WO2012168668A1 - Procede de synthese de composes hydrocarbones bi-fonctionnels a partir de biomasse - Google Patents
Procede de synthese de composes hydrocarbones bi-fonctionnels a partir de biomasse Download PDFInfo
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- WO2012168668A1 WO2012168668A1 PCT/FR2012/051295 FR2012051295W WO2012168668A1 WO 2012168668 A1 WO2012168668 A1 WO 2012168668A1 FR 2012051295 W FR2012051295 W FR 2012051295W WO 2012168668 A1 WO2012168668 A1 WO 2012168668A1
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- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
- C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
- C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
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- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
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- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
- C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
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- C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
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- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
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- C12P7/52—Propionic acid; Butyric acids
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Definitions
- the subject of the present invention is a process for the synthesis of bi-functional hydrocarbon compounds from biomass comprising a step of fermentation of the biomass and a step of oxidation of the intermediate compounds resulting from the fermentation step.
- bi-functional hydrocarbon compounds such as unsaturated acids, unsaturated nitriles, acid anhydrides, acetals, aldehydes, epoxides including ethylene oxide and propylene oxide is carried out industrially chemically using raw materials from fossil hydrocarbons.
- bi-functional hydrocarbon compounds the compounds of 2 to 6 carbon atoms per molecule comprising two functions, and by function, the functions acid, nitrile, aldehyde, ether or olefinic unsaturation.
- These bi-functional compounds are, for example, diacids, acid anhydrides, unsaturated acids, unsaturated nitriles, unsaturated aldehydes, acetals, diols in epoxide (or oxirane) form, such as ethylene oxides, of propylene ... by intermediate compounds (fermentation), saturated acids, hydroxy acids, lactic acid, 3-hydroxypropionic acid, 3-hydroxybutyric acid, 2-hydroxyisobutyric acid,
- biomass the biodegradable fraction of products and waste as defined in European Directive 2003/30 / EC of 8 May 2003 and capable of being transformed by fermentation in the presence of microorganisms such as enzymes, bacteria, yeasts, mushrooms ...
- biomass By biomass will be understood sugars, starches, celluloses and hemicellulose and any plant material containing sugar, cellulose, hemicellulose and / or starch as well as synthesis gas.
- Vegetable materials containing sugars are mainly sugar cane and sugar beet; for example, maple, date palm, sugar palm, sorghum or American agave.
- Vegetable materials containing cellulose and / or hemicellulose are, for example, wood, straw, corn cobs, grain cake or fruit cake.
- Vegetable materials containing starches are mainly cereals and legumes, wheat, maize, sorghum, rye, wheat, rice, potato, cassava, sweet potato or seaweed.
- materials resulting from recovered materials mention may be made of vegetable or organic waste containing sugars and / or starches and / or celluloses and more generally any fermentable waste, including synthesis gas resulting from natural or industrial processes, and carbon monoxide.
- the synthesis gas that may be suitable for this type of fermentation may have a molar ratio H 2 / CO varying over a wide range, in particular from 0/1 to 4/1.
- microorganisms used in bioconversion are also well known. These microorganisms depend on the type of biomass to be treated and the fermentation method, aerobic or anaerobic retained.
- alcoholic fermentation with yeasts and bacteria of the genus Zymomonas or Zymosarcina; homolactic fermentation with bacteria of the genus Streptococcus or Lactobacillus, heterolactic fermentation with bacteria of the genus Leuconostoc or Lactobacillus, propionic fermentation with bacteria of the genus Clostridium, Propionibacterium or Corynebacterium, butyroacetonobutyl fermentation with bacteria of the genus Butyribacterium or Zymosarcina, mixed acid fermentation with bacteria of the genus Escherichia, Salmonella or Proteus, and glycolic butylene fermentation with bacteria of the genus Aerobacter or Aeromonas etc.
- the compound to be oxidized (alcohol, saturated acid or aldehyde, hydrocarbon, etc.) is generally brought into contact with air, often with air diluted with water. nitrogen, in an oxidation reactor.
- the implementation of this highly exothermic reaction is technologically delicate and requires the use of multitubular reactors or fluidized bed reactors.
- the solutions usually used to avoid the flammability range consist in diluting the reaction gases either with steam or with recycling gases that are depleted of oxygen (and therefore rich in nitrogen).
- the object of the invention is therefore to manufacture bi-functional hydrocarbon compounds of the unsaturated acid, unsaturated nitrile, acid anhydride, unsaturated aldehyde, acetal, epoxide type from biomass, thus avoiding the use of matter.
- first of fossil origin while allowing optimization of the operating conditions of the oxidation step.
- the invention consists in combining a first step where the formation of intermediate compounds such as olefins, saturated acids, hydroxy acids or alcohols, with the formation of a gas rich in C0, is carried out by fermentation of the biomass. 2 , with a second step of transformation with the aid of molecular oxygen in the gas phase of the intermediate compounds in the presence of C0 2 from the first step.
- the subject of the invention is a process for the synthesis of bi-functional hydrocarbon compounds comprising from 2 to 6 carbon atoms per molecule, the two functions being chosen from the functions of acid, aldehyde, nitrile, acetal and ⁇ -olefinic unsaturation from biomass consisting in a first step of subjecting the biomass to fermentation in the presence of a suitable microorganism and / or enzyme allowing the formation of intermediate compounds chosen from saturated acids, optionally carrying a hydroxyl function, alcohols and the olefins, in liquid or gaseous form, as well as CO 2 , then in a second step to be oxidized to catalytically transform the intermediate compounds in the catalytic phase with the aid of molecular oxygen in the presence of C0 2 resulting from the first stage.
- the CO 2 resulting from the fermentation stage can also come from a use of CO 2 as an inerting gas during anaerobic fermentations.
- the functions of the hydrocarbon compounds of the invention will be either two COO acid functional groups, in diacid form or in acid anhydride form, or two COC functions of ether type in the form of acetal, or two C-O hydroxyl functions or in the form of epoxides (oxides of ethylene or propylene ...), an acid function and an unsaturation-olefin, or an aldehyde function and an unsaturation-olefinic.
- an intermediate compound is synthesized by fermentation of the biomass in a known manner, which will be either i) an alcohol containing from 2 to 4 carbon atoms, for example ethanol, propanol, isopropanol, butanol or isobutanol, or ii) an ⁇ -olefin containing from 2 to 4 carbon atoms, for example ethylene, propylene, n-butene or isobutene, or iii) a saturated organic acid, bearing, if appropriate, Examples of such saturated organic acids are propionic acid, butyric acid, iso-butyric acid, lactic acid, lactic acid and the like.
- 3-hydroxypropionic acid, 2- or 3-hydroxyisobutyric acid and 3-hydroxybutyric acid or a salt of a saturated organic acid, optionally carrying a hydroxyl group, having 2 to 4 carbon atoms mention by way of example of such salts of saturated organic acids propionic acid salt, butyric acid salt, isobutyric acid salt, lactic acid salt, 3-hydroxypropionic acid salt, acid salt 2 or 3-hydroxyisobutyric acid and 3-hydroxybutyric acid salt.
- the cation of the saturated organic acid salt is monovalent and preferred selected from sodium, potassium and ammonium.
- Biomass refers to the biodegradable fraction of products, waste, etc. of plant or animal origin as well as synthesis gases. Subjected to fermentation, it will supply via the carbon it contains the energy necessary for the development of the microorganism used and its transformation into light organic compounds.
- the biomass according to the invention consists of sugars, starches, celluloses and any plant material containing sugar, cellulose, hemicellulose and / or starch as well as synthesis gases.
- the biomass will preferably contain carbohydrates, sugars with 5 or 6 carbon atoms (pentoses or hexoses), polyols (glycerol) or natural biodegradable polymers such as starch, cellulose or hemicellulose or polyhydroxyalkanoates (PHA). such as PHB (polyhydroxybutyrate) or PHVB (polyhydroxybutyratevalerate).
- micro-organism (s) used in the first step will depend on the nature of the biomass treated and the type of desired intermediate compound induced by the final objective compound.
- Fermentation can be anaerobic or aerobic. In the first case of anaerobic fermentation, this can be in some cases conducted in the presence of an inert gas such as for example C0 2 . In the second case, the fermentation is carried out in the presence of molecular oxygen, most often brought in the form of air. The gaseous mixture resulting from the fermentation whatever its form will then consist of nitrogen, oxygen, CO 2 and other hydrocarbon gases such as olefins or light organic compounds.
- an inert gas such as for example C0 2
- molecular oxygen most often brought in the form of air.
- the gaseous mixture resulting from the fermentation whatever its form will then consist of nitrogen, oxygen, CO 2 and other hydrocarbon gases such as olefins or light organic compounds.
- the intermediate compound is then subjected to an oxidation step using molecular oxygen.
- the oxygen is introduced into the oxidation reactor in the form of air, pure oxygen or intermediate air-oxygen mixtures such as enriched air.
- oxidation step is meant in the broad sense any reaction step involving oxygen as a reagent.
- the oxyhydrogenation is an oxidation in the sense of the invention as well as the oxidationhydration which is the combination of dehydration and oxidation.
- the oxidation step is carried out in the presence of C0 2 produced during or from the first fermentation step.
- the C0 2 present during the oxidation phase serves two functions that of "stabilizing agent", that is to say of inert gas avoiding being in the conditions of flammability of the reactive mixture and, that, thanks to its high specific heat, caloric transfer agent produced during the exothermic oxidation reaction the latter function is often called "thermal ballast".
- fermentation-oxidation coupling those which pass through the following routes may be mentioned as examples:
- Biomass -7 isopropanol -7 acrylic acid
- methacrylic The various acids mentioned above can be obtained in their nitrile form by carrying out the last oxidation step in the presence of ammonia.
- the gas phase oxidation step of the intermediate compounds is carried out according to the following reaction schemes depending on the intermediate compounds and end products sought.
- CH 2 CH-CH 3 + 0 2
- CH 2 CH-CHO + H 2 O
- the dehydration step of the alcohol is carried out on an acid catalyst, for example a gamma-alumina, at a temperature of 200 to 400 ° C, and preferably in the presence of steam.
- the oxidation step of the olefin is conducted in the vapor phase in the presence of air and steam at a temperature between 300 and 380 ° C under low pressure, 1 to 5 bar absolute, in the presence of oxide catalysts. mixed Mo, Co, Bi, Fe.
- the oxidation of the aldehyde is carried out under similar conditions, 250 ⁇ T ° C ⁇ 350, Kp ⁇ 5 bar in the presence of a catalyst based on Mo and V and optionally W, P, Cu plus, where appropriate, other elements.
- the oxidation is carried out in the gaseous phase at a temperature of between 300 and 600 ° C. under a low pressure of between 1 and 4 bars absolute in the presence of a catalyst based on vanadium and / or molybdenum oxides. Under certain (low) temperature conditions, the formation of o-phthalic acid or its anhydride (phthalic anhydride) on the side of the maleic compounds can be observed.
- a catalyst based on vanadium and / or molybdenum oxides Under certain (low) temperature conditions, the formation of o-phthalic acid or its anhydride (phthalic anhydride) on the side of the maleic compounds can be observed.
- the oxidation of alcohols can also be carried out in partial form by working, for example, according to the following reactions.
- the oxidationhydrogenation can be carried out according to the following overall reaction process:
- the synthesis of the aldehyde from the alcohol can thus be carried out either by oxy-dehydrogenation with a silver metal catalysis at a high temperature of between 500 and 700 ° C. and under equal or slightly higher pressure. at atmospheric pressure, between 1 and 5 bars, or by direct oxidation in the presence then mixed oxide type catalysts, preferably a molybdenum-vanadium or molybdenum-iron mixed oxide at a temperature between 200 and 400 ° C under a substantially atmospheric pressure of between 1 and 5 bar.
- mixed oxide type catalysts preferably a molybdenum-vanadium or molybdenum-iron mixed oxide at a temperature between 200 and 400 ° C under a substantially atmospheric pressure of between 1 and 5 bar.
- the direct synthesis of acetals preferably uses as catalyst a mixed oxide of molybdenum-vanadium or molybdenum-iron type as described in application WO2010 / 010287 in the name of the applicant.
- the operating conditions are preferably as follows: temperature between 200 and 300 ° C and pressure between 1 and 5 bar.
- a common point between the two applications WO 2007/034264 and WO 2008/007014 is the use of a light non-reactive hydrocarbon, especially methane, to improve the operating conditions and safety of the process.
- the compounds produced are olefins such as ethylene, propylene, n-butene and isobutene
- their oxidation is carried out under conditions that are well known since they are already used in industrial processes. using petroleum derivatives as a raw material.
- Propylene is vapor phase oxidized successively to acrolein and acrylic acid according to the following reaction process.
- the first step is carried out at a relatively low temperature, between 300 and 380 ° C under a low pressure between 1 and 5 bar in the presence of a catalyst consisting of a mixture of mixed oxides containing molybdenum and possibly other metals such as Bi, K, Co, Fe, Ni, Sn, Te, W ..).
- a diluent gas is also used, in general nitrogen and optionally water vapor.
- the second step is conducted at a slightly lower temperature, between 250 and 350 ° C under a pressure of 1 to 5 bar in the presence of a catalyst based on mixed oxides Mo-V generally doped.
- the two reactions are often carried out within the same reactor comprising two successive zones or in two consecutive reactors, under conditions similar to those described above for the oxidation of alcohols.
- CH 2 C (CH 3 ) -CHO + 1 ⁇ 2O 2
- CH 2 CCH 3 -COOH.
- the reactions are carried out at a relatively low temperature, between 300 and 400 ° C. under a low pressure of between 1 and 5 bar in the presence of a catalyst composed of a mixture of mixed oxides (Mo, Bi, K, Co, Fe ...) for the first step and a catalyst based on mixed oxides Mo-V for the second.
- a catalyst composed of a mixture of mixed oxides (Mo, Bi, K, Co, Fe ...) for the first step and a catalyst based on mixed oxides Mo-V for the second.
- a diluent gas generally water vapor, is also used.
- Ethylene and propylene can be converted to ethylene oxide or propylene oxide depending on the reactions.
- the reactions are carried out at "low" temperature, generally between 260 and 290 ° C., by means of a silver catalyst deposited on a low porous support such as alumina, silicoaluminum or silicon carbide. From an industrial standpoint, obtaining ethylene oxide by this route gives excellent performance, whereas obtaining propylene oxide requires, in order to obtain acceptable yields, catalysts with silver or gold more sophisticated.
- the propionic acid is oxidized to acrylic acid by oxidationhydrogenation according to the reaction:
- Lactic acid is converted to acrylic acid by dehydration in the presence of oxygen according to the reaction (oxygen being used to limit coke formation):
- the C4, iso-butyric, 2-hydroxyisobutyric and 3-hydroxyisobutyric acids lead to methacrylic acid by reaction mechanisms, oxidized hydrogenation and dehydration, analogous to those of C3 acids according to the reactions.
- the oxy-dehydrogenation is carried out in the vapor phase at a temperature of about 400-450 ° C with mixed oxide catalysts containing Mo and optionally P, V or Fe.
- the dehydration is carried out at a temperature generally between 220 and 400 ° C, preferably between 250 and 350 ° C and at a pressure between 0.5 and 5 bar.
- the catalysts are acidic (Hammett's Acidity ⁇ +2); they will be chosen from siliceous materials, acidic zeolites or mixed oxides such as those based on iron and phosphorus or those based on cesium, phosphorus and tungsten.
- the oxidation reaction in the gas phase is carried out on the effluent from the first step.
- This under normal conditions of pressure and temperature, is in gaseous form in the case where the intermediate compound is an olefin, or in liquid form in aqueous solution when the intermediate compound is an alcohol or a saturated acid.
- the liquid fraction is accompanied by a gaseous fraction including in particular C0 2 resulting from the degradation of carbohydrates subjected to fermentation.
- C0 2 is often used as a material for the gasification of beverages.
- the gaseous fraction containing the intermediate compound as well as the CO 2 and other molecules resulting from the fermentation is sent to the oxidation step.
- H 2 can be produced which will then have to be removed, for example by combustion, membrane separation or any other known technique.
- the C0 2 produced can be present in a mixture with residual oxygen and nitrogen. The mixture can be used directly for the oxidation reaction or can be purified to generate a carbon dioxide enriched stream that will be used for the oxidation reaction.
- the oxidation step is carried out by means of molecular oxygen, in the form of air, air enriched in O 2 or pure oxygen.
- molecular oxygen in the form of air, air enriched in O 2 or pure oxygen.
- the choice of the form of the oxidant depends in particular on the end products to be synthesized (of the reaction to be carried out), the synthesis of maleic anhydride from n-butene requiring, for example, much more oxygen than that of the oxides of ethylene or propylene.
- the gaseous oxidation reaction medium will comprise the intermediate compound (Intermediate) to be oxidized, oxygen (oxygen) and "inert” gases, in particular C0 2 .
- Inert gases Inert gases are understood to mean all compounds that do not enter the chemical reaction. Regardless of C0 2 , we can find nitrogen, argon (if air is used), water vapor ...
- the content of these different constituents will be such that the ratio Oxygen / Intermediate will be between 1/12 and 6/1, preferably between 1/6 and 4/1, the Intermediate / Medium ratio of between 1 and 40% and preferably between 3 and 20%, the Inert content of the medium between 40 and 90% and preferably between 60 and 80%, the CO 2 / Inert ratio of between 50 and 90% and the content of the nitrogen inert of between 1 and 50% and in stabilized operation (after starting of the installations) preferably between 1 to 20%.
- the intermediate compound is in liquid form
- the C0 2 from the first step is captured for use in the oxidation step. It can be used to stripper this intermediate compound before sending it into the oxidation reactor. It can also be sent to the oxidation reactor independently of the liquid intermediate compound which will be extracted from the middle of the first stage by any suitable means.
- the gas stream rich in C0 2 is optionally purified (by any technique known to those skilled in the art) before being sent into the oxidation reactor in order to eliminate the compounds that may possibly be harmful to the latter (hydrogen, sulfur compounds, ).
- the oxidation is carried out with "pure" oxygen in order to limit the amount of nitrogen, an inert gas that is not very effective in extracting the calories produced during the reaction.
- pure oxygen
- an inert gas that is not very effective in extracting the calories produced during the reaction.
- gas phase oxidation reactions generally utilize multitubular reactor or fluidized bed reactor technologies.
- the selected reactor technology uses multitubular reactors, the temperature within the reactor is not uniform. There are hot spots, related to the difficulties of evacuation of the heat of reaction within the reactor.
- fluidized bed reactors the temperature is more homogeneous than in the previous case because the catalyst carries part of the heat throughout the reactor.
- the gas carries a significant portion of the heat of reaction.
- a coolant is circulated between the tubes, often molten salts such as mixtures of NaN0 2 , NaN0 3 and KNO 3 , which transfers a large part of the heat reaction to a boiler that produces steam under pressure.
- cooling pins may be inserted into the catalyst bed to extract a portion of the heat of reaction.
- the use of inert gases of high heat capacity in place of nitrogen makes it possible to better manage the extraction of calories and thus to better control the temperature in the reactor.
- the use of the carbon dioxide produced during the first step has the advantage of improving the overall performance of the unit while avoiding the release of this highly harmful gas.
- the process of the invention makes it possible in particular to produce "bio-resourced” products, that is to say synthesized products from non-fossil natural products whose origin, plant or animal, was the opportunity to set the C0 2 conferring on the whole a particularly satisfactory balance sheet.
- synthesized product (acid, anhydride, nitrile, acetal, oxide) "bio-resourced” means a compound having a carbon content 14 C characteristic of the natural non-fossil origin of the raw materials used.
- carbonaceous raw materials of natural and renewable origin can be detected thanks to the carbon atoms used in the composition of the final product.
- materials made from renewable raw materials contain 14 C. All carbon samples taken from living organisms (animals or plants) are in fact a mixture of 3 isotopes: 12 C (representing ⁇ 98, 892%), 13 C ( ⁇ 1.108%) and 14 C (traces: 1, 2.10 "10
- the 14 C / 12 C ratio of living tissues is identical to that of the atmosphere.
- 14 C exists in two predominant forms: in mineral form that is to say carbon dioxide (C0 2 ) and in organic form ie carbon integrated in organic molecules.
- the 14 C / 12 C ratio is kept constant by the metabolism because the carbon is continuously exchanged with the environment.
- the proportion of 14 C being substantially constant in the atmosphere, it is the same in the body, as long as it is alive, since it absorbs 14 C as it absorbs 12 C.
- the average ratio of 14 C / 12 C is equal to 1, 2 ⁇ 10 -12 .
- 12 C is stable, that is to say that the number of atoms of 12 C in a given sample is constant over time.
- 14 C is radioactive and every gram of living carbon contains enough 14 C isotope to give 13.6 disintegrations per minute.
- the half-life (or period) ⁇ / 2 related to the decay constant of 14 C is 5730 years. Given this time, it is considered that the 14 C content is practically constant from the extraction of the vegetable raw materials to the production of the final product.
- the sample is reduced to graphite or C0 2 gas, analyzed in a mass spectrometer.
- This technique uses an accelerator and a mass spectrometer to separate 14 C ions and 12 C and thus determine the ratio of the two isotopes.
- the invention relates to a process of "bio-resourced" products having a mass content of 14 C such that the ratio 14 C / 12 C is between 0.2.10 ⁇ 12 and 1.2.10 ⁇ 12 .
- the ratio 14 C / 12 C is between 0.6.10 ⁇ 12 and 1.2.10 ⁇ 12 and more preferably between 0.9.10 ⁇ 12 and 1.2.10 ⁇ 12 .
- the 14 C / 12 C ratio will depend on the production methods used, the raw materials used, all or part of non-fossil natural origin, or as a function of mixtures made later. This ratio can not exceed 1.2.10 ⁇ 12 ; if this were the case, it would imply that the operator artificially introduced the 14 C atoms into the product compound.
- the medium After neutralization of the acid, the medium is brought to a pH of about 5 which is required by the enzymatic hydrolysis.
- a cellulase solution is prepared in the presence of nutrients in serial fermentors, the culture of the microorganism Trichoderma reesi being carried out in the first fermenters from straw previously ground, and the cellulose being produced in the following fermentors. From the contents of the last ferraenter, the desired enzymatic solution is separated by centrifugation and filtration.
- Enzymatic hydrolysis of straw pretreated above by enzymatic solution above is carried out in series-connected reactors.
- Aceto-butyl fermentation of the C 6 and C 5 sugar solutions above is then carried out using the microorganism Clostridium acetobutylicum under aseptic conditions.
- the fermentation comprises two successive phases, the first leading to the production of acetic and butyric acids and the second to the production of acetone, butanol and ethanol in the following proportions by weight: butanol 68%; acetone 29%; and ethanol 3%.
- the acetone is separated by azeotropic distillation.
- the CO 2 produced during the fermentation is recovered and isolated from other gases (in particular hydrogen) by absorption in potash.
- the C0 2 is thus produced for the reaction
- the isopropanol is injected to dehydrate in a tubular reactor having a diameter of 127 mm under vacuum (pressure of about 0.8 bar) at a temperature at 345 ° C containing a bed catalytic converter consisting of a layer of ESM110 ® alumina from EUROSUPPORT, the hourly volume velocity (ratio of the volume flow rate of acetone to the volume of catalyst) being 1 hr -1 .
- the mixture of water and propylene produced in the reactor is cooled in a heat exchanger, before being sent to a gas-liquid separator where propylene and water are separated.
- a propylene purification step is carried out before carrying out the second oxidation step, by condensing traces of residual organic compounds (acetone, isopropanol, ether, etc.) in propylene.
- Example 2 Oxidation of Propylene in the Presence of C0 2
- a tubular reactor with an internal diameter of 25.4 mm and a length of 3 m was filled with Nippon Shokubai commercial catalysts ACF7, connected in series with another tubular reactor of the same diameter and length 2.4 m and filled with catalysts.
- ACS7 commercials from Nippon Shokubai.
- the tubes are equipped with a multipoint thermocouple in their center for direct reading of a temperature profile.
- the reactors are of molten salt bath type, the agitation of the salt being ensured by a bubbling of nitrogen in the molten salt.
- the first reactor was charged with 315 g of ACF7L catalyst at the top (ie 438 ml) and 773 g of ACF7S at the bottom (ie 1023 ml), representing respectively 0.9 m and 2.1 m of length of tube.
- the second reactor was charged with 508 g of overhead ACS7L catalyst (ie 438 ml) and 935 g of ACS7S at the bottom (ie 731 ml), representing respectively 0.9 m and 1.5 m of tube length.
- the composition of the gas supplying the first reactor is a mixture 0 2 / propylene / N 2 / CO 2 (use of air diluted with nitrogen) and by varying the CO 2 content from 0 to 66%, substituting nitrogen by C0 2 .
- the CO 2 content in the gas is gradually increased, with 8-hour increments for each C0 2 concentration level, to the highest concentration (66%) where a 20 hr balance sheets. These show a reproducibility of the results over this period.
- VVH conditions 1560 h -1 VVH 1560 h -1 feed 6.9% propylene 9.0% propylene,
- VVH supply conditions 1560 hr 1 VVH 1560 hr 1
- the gain provided by the use of C0 2 in this reaction can be utilized to obtain a gain in selectivity.
- Crude fermented isobutanol obtained from fermentation and containing 50% by weight of water and 4% by weight of ethanol is sent to a dehydration reactor containing a silica alumina Siralox 40/450, maintained at 300 ° C.
- the products of the reaction are separated in a liquid gas separator to condense the water produced at 0 ° C. as well as the unreacted isobutanol.
- the gaseous mixture is then sent to an oxidation reactor 15 mm in diameter and 50 cm in length.
- the CO2-rich gas produced during the fermentation is used to dilute the reaction gases.
- the ideal catalyst for this example the ACF7S catalyst described in Example 2 is used.
- Ammonium lactate is prepared by anaerobic fermentation of dextrose by controlling the fermentation atmosphere by feeding the fermentation reactor with CO 2 generated during an alcoholic fermentation (ethanol production).
- the pH of the medium is controlled during fermentation by continuously adding ammonia to the medium to maintain a neutral pH.
- the ammonium lactate is recovered by filtration (to separate it from the microorganism).
- the medium is then concentrated to a content of 30% by weight.
- the aqueous solution of ammonium lactate will be used in a dehydration reactor.
- the gas leaving the fermentation reactor is a gas rich in CO 2 , but containing some impurities, including ammonia, water vapor, and nitrogen. This gas will constitute the fluidization gas during the dehydration of ammonium lactate.
- a fluidized bed pilot reactor is used to dehydrate ammonium lactate.
- the dimensions of the reactor are 5 cm in diameter and 75 cm in height.
- the gas is introduced through the bottom of the reactor to ensure fluidization of 300 g of catalyst.
- the selected catalyst is hydroxyapatite (hydrated calcium phosphate) having a P / Ca molar ratio of 1.6.
- the reaction temperature is 320 ° C.
- the aqueous solution of ammonium lactate is fed through a fogger just above the distribution grid at the bottom of the reactor.
- the molar composition of the reaction mixture is adjusted to have 4 mol% of ammonium lactate, 1 mol% of oxygen and the remainder of CO2-rich gas from the fermentation.
- the yield of acrylic acid obtained is 37%.
- SASOL Alumina Gamma Catalyst of the PURALOX SCCa 150/200 type, having a silica content of 0.03% by weight and an iron oxide content of 0.02% by weight, with a specific surface area of 200 m 2 / g, is used.
- This alumina is in the form of a powder with an average particle size of 150 microns and can be used directly.
- a tubular reactor of 10 mm inner diameter is charged with 10 grams of catalyst.
- the reactor is fed with an isobutanol / water mixture (from a fermentation process) of ratio 95/5 with a flow rate of 1.2 g of isobutanol per minute.
- the WH Total is 2650 h -1 for this reaction carried out in the gas phase.
- the reactor is maintained at 325 ° C.
- the product gas is combined with the C0 2 rich gases resulting from the fermentation, and an isobutene oxidation reactor is fed as in Example 4.
- the composition of the gaseous mixture is 4% isobutene, 6% oxygen, and 40% CO 2 .
- the yield of methacrolein is 40
- Example 7 Oxidation of fermentation isobutanol in the presence of fermentation CO 2 with another catalyst.
- MFM3-MS supplied by MAPCO having a Mo / Fe atomic ratio of 2.5, mixed with 300 mg of silicon carbide and loaded into the reactor.
- the catalyst is first activated under a stream of Helium / Oxygen (48 Nml / min - 12 Nml / min) at 300 ° C for 15 hours and 30 minutes. Then, the temperature is reduced to 250 ° C and data acquisition begins. After stabilization, the performances of the catalyst are recorded. Then the temperature of the catalyst is increased by trays and at each level (260, 280 and 300 ° C) data are taken.
- Helium / Oxygen 48 Nml / min - 12 Nml / min
- the flow rates of oxygen and helium are respectively 6.7 and 26.4 Nml / min and the isobutanol concentration is adjusted to 5%. (conditions: isobutanol / O 2 / Helium / CO 2 fermentation: 5/13/82/0) for a WH of 10,000 ml. h "1. g " 1 .
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US14/125,529 US10030255B2 (en) | 2011-06-10 | 2012-06-08 | Process for synthesizing bifunctional hydrocarbon-based compounds from biomass |
CN201280039086.8A CN103732754A (zh) | 2011-06-10 | 2012-06-08 | 用于从生物质合成基于双官能烃的化合物的方法 |
BR112013031807A BR112013031807A2 (pt) | 2011-06-10 | 2012-06-08 | processo para sintetizar compostos bifuncionais baseados em hidrocarbonetos a partir de biomassa |
EP12731552.1A EP2718452A1 (fr) | 2011-06-10 | 2012-06-08 | Procede de synthese de composes hydrocarbones bi-fonctionnels a partir de biomasse |
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FR1155110A FR2976293B1 (fr) | 2011-06-10 | 2011-06-10 | Procede de synthese de composes hydrocarbones bi-fonctionnels a partir de biomasse |
FR11.55110 | 2011-06-10 |
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EP (1) | EP2718452A1 (fr) |
CN (1) | CN103732754A (fr) |
BR (1) | BR112013031807A2 (fr) |
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WO (1) | WO2012168668A1 (fr) |
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US20050222458A1 (en) * | 2004-04-02 | 2005-10-06 | Liliana Craciun | Preparation of acrylic acid derivatives from alpha-or beta-hydroxy carboxylic acids |
WO2007034264A1 (fr) | 2005-09-20 | 2007-03-29 | Arkema France | Procédé de synthèse de produits d'oxydation partielle d'alcools courts par oxydation directe d'un alcool court et catalyseurs pouvant être employés dans ce procédé |
WO2007128941A2 (fr) | 2006-05-09 | 2007-11-15 | Arkema France | Procede de fabrication de produits d'oxydation partielle d'alcools inferieurs par oxydation directe d'un alcool inferieur |
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WO2008007014A1 (fr) | 2006-07-13 | 2008-01-17 | Arkema France | Procede de synthese d'aldehyde leger par oxydation catalytique de l'alcool correspondant en presence de methane |
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GB809452A (en) * | 1954-09-10 | 1959-02-25 | Celanese Corp | Oxidation of fatty acids |
SE526429C2 (sv) * | 2003-10-24 | 2005-09-13 | Swedish Biofuels Ab | Metod för att framställa syreinnehållande föreningar utgående från biomassa |
BRPI1008287A2 (pt) * | 2009-02-24 | 2016-03-15 | Gevo Inc | métodos de preparação de butadieno e isopreno renováveis |
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2011
- 2011-06-10 FR FR1155110A patent/FR2976293B1/fr active Active
-
2012
- 2012-06-08 WO PCT/FR2012/051295 patent/WO2012168668A1/fr active Application Filing
- 2012-06-08 EP EP12731552.1A patent/EP2718452A1/fr active Pending
- 2012-06-08 CN CN201280039086.8A patent/CN103732754A/zh active Pending
- 2012-06-08 US US14/125,529 patent/US10030255B2/en active Active
- 2012-06-08 BR BR112013031807A patent/BR112013031807A2/pt not_active Application Discontinuation
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EP2718452A1 (fr) | 2014-04-16 |
CN103732754A (zh) | 2014-04-16 |
US20140356918A1 (en) | 2014-12-04 |
FR2976293B1 (fr) | 2015-01-02 |
FR2976293A1 (fr) | 2012-12-14 |
US10030255B2 (en) | 2018-07-24 |
BR112013031807A2 (pt) | 2017-01-31 |
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