanol, propanol, butanol, 2.3-butanediol, propylene, butadiene, isobutylene and ethylene. Above described products, and other products may possess value as material base other processes, such as production of polymers, pharmaceutical preparations and agrochemical agents. In specific form of realization product of fermentation is used for production of hydrocarbons gasoline row of (approximately 8 carbon atoms), diesel hydrocarbons (approximately 12 carbon atoms) or hydrocarbons jet fuel (approximately 12 carbon atoms).

Invention also provides, that at least part of the hydrocarbon product, obtained in fermentation, repeatedly is used in the process of reforming S02. In specific form of realization ethanol is subjected to recirculation for use as raw material for the reforming process S02. In additional the form of realization hydrocarbon raw material and/or product is passed through device preliminary reforming before application in the process of reforming S02. Passing through device preliminary reforming partially complements the a steam reforming stage process of steam reforming, which can to increase efficiency of production of hydrogen and reduced power consumption of reactor reforming S02.

Methods according to the invention may also be used to by aerobic fermentatsiyam and to anaerobic or by aerobic fermentatsiyam other products, including, but not limited by them, isopropanol.

Isolation of product of reaction products of fermentation can be to detect, using known methods. Pictorial methods include methods, described in the following documents: WO07/117157, WO08/1 15080, US 6340581, US 6136577, US 5593886, US 5807722 and US 5821111. The fact of not less than, in transcribed and in one, ethanol one can discern from enzymatic broth such methods, as fractional distillation or evaporation, and also extractive fermentation.

As a result of of distillation of ethanol from fermentation broth is obtained azeotropic mixture of ethanol and water (i.e. 95% ethanol and 5% water). Then can be anhydrous ethanol by means of application technology dehydration of ethanol with means of molecular sieves, which also well is known in this engineering.

Methods of extractive fermentation include application for extracting ethanol from diluted enzymatic broth mixed with water of solvent, which is low risk of toxicity for fermenting organism. For example, oleyl alcohol is solvent, which can be used in the process of extraction of this type. Oleyl alcohol is continuously introduced into fermenter, where this solvent causes formation of layer in upper part of fermenter, which continuously extracted and is fed through centrifuge. Then water and cells easily separated from oleilovogo alcohol and returned into fermenter, at that solvent with layer is fed in device instantaneous evaporation. Larger part of ethanol evaporates and is condensed, while oleyl alcohol is nonvolatile, and its is isolated for repeated use in fermentation.

Acetate, which can be obtained as by-product fermentation reaction, may also be to isolate from enzymatic broth, using methods, known engineering.

For example, can be used adsorption system, including activated carbon filter. In this case preferably first remove bacterial cells from enzymatic broth, using suitable separating device. In this engineering are known much numerical methods for preparing acellular enzymatic broth for isolation of the product, based on filtration. Then cell-free permeat , containing ethanol and acetate, is passed through column, containing activated carbon, for adsorption of acetate. Acetate in the form of acid (acetic acid) lighter-than-adsorbed activated carbon, than salt form (acetate). Therefore before passing fermentation broth through column with activated carbon preferably decrease of its ph to value, component of less than approximately 3, to transform main part acetate in the form of acetic acid.

Acetic acid, adsorbed on activated carbon, one can discern by elution, using methods, known engineering. For example, for elution connected acetate can be used ethanol. In some forms of realization for elution acetate can be used itself ethanol, obtained by fermentation process.

Because boiling temperature ethanol 78.8 ° with, and boiling temperature acetic acid is 107° with, ethanol and acetate can be easily separate from each other, using method, based on volatility, such as distillation.

Other methods of isolating acetate from enzymatic broth also are known in this engineering and can be used. For example, in Patent US 6368819 and US 6753170 a system solvent and cosolvent, which may be used for extraction of acetic acid from enzymatic broths. Similarly example system based on oleilovogo alcohol, described for extractive fermentation of ethanol, in systems, described in Patent US 6368819 and US 6753170, described is non-miscible with water solvent/cosolvent, which can be combined with enzymatic broth or in the presence of, or in the absence of fermentiruyushchikh microorganisms with for extraction of product, representing acetic acid. Then solvent/cosolvent, containing product, representing acetic acid, is separated from the broth by distillation.

Then can be used the second stage of distillation, to purification of acetic acid from system of solvent/cosolvent.

Products of reaction of fermentation (for example, ethanol and acetate) can from enzymatic broth by continuous extraction of part of broth from the bioreactor fermentation, separation of bacterial cells from broth (convenient by filtration) and isolation of one or more products from broth simultaneously or sequentially. In case of ethanol it may be convenient to separate by distillation, and acetate can by adsorption on activated carbon, using the described above methods. Separated bacterial cells preferably returned into bioreactor fermentation.

Cell-free permeat , remained after isolation of ethanol and acetate, also preferably returned into bioreactor fermentation. To replenish nutrient medium, before return into bioreactor cell permeat can be added additional nutrients (such as vitamins in). Also, if ph broth was brought, as described above, for reinforcing adsorption of acetic acid on activated carbon, before return into bioreactor ph should be again bring to value ph broth in bioreactor fermentation.

Biomass, isolated from the bioreactor, can undergo anaerobic enzymatic hydro lys in module enzymatic hydro lipolysis to obtain product biomass, preferably methane. The product biomass can be used as raw material for reforming process S02 (optionally through module preliminary reforming) or used for producing additional heat of, guide one or more reactions, described in the given invention.

Separation/preparing gas fermentation according to the present invention has advantage, consists in the fact, that it is stable to use substrates with impurities and differing in concentration of gas. Respectively, production of hydrocarbon product yet is at application of a wide range of compositions of gas as substrate fermentation. Reaction fermentation may also be used as method of separating and/or catching of certain gases (for example, with) of substrate and for concentration of gases, for example, of h2, for subsequent isolation of. At application in combination with one or more other processes, certain in this invention, reaction of fermentation can reduced concentration with in gas flow (substrate), and, consequently, concentrating h2, so, providing diffusion nnyi output h2.

Gas flow from the reforming process S02 may be passed directly in bioreactor for fermentation. Alternatively process of reforming S02 can obtain gaseous substrate from the bioreactor, optionally through other processes. These different system may possess advantage as a result of Your condensate costs and any-either energy losses, associated with intermediate stages. Besides, these system may to modify the fermentation process due to substrate, with high contents of with.

Since composition of gas flow changes in time of its passage through bioreactor, after fermentation can be more efficiently perform trapping its components. Passing this flow to the stage reforming S02 can, so, to increase efficiency of the reforming process S02 and/or catching of one or more components of flow. For example, execution of stage psa after fermentation allows for higher pressure regeneration. At this reduces hydrogen output via the stage psa, hydrogen can be isolated from at least part of the fermentation product. Higher pressure regeneration gives possibility for less stringent operation conditions on stage psa.

In specific form of realization invention a membrane module, adapted to receive signal gaseous substrate from the bioreactor. In characteristic case of gaseous substrate from the bioreactor contains the following gases: with, h2, S02 , 1 or SN4 , and membrane module preferably is adapted to separation of one or more gases of gaseous substrate. More preferably membrane module is adapted to separation of h2 and/or S02 from gaseous substrate. This separation of (a) increases efficiency of isolating h2 from substrate ; (b) gives possibility of recirculation of separated gases, preferably including with, SN4 and/or 1, in bioreactor or blowing their from the system; and/or (with) enhanced purity of reagents, passing through in the module reforming S02.

Three-reforming in this invention also considered, that bioreactor may also possess usefully at application in one or more reactions, components part process three-reforming, in whole certain the following equations:

SN4 + S02 -> 2SO + 2N2

SN4 + N20 >-WITH + ZN2

CH4 + U2O2 >-WITH + 2N2

SN4 + 202-> S02 + 2N20

Trapping carbon on industry is considerable pressure in with respect to reducing emission of carbon (including S02), and in the present time applied force to trapping carbon before ejection. Trying induce industry to limit emission of the carbon, in some jurisdictions defined economic stimulation on Your lu emissions of carbon and quotas on emission of greenhouse gases.

As a result of the present invention carbon entrapped from substrate, containing with and/or of h2 and/or S02 and/or SN4 , by means of fermentation process, and is valuable hydrocarbon product ("valuable" indicates a potentially useful for any-either target, and optionally possessing monetary value). In characteristic case of with, made process of reforming S02 , converted into S02 by burning or by water gas conversion. Process of reforming S02 and subsequent burning of also in characteristic case of leads as a result of to release S02 in atmosphere. Invention a method of catching carbon, which in otherwise vybrasyvalsya least in atmosphere, in the form of hydrocarbon product. If obtained energy is used for production of electricity, likely considerable loss of energy due to transmission lines of high voltage. Opposite, hydrocarbon product, made as a result of the present invention, can be easily transport and deliver in otherwise form of industrial, commercial, constant and transported final consumers, which leads to diffusion nnoi efficiency of energy and convenience. Production of hydrocarbon products, resulting from effectively exhaust gases, is attractive selling order industry. This especially true for industrial production, located remotely, if from logistics reasons of possible transport product on long distances. So, invention can provide diffusion nnoe trapping carbon, and also to modify the production of h2.

Common convergence shape of invention are described in one of. The fact of not less than, understandable, that specific stage or setting, mandatory in one form of realization, may not be are obligatory in other. Opposite, stage or setting, connected in description specific form of realization, can be optionally preferably used in forms realization, where they specially not are given.

At invention in a wide sense described with a reference to the any-either type of flow, which can move along system or around system (systems) by means of any known means of displacement, in some forms of realization riformirovannye and/or mixed streams of substrate are gaseous. Professionals in this engineering understandable, that specific plant may be connected suitable pipe means whether the similar, which may be are constructed for receiving or transmission flows through system. May be provided pump or compressor, to enable delivery of flows in specific installation. Besides, compressor can be used for diffusion condensate gas pressure, supplied in one or more plants, for example, into bioreactor. As discussed in this operation above, pressure of gases inside the bioreactor can mediate on efficiency performed in them reactions fermentation. So, pressure can be adjusted for diffusion condensate efficiency of fermentation. Suitable pressure for conventional reactions are known in this engineering.

Besides, system or methods can optionally include controlling means and/or control of other parameters of, to increase total efficiency of the method. For example, specific form of realization may include agent for determining, performing monitoring composition substrate and/or spent flow of (flows).

Additionally specific form of realization may include control means delivery of flow of (flows) substrate in specific mounting or elements within the separate system, if agent for determining is determined, that the composition of flow is suitable for a specific installation. For example, in cases of, where flow of gaseous substrate has low levels of with or high levels 02, may be hurtfully for fermentation reaction, flow of substrate can be carry off from bioreactor. In specific forms of invention system includes means for monitoring and control of the target condition of the flow substrate and/or speed, to flow, having desired or suitable composition, can be delivered into a specific installation.

Besides, may be necessary heated or cooled specific components system or flow of (and) substrate before or during location of in one or more plants in the process of. In such cases can be used known means of heating or cooling.

Different shapes of realization systems by the invention are described in accompanying graphic materials.

Alternative form of realization, described on figs. 1-3, include common with each other signs, and for designation of one and the same or neighboring signs in various graphical materials used similar position. Described are only new signs (relative to previous graphic materials), and, consequently, graphic materials should be considered in combination with the description of Figure 1.

On Figure 1 is system for production of hydrocarbon in accordance with one form of invention. System of Figure 1 includes:

module 10 reforming S02 , adapted to production with and/or of h2 in accordance with process of reforming S02 , in whole certain the following equation:

S02 + SN4 -> 2SO + 2N2 ;

module 6 by heating of adsorption (PSA), adapted to receive signal from gaseous substrate; membrane module (not shown), adapted to separation of one or more gases from one or more other gases, more preferably to separation of h2 and S02 from gaseous substrate, containing any one or more of the following gases: with, h2, S02 , N2 and SN4 ; module 12 enzymatic hydro lipolysis, adapted to receive signal biomass from the bioreactor and to production of product biomass, preferably methane.

Module 6 psa may be adapted to receive signal substrate from any one or more modules or from the bioreactor 4. Module 6 psa is adapted to separation of hydrogen from substrate. Substrate after fermentation from the bioreactor 4 may contain with and/or h2, and this substrate can be optionally subjected to recirculation in the bioreactor for production of hydrocarbon product.

Alternatively hydrocarbon, made a bioreactor, can be used as raw material for reforming process S02.

System may optionally include module preliminary reforming, adapted to receive signal of hydrocarbon, which can be checked a bioreactor. Device preliminary reforming is able to cleave more heavy hydrocarbons in process preliminary reforming to produce methane or other hydrocarbons, suitable for reforming process S02.

On Figure 2 is shown method and system for combining with system reforming S02 in accordance with one form of invention. With a reference to the Figure 2, substrate, containing with and/or h2, is passed in bioreactor 4.

This substrate, containing with and/or h2, subjected to fermentation in bioreactor to produce ethanol and/or 2.3-butanediol (2.3 BDO). Flow of gas, coming from bioreactor 4, is passed through membrane 8, where membrane 8 constructed so, to separating one or more gases from one or more other gases. In characteristic case of such gases, as SN4 and 1, are entrapped membrane 8 and is blown 14. Then residual gas flow, containing co and h2, is passed in module 6 psa, where at least part of the hydrogen is separated from gas flow.

Flow of gas, coming from module 6 psa, is passed in device 10 reforming S02 , where gas flow is converted into substrate, containing with, which can be then passed back into bioreactor 4. In some forms of invention implementation substrate, containing with and/or h2, factorable into bioreactor, is system of reforming S02.

Figure 3 represents is an example of one form of invention, where invention provides, that part SN4 , used for the reforming process S02 , obtained as a result of gasification of raw material refining. On Figure 3 is indicated system for production of hydrocarbon product, including module reforming S02 and bioreactor. Module reforming S02 includes module 16 of gasification, module 18 substitute of natural gas and device reforming S02. Module 16 of gasification is constructed so, to synthetic gas in a result of gasification of raw material refining, for example, coal or gas. Gasification may be made methods, known in this engineering. Module 16 gasification includes at least device of gasification. Module of gasification may also include additional symptoms, including device heat exchange and device gas cleaning. At least part of synthetic gas, produced module 16 of gasification, is passed in module 4 bioreactor. Additional part of synthetic gas, produced module 16 of gasification, is passed in the module 18 substitute of natural gas (ugs). Module 18 ugs comprises catalytic reactor substitute of natural gas, constructed so, to to transform synthetic gas, obtained from module 16 of gasification, in ugs, where ugs mainly includes methane (SN4). Then the stream ugs from module 18 ugs is passed in device 10 reforming S02 , where it is subjected to interaction with S02 to produce gaseous substrate, containing co and h2, in accordance with the following stoichiometry: S02 + SN4 -► 2SO + 2N2. Then substrate, containing co and h2, is passed in module 20 separation of gases. Module separation of gases may include any known means of separating gases.

Illustrative means separation of gases are means by heating of adsorption. As shown on Figure 3, at least part of hydrogen in flow of substrate separated from flow and isolated. Then residual gas flow, enriched with, is passed in bioreactor 4. In bioreactor 4, containing culture of one or more microorganisms, substrate, containing with and/or h2, subjected to fermentation to produce one or more hydrocarbon products. Hydrocarbon products in one form of realization represent ethanol and 2.3-butanediol. In some forms of realization residual gas, containing S02 and h2, coming from bioreactor 4, is passed directly in device 10 reforming S02. In some forms of realization residual gas, coming from bioreactor 4, is passed in the module 20 separation of gases, where h2 is separated and is isolated, and residual gas flow, enriched S02 , is passed in device 10 reforming S02.

In this description of invention described referring to a some preferred form of realization, to enable the reader to invention in practice without excessive experimentation. The fact of not less than, ordinary technician in this engineering easily understand, that numerous components and parameters can be to vary or modify to definite degree or replace the known equivalents without deviation from volume of invention. Understandable, that such modification and equivalents are connected in this operation as presented individually. Invention also involves all stages, signs, compositions and compounds, related to the present description or indicated in it, separately or all together, and also all and every combination of any two or more stages or signs.

If given above description there is link on integers, having their known equivalents, these integers are connected in the present description as presented separately.

Besides, headers, Captioning or similar are presented, to provide reader comprehension of this document, and their should not be it possible to consider limiting volume of this invention. Complete description of all requests on patents, patents and publications, cited above and below, if they is, are connected in the present description by references.

In the description reference to any-either preceding level of equipment is not confirmation or any-either form of assumptions, that preceding level of equipment is part of the general knowledge in the field of science in any this country of the world, and should not construed so.

During the whole of this description and any point below the following the formula of invention, if context does not require other, word "includes", "including" and the like should be interpreted due to no inclusive, opposite meaning excluding, i.e. due to no "including, but not limited by".