EP4222232A1 - Production of aromatics and ethanol by pyrolysis, reverse water-gas shift reaction, and fermentation - Google Patents
Production of aromatics and ethanol by pyrolysis, reverse water-gas shift reaction, and fermentationInfo
- Publication number
- EP4222232A1 EP4222232A1 EP21773411.0A EP21773411A EP4222232A1 EP 4222232 A1 EP4222232 A1 EP 4222232A1 EP 21773411 A EP21773411 A EP 21773411A EP 4222232 A1 EP4222232 A1 EP 4222232A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- pyrolysis
- unit
- gas
- cut
- rwgs
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 146
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 106
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 87
- 238000000855 fermentation Methods 0.000 title claims abstract description 84
- 230000004151 fermentation Effects 0.000 title claims abstract description 84
- 230000002441 reversible effect Effects 0.000 title abstract description 6
- 238000004519 manufacturing process Methods 0.000 title description 30
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 72
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 58
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 57
- 239000008096 xylene Substances 0.000 claims abstract description 54
- 238000000034 method Methods 0.000 claims abstract description 43
- 238000006317 isomerization reaction Methods 0.000 claims abstract description 42
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims abstract description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 229910001868 water Inorganic materials 0.000 claims abstract description 38
- 238000000926 separation method Methods 0.000 claims abstract description 31
- 150000001491 aromatic compounds Chemical class 0.000 claims abstract description 30
- 238000005194 fractionation Methods 0.000 claims abstract description 20
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 139
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 125
- 239000007789 gas Substances 0.000 claims description 88
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 claims description 71
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims description 63
- 239000003054 catalyst Substances 0.000 claims description 51
- 125000004432 carbon atom Chemical group C* 0.000 claims description 44
- 230000008569 process Effects 0.000 claims description 33
- 150000003738 xylenes Chemical class 0.000 claims description 31
- 244000005700 microbiome Species 0.000 claims description 30
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 28
- 229910021536 Zeolite Inorganic materials 0.000 claims description 27
- 239000010457 zeolite Substances 0.000 claims description 27
- 238000010555 transalkylation reaction Methods 0.000 claims description 22
- 238000007327 hydrogenolysis reaction Methods 0.000 claims description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims description 17
- 239000001257 hydrogen Substances 0.000 claims description 17
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 claims description 16
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 13
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 11
- 239000005977 Ethylene Substances 0.000 claims description 11
- 229910052751 metal Inorganic materials 0.000 claims description 11
- 239000002184 metal Substances 0.000 claims description 11
- 230000018044 dehydration Effects 0.000 claims description 10
- 238000006297 dehydration reaction Methods 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 9
- 125000004430 oxygen atom Chemical group O* 0.000 claims description 8
- 238000007323 disproportionation reaction Methods 0.000 claims description 6
- 229910052742 iron Inorganic materials 0.000 claims description 6
- 230000012010 growth Effects 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 229910052783 alkali metal Inorganic materials 0.000 claims description 3
- 150000001340 alkali metals Chemical class 0.000 claims description 3
- 229910001657 ferrierite group Inorganic materials 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 78
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 130
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 75
- 239000001569 carbon dioxide Substances 0.000 description 65
- 229910002092 carbon dioxide Inorganic materials 0.000 description 65
- 125000003118 aryl group Chemical group 0.000 description 40
- 239000000203 mixture Substances 0.000 description 31
- 150000001875 compounds Chemical class 0.000 description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 17
- 229910052799 carbon Inorganic materials 0.000 description 17
- 239000007788 liquid Substances 0.000 description 15
- 239000000047 product Substances 0.000 description 15
- 239000006227 byproduct Substances 0.000 description 13
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 11
- 150000001298 alcohols Chemical class 0.000 description 11
- 239000002609 medium Substances 0.000 description 11
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 11
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 10
- 239000002029 lignocellulosic biomass Substances 0.000 description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 9
- 241000894007 species Species 0.000 description 9
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 8
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 8
- 230000000789 acetogenic effect Effects 0.000 description 8
- 230000003197 catalytic effect Effects 0.000 description 8
- 235000015097 nutrients Nutrition 0.000 description 8
- 241000193403 Clostridium Species 0.000 description 7
- 239000002253 acid Substances 0.000 description 7
- 238000005804 alkylation reaction Methods 0.000 description 7
- 238000004821 distillation Methods 0.000 description 7
- 239000012530 fluid Substances 0.000 description 7
- 150000002431 hydrogen Chemical class 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Natural products CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 6
- 241001656809 Clostridium autoethanogenum Species 0.000 description 6
- 238000000605 extraction Methods 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 230000006641 stabilisation Effects 0.000 description 6
- 238000011105 stabilization Methods 0.000 description 6
- 241000186566 Clostridium ljungdahlii Species 0.000 description 5
- 150000007513 acids Chemical class 0.000 description 5
- 230000008901 benefit Effects 0.000 description 5
- 210000004027 cell Anatomy 0.000 description 5
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 5
- 229910052759 nickel Inorganic materials 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 4
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000001833 catalytic reforming Methods 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- ZSIAUFGUXNUGDI-UHFFFAOYSA-N hexan-1-ol Chemical compound CCCCCCO ZSIAUFGUXNUGDI-UHFFFAOYSA-N 0.000 description 4
- 239000000543 intermediate Substances 0.000 description 4
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 4
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 4
- 150000002739 metals Chemical class 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 239000011591 potassium Substances 0.000 description 4
- 229910052700 potassium Inorganic materials 0.000 description 4
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 4
- LWIHDJKSTIGBAC-UHFFFAOYSA-K tripotassium phosphate Chemical compound [K+].[K+].[K+].[O-]P([O-])([O-])=O LWIHDJKSTIGBAC-UHFFFAOYSA-K 0.000 description 4
- 238000010977 unit operation Methods 0.000 description 4
- 241001464894 Blautia producta Species 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- OWBTYPJTUOEWEK-UHFFFAOYSA-N butane-2,3-diol Chemical compound CC(O)C(C)O OWBTYPJTUOEWEK-UHFFFAOYSA-N 0.000 description 3
- 150000001735 carboxylic acids Chemical class 0.000 description 3
- 238000007233 catalytic pyrolysis Methods 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 229910052593 corundum Inorganic materials 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- FUZZWVXGSFPDMH-UHFFFAOYSA-N n-hexanoic acid Natural products CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 150000005201 tetramethylbenzenes Chemical class 0.000 description 3
- JZRWCGZRTZMZEH-UHFFFAOYSA-N thiamine Chemical compound CC1=C(CCO)SC=[N+]1CC1=CN=C(C)N=C1N JZRWCGZRTZMZEH-UHFFFAOYSA-N 0.000 description 3
- 150000005199 trimethylbenzenes Chemical class 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- 229910001845 yogo sapphire Inorganic materials 0.000 description 3
- YGHRJJRRZDOVPD-UHFFFAOYSA-N 3-methylbutanal Chemical compound CC(C)CC=O YGHRJJRRZDOVPD-UHFFFAOYSA-N 0.000 description 2
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 2
- 241001534860 Alkalibaculum bacchi Species 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- 239000004254 Ammonium phosphate Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- FERIUCNNQQJTOY-UHFFFAOYSA-M Butyrate Chemical compound CCCC([O-])=O FERIUCNNQQJTOY-UHFFFAOYSA-M 0.000 description 2
- 241001058118 Caldanaerobacter Species 0.000 description 2
- WWZKQHOCKIZLMA-UHFFFAOYSA-N Caprylic acid Natural products CCCCCCCC(O)=O WWZKQHOCKIZLMA-UHFFFAOYSA-N 0.000 description 2
- 241001656810 Clostridium aceticum Species 0.000 description 2
- 241000193401 Clostridium acetobutylicum Species 0.000 description 2
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- 241000328950 Clostridium drakei Species 0.000 description 2
- 241000186587 Clostridium scatologenes Species 0.000 description 2
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
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- UUIQMZJEGPQKFD-UHFFFAOYSA-N Methyl butyrate Chemical compound CCCC(=O)OC UUIQMZJEGPQKFD-UHFFFAOYSA-N 0.000 description 2
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- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
- C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
- C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/245—Stationary reactors without moving elements inside placed in series
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
- B01J6/008—Pyrolysis reactions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2729—Changing the branching point of an open chain or the point of substitution on a ring
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2729—Changing the branching point of an open chain or the point of substitution on a ring
- C07C5/2732—Catalytic processes
- C07C5/2737—Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/09—Purification; Separation; Use of additives by fractional condensation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/026—Increasing the carbon monoxide content, e.g. reverse water-gas shift [RWGS]
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
- C12P7/065—Ethanol, i.e. non-beverage with microorganisms other than yeasts
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
- C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1014—Biomass of vegetal origin
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the invention relates to the production of aromatics (benzene, toluene, xylenes, Le., BTX) and ethanol for petrochemicals. More particularly, the object of the invention is to be able to produce aromatics and ethanol by a process of pyrolysis of hydrocarbon compounds, and preferably of biomass, by conversion of CO and CO2 by-products of pyrolysis, all of the carbon and in particular bio-based carbon can thus be recovered.
- An aromatic complex (or device for converting aromatic compounds) is a device powered by charges mainly composed of six to ten or more carbon atoms, denoted C6 to C10+ charges.
- C6 to C10+ charges Different sources of aromatic compounds can be introduced into an aromatic complex, the most common being from a catalytic naphtha reforming process.
- aromatic alkyls e.g. toluene, paraxylene, orthoxylene
- aromatic alkyls e.g. toluene, paraxylene, orthoxylene
- the products of interest are aromatics with 0 (benzene), 1 (toluene) or 2 (xylenes) methyl groups, and in particular, within xylenes, paraxylene, having the highest market value.
- Hydrocarbon compound pyrolysis processes produce aromatic compounds but also a lot of CO and CO2 as conversion by-products.
- the pyrolysis is catalytic, the combustion of the coke present on the catalyst used in the pyrolysis reactor also produces a significant quantity of CO2.
- An aromatic complex generally has at least one catalytic unit having at least one of the following functions:
- A8 compounds the isomerization of aromatic compounds with 8 carbon atoms, denoted A8 compounds, making it possible to convert orthoxylene, metaxylene and ethylbenzene into paraxylene; - transalkylation to produce xylenes from a mixture of toluene (and optionally benzene) and A9+ compounds such as trimethylbenzenes and tetramethylbenzenes; and
- the aromatic loop makes it possible to produce high purity paraxylene by separation by adsorption or by crystallization, an operation well known in the prior art.
- This “C8-aromatic loop” includes a step for removing heavy compounds (i.e., C9+) in a distillation column called the “xylene column”.
- the overhead from this column which contains the C8-aromatic isomers (i.e., A8), is then sent to the paraxylene separation process which is very generally a simulated moving bed adsorption (LMS) separation process to producing an extract and a raffinate, or a crystallization process in which a fraction of paraxylene is isolated from the rest of the constituents of the mixture in the form of crystals.
- LMS simulated moving bed adsorption
- the extract which contains paraxylene, is then distilled to obtain high purity paraxylene.
- the raffinate rich in metaxylene, orthoxylene and ethylbenzene, is treated in a catalytic isomerization unit which gives a mixture of C8 aromatics, in which the proportion of xylenes (ortho-, meta-, para-xylenes) is practically at thermodynamic equilibrium and the amount of ethylbenzene is reduced. This mixture is again sent to the “xylene column” with the fresh feed.
- Aromatic complexes producing benzene and paraxylene are mostly fed by feedstocks from petroleum or natural gas. These complexes do not make it possible to produce biobased aromatics, nor to co-produce ethanol. Another challenge is to recover carbon in the form of CO and CO2, and in particular bio-sourced carbon, into compounds with high added value.
- the object of the present invention is to overcome these drawbacks.
- a first object of the present description is to overcome the problems of the prior art and to provide a device and a process for the production of aromatics for the petrochemical industry allowing, when the aromatic compounds are produced by pyrolysis of hydrocarbon compounds, to convert (for example all) CO and CO2, by-products of the pyrolysis section, into ethanol.
- the CO2 resulting from the combustion of the coke present on the catalyst of the pyrolysis process can also be advantageously converted into ethanol.
- all of the carbon present in the charge to be pyrolyzed is upgraded to aromatic compounds and ethanol.
- the invention is based on the arrangement of one or more units making it possible to convert the CO and CO2 by-products of the pyrolysis of hydrocarbon compounds into ethanol.
- the object of the present invention can be summarized as adding a reverse water gas conversion unit (or RWGS or "Reverse Water Gas Shift" according to the English terminology) to at least partially convert the CO2 into CO and thus obtain a CO-enriched gas, followed by a CO to ethanol fermentation unit.
- the CO2 present at the outlet of the fermentation unit is recycled at the inlet of the Reverse Water Gas Shift unit, thus allowing the total conversion of CO2.
- a device for converting a first hydrocarbon feed comprising aromatic compounds comprising:
- fractionation train adapted to extract at least one cut comprising benzene, one cut comprising toluene and one cut comprising xylenes and ethylbenzene from the first hydrocarbon feedstock;
- a xylene separation unit suitable for processing the cut comprising xylenes and ethylbenzene and producing an extract comprising paraxylene and a raffinate comprising orthoxylene, metaxylene and ethylbenzene;
- an isomerization unit adapted to treat the raffinate and produce an isomerate enriched in paraxylene sent to the fractionation train;
- a pyrolysis unit suitable for treating a second hydrocarbon charge, producing at least one pyrolysis effluent comprising hydrocarbon compounds with 6 to 10 carbon atoms supplying at least partially the first hydrocarbon charge, and producing a pyrolysis gas comprising at least CO, CO2 and H2;
- an RWGS reaction section adapted to treat the pyrolysis gas and produce an RWGS gas enriched in CO and water;
- One of the advantages of the invention is in particular to be able to send, without a separation step, the effluent from the RWGS (for example in full) containing a mixture consisting of CO, CO2, H2O and H2 directly into the fermentation reaction section to produce ethanol.
- the ethanol thus produced can be upgraded in various forms, such as for example in the form of ethylene (eg after dehydration of the ethanol).
- benzene such as benzene from the aromatic complex is converted into ethylbenzene by reaction with ethylene.
- the ethylbenzene obtained can advantageously be sent to the isomerization unit to form additional xylenes.
- ethylene is oligomerized into longer olefins (butenes, hexenes, octenes). It is thus possible to obtain the monomers useful for obtaining biobased polymers.
- the fermentation reaction section is suitable for recycling CO2 present at the fermentation outlet to the inlet of the RWGS reaction section.
- the device further comprises a make-up line to provide an H2 supply in the pyrolysis gas.
- the fractionation train is suitable for extracting a cut of C9-C10 mono-aromatics from the first hydrocarbon charge.
- the device further comprises a transalkylation unit suitable for treating the C9-C10 mono-aromatic cut with the cut comprising toluene and producing xylenes sent to the fractionation train.
- the device further comprises a selective hydrogenolysis unit is suitable for:
- the device further comprises a disproportionation unit suitable for treating at least part of the cut comprising toluene and producing a cut enriched in xylenes recycled to the isomerization unit.
- the method comprises a step of recycling CO2 present at the fermentation outlet at the inlet of the RWGS reaction section.
- the method further comprises providing an H2 supply in the pyrolysis gas by means of a make-up line.
- the pyrolysis unit comprises at least one reactor used in at least one of the following operating conditions:
- - zeolite catalyst comprising and preferably consisting of at least one zeolite chosen from ZSM-5, ferrierite, Beta zeolite, Y zeolite, mordenite, ZSM-23, ZSM-57, EU-1, ZSM-11 and preferably the catalyst is a catalyst comprising only ZSM-5.
- the reaction section of RWGS comprises at least one reactor used in at least one of the following operating conditions:
- - pressure between 0.1 and 10 MPa, preferably between 0.1 and 5 MPa, and more preferably between 0.1 and 2.5 MPa; - gas space velocity at the reactor inlet of between 5000 and 20000 mL/g ca ta/h;
- the fermentation reaction section comprises at least one reactor used under at least one of the following operating conditions:
- the isomerization unit comprises a gas-phase isomerization zone and/or a liquid-phase isomerization zone, in which the gas-phase isomerization zone is used in at least one of the following operating conditions:
- a catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms, and at least one group VIII metal with a content between 0.1 and 0 .3% by weight, limits included, and in which the liquid phase isomerization zone is used under at least one of the following operating conditions:
- a catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms.
- FIG. 1 represents a schematic view of a process according to the present invention making it possible to increase the production of aromatic compounds.
- an effluent comprising essentially or only compounds A corresponds to an effluent comprising at least 80 or 90% by weight, preferably at least 95% by weight, very preferably at least 99% by weight, of compounds HAS.
- the present invention can be defined as a device and a process comprising a sequence of unit operations making it possible to produce paraxylene, benzene and ethanol. This sequence of unit operations makes it possible to convert all of the CO and CO2 by-products.
- the device and the process according to the invention are characterized in that they comprise and use the catalytic units and the separation units known to those skilled in the art for producing benzene and paraxylene, units which are usually found in aromatic complexes.
- One of the characteristics of the present invention can be summarized in the use of CO and CO2, a by-product of a unit for the pyrolysis of hydrocarbon compounds to produce ethanol.
- the combination of a reaction section for the conversion of CO2 into CO by RWGS reaction, a reaction section for the fermentation of the CO present into ethanol in the gas enriched in CO and water leaving the RWGS unit makes it possible to recover all the CO and CO2 by-products of the pyrolysis unit into ethanol and thus obtain a co-production of aromatics and d ethanol from hydrocarbon compounds.
- the device for converting aromatic compounds comprises:
- an optional charge separation unit 1 to separate the first hydrocarbon charge 2 from the aromatic complex into a hydrocarbon cut with 7 carbon atoms or less (C7-) and an aromatic cut with 8 carbon atoms or more (A8+);
- an optional transalkylation unit 8 converting toluene (and optionally benzene) and methylalkylbenzenes such as trimethylbenzenes into xylenes - advantageously this unit can also process tetramethylbenzenes;
- an optional selective hydrogenolysis unit 9 suitable for treating a cut comprising aromatic compounds with 9 and 10 carbon atoms and producing a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds
- an optional separation unit for separating the hydrogenolysis effluent disposed (e.g. directly) downstream of the selective hydrogenolysis unit 9, to produce a plurality of liquid effluent cuts;
- a xylene separation unit 10 e.g. of the crystallization or simulated moving bed type using a molecular sieve and a desorbent such as toluene
- a xylene separation unit 10 making it possible to isolate paraxylene from xylenes and ethylbenzene
- an optional stabilization column 12 making it possible in particular to remove the more volatile species (e.g. C5-) from the aromatic complex, in particular from the effluents from the transalkylation unit 8 and/or from the isomerization unit 11;
- the more volatile species e.g. C5-
- a pyrolysis unit 13 preferably catalytic, for treating a second hydrocarbon charge 30, producing a pyrolysis effluent 31 supplying at least partially the first hydrocarbon charge 2 of the aromatic complex, a pyrolysis gas 32 comprising CO, CO2 and H2, and by-products 33 (mainly compounds middle distillates which, after hydrotreating and/or hydrocracking, can be recovered in the form of Jet Fuel, diesel or marine fuel);
- an RWGS 50 reaction section for treating the pyrolysis gas 32 coming from the pyrolysis unit 13, and producing an RWGS 51 gas enriched in CO and water (and thus depleted in CO2 and H2) with respect to the gas pyrolysis 32;
- an optional dehydration unit (not shown) to dehydrate the ethanol from the fermentation effluent 53 into ethylene;
- an optional alkylation reaction section (not shown) to alkylate at least in part a cut comprising benzene 22 with said ethylene and produce a cut enriched in ethylbenzene (optionally sent to the isomerization unit 11).
- the charge separation unit 1 treats the first hydrocarbon charge 2 of the aromatic complex to separate an overhead cut comprising (e.g. essentially) compounds with 7 carbon atoms or less 16 (C7-) containing in particular benzene and toluene, and a bottoms cut comprising (e.g. essentially) aromatics with 8 or more carbon atoms 17 (A8+) sent to the xylene column 6.
- the unit of Feed separation 1 also separates a first toluene cut 18 comprising at least 90% by weight, preferably at least 95% by weight, most preferably at least 99% by weight of toluene.
- the first toluene cut 18 is sent to the first column for the distillation of aromatic compounds 4, also called the benzene column, and/or to the second column for the distillation of aromatic compounds 5, also called the column of toluene.
- the first hydrocarbon charge 2 is a hydrocarbon cut containing mainly (i.e., > 50% by weight) molecules whose carbon number ranges from 6 to 10 carbon atoms.
- This filler may also contain molecules having more than 10 carbon atoms and/or molecules with 5 carbon atoms.
- the first hydrocarbon charge 2 of the aromatic complex is rich in aromatics (eg > 50% by weight) and preferably contains at least 20% by weight of benzene, preferably at least 30% by weight, very preferably at least 40% by weight of benzene.
- the first hydrocarbon charge 2 can be produced by catalytic reforming of a naphtha or be a product of a cracking unit (eg steam, catalytic) or any other means of producing alkyl aromatics.
- the first hydrocarbon feedstock 2 is at least partially or even entirely biobased.
- the first hydrocarbon feedstock 2 comes (essentially) from a lignocellulosic biomass conversion process.
- an effluent produced by conversion of lignocellulosic biomass can be treated to meet the specifications required of the first hydrocarbon charge 2 in order to present contents of sulphurous, nitrogenous and oxygenated elements compatible with an aromatic complex.
- the first hydrocarbon charge 2 of the aromatic complex comprises at least 25% by weight, preferably at least 30% by weight, very preferably at least 35% by weight, of pyrolysis effluent 31 originating from the pyrolysis unit 13 with respect to the total weight of the charge, the balance comprising (preferably consisting of) a mixture of non-biosourced aromatic and paraffinic compounds (coming for example from a catalytic reforming unit).
- the first hydrocarbon charge 2 of the aromatic complex comprises at least 80% by weight, preferably at least 90% by weight, very preferably at least 95% by weight, of pyrolysis effluent 31 originating from the pyrolysis unit 13.
- the first hydrocarbon charge 2 of the aromatic complex consists of the pyrolysis effluent 31 originating from the pyrolysis unit 13.
- the first hydrocarbon feedstock 2 comprises less than 10 ppmw, preferably less than 5 ppmw, very preferably less than 1 ppmw of elemental nitrogen, and/or less than 10 ppmw, preferably less than 5 ppmw, most preferably less than 1 ppmw elemental sulfur, and/or less than 100 ppmw, preferably less than 50 ppmw, most preferably less than 10 ppmw elemental oxygen.
- the aromatic cut 20 (essentially benzene and toluene) called the extract of the unit extraction of aromatics 3, optionally mixed with the heavy fraction 21 of the transalkylation unit 8 which will be defined below, is sent to the benzene column 4.
- the aromatic fraction 20 is an aromatic (eg essentially) C6-C7 (A6-A7) hydrocarbon feedstock.
- the fractionation train comprises the aromatic compound distillation columns 4, 5, 6 and 7 making it possible to separate the following 5 cuts:
- a cut comprising (e.g. essentially) aromatic compounds with 9 and 10 carbon atoms 25;
- a cut comprising (e.g. essentially) aromatic compounds, the most volatile species of which are aromatics with 10 carbon atoms 26.
- the benzene column 4 is suitable for: treating the aromatic cut 20 which is an (e.g. essentially) aromatic C6-C10 (A6+) hydrocarbon feedstock; produce at the head the cut comprising benzene 22 which may be one of the desired products at the output of the aromatic complex; and producing an (e.g. essentially) aromatic C7-C10 27 (A7+) effluent in the bottom.
- aromatic cut 20 which is an (e.g. essentially) aromatic C6-C10 (A6+) hydrocarbon feedstock
- A6+ aromatic C6-C10
- the toluene column 5 is suitable for: treating the aromatic C7-C10 27 (A7+) effluent, the bottom product of the benzene column 4; produce at the head the cut comprising toluene 23 which is sent to the transalkylation unit 8; and producing an (e.g. essentially) aromatic C8-C10 28 (A8+) effluent in the bottom.
- the third distillation column for aromatic compounds 6, also called a xylene column, is suitable for: treating the aromatic cut with 8 or more carbon atoms 17 (A8+) of the aromatic complex charge and optionally the column bottom effluent toluene 28; produce at the head the cut comprising xylenes and ethylbenzene 24 which is sent to the xylene separation unit 10; and producing an effluent in the bottom (e.g. essentially) comprising C9-C10 aromatics 29 (A9+).
- the fourth distillation column for aromatic compounds 7, also called the heavy aromatics column, is optional and is suitable for: treating the bottom effluent from the xylene column 29; produce at the top the fraction comprising C9-C10 mono-aromatics; and produce in the background the cut comprising (eg essentially) compounds aromatics, the most volatile species of which are aromatics with 10 carbon atoms 26 (A10+).
- the bottom section 26 comprises C11+ compounds.
- the fraction comprising C9-C10 mono-aromatics 25 (and/or the hydrogenolysis effluent enriched in methyl-substituted aromatic compounds described below) is mixed with the cut comprising toluene 23 coming from the head of the toluene column 5, and feeds the reaction section of the transalkylation unit 8 to produce xylenes by transalkylation of aromatics lacking methyl groups (toluene), and in excess of methyl groups (e.g. tri- and tetra-methylbenzenes).
- the transalkylation unit 8 is supplied with benzene (line not shown in Figure 1), for example when an excess of methyl groups is observed for the production of paraxylene. According to one or more embodiments, the transalkylation unit 8 directly treats the bottoms effluent from the xylene column 29.
- the transalkylation unit 8 comprises at least one first transalkylation reactor adapted to be used under at least one of the following operating conditions:
- the first transalkylation reactor is operated in the presence of a catalyst comprising zeolite, for example ZSM-5.
- the second transalkylation reactor is of the fixed bed type.
- the effluents from the reaction section of the transalkylation unit 8 are separated in a first separation column (not shown) downstream of said reaction section of the transalkylation unit 8.
- a cut comprising at least part of the benzene and the more volatile species 38 (C6-) is extracted at the top of the first separation column and is sent to an optional stabilization column 12, making it possible in particular to remove the more volatile species (eg C5-) of the aromatic complex.
- the heavy fraction 21 of the effluents from the first separation column comprising (eg essentially) aromatics with at least 7 carbon atoms (A7+), is optionally recycled to the fractionation train 4-7, for example to the benzene column 4.
- the cut comprising xylenes and ethylbenzene 24 is treated in the xylene separation unit 10 to produce a fraction or an extract 39 comprising paraxylene and a raffinate 40.
- the extract 39 can then be distilled (eg if separation by LMS adsorption), for example by means of an extract column and then an additional toluene column (not shown) in the case where toluene is used as a desorbent, to obtain high purity paraxylene exported as the main product .
- the raffinate 40 from the xylene separation unit 10 comprises (eg essentially) orthoxylene, metaxylene and ethylbenzene and feeds the isomerization unit 11 .
- the xylene separation unit 10 also separates a second toluene cut 41 comprising at least 90% by weight, preferably at least 95% by weight, very preferably at least 99% by weight of toluene .
- the toluene cut 41 may for example be part of the toluene used as a desorbent when the xylene separation unit 10 comprises a so-called simulated moving bed adsorption unit.
- the second toluene cut 41 is sent to the transalkylation unit 8.
- the paraxylene isomers are isomerized while the ethylbenzene can be: isomerized into a mixture of C8 aromatics, for example if it is desired to produce mainly paraxylene; and/or dealkylated to produce benzene, for example if it is desired to produce both paraxylene and benzene.
- the effluents from the isomerization reaction section are sent to a second separation column (not shown) to produce at the bottom an isomerate 42 enriched in paraxylene, preferably recycled to the xylene column 6; and produce at the top a hydrocarbon cut comprising compounds with 7 carbon atoms or less 43 (C7-) sent to the optional stabilization column 12, for example with the cut comprising at least a part of the benzene and the more volatile species 38.
- the isomerization unit 11 comprises a first isomerization zone working in the liquid phase, and/or a second isomerization zone working in the gas phase, as described in the patents above. listed.
- the isomerization unit 11 comprises a first isomerization zone working in the liquid phase, and a second isomerization zone working in the gas phase.
- a first part of the raffinate 40 is sent to the liquid-phase isomerization unit, to obtain a first isomerate which directly and at least partially feeds the separation unit 10, and in the gas phase isomerization unit a second part of the raffinate 40 to obtain an isomerate which is sent to the xylene column 6.
- the gas phase isomerization zone is suitable for use under at least one of the following operating conditions:
- a catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (10 MR or 12 MR), and at least one group VIII metal with a between 0.1 and 0.3% by weight (reduced form), limits included.
- the liquid phase isomerization zone is suitable for use under at least one of the following operating conditions:
- WH hourly space velocity
- a catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (10 MR or 12 MR), preferably a catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 oxygen atoms (10 MR), and even more preferably a catalyst comprising a ZSM-5 type zeolite.
- WH corresponds to the hourly volume of hydrocarbon charge injected relative to the volume of catalyst charged.
- the optional stabilization column 12 produces: at the bottom a stabilized cut comprising (eg essentially) benzene and toluene 44 optionally recycled at the inlet of the charge separation unit 1 and/or aromatics extraction unit 3; and at the top a cut of more volatile species 45 (eg C5-) removed from the aromatic complex.
- the selective hydrogenolysis unit 9 is suitable for:
- the selective hydrogenolysis unit 9 can be adapted to treat aromatics having between 9 and 10 carbon atoms 25 by converting one or more alkyl group(s) with at least two carbon atoms (ethyl groups, propyl, butyl, isopropyl, etc.) attached to a benzene ring, in one or more methyl group(s), i.e. formed from a single CH 3 group .
- the major advantage of the selective hydrogenolysis unit 9 is to increase the content of CH 3 groups and lower the content of ethyl, propyl, butyl, isopropyl, etc., groups in the charge of the unit of isomerization 11 to increase the rate of production of xylenes, and in particular of paraxylene, in said isomerization unit 11 .
- the selective hydrogenolysis unit 9 comprises at least one hydrogenolysis reactor adapted to be used under at least one of the following operating conditions:
- H 2 /HC (hydrocarbon charge) molar ratio of between 1 and 10, and preferably between 1.5 and 6;
- - PPH between 0.1 and 50 h 1 (eg 0.5-50 h 1 ), preferably between 0.5 and 30 h 1 (eg 1 -30 h 1 ), and more preferably between 1 and 20 h 1 (eg 2-8: 1 p.m., 5-8: 1 p.m.).
- the hydrogenolysis reactor is operated in the presence of a catalyst comprising at least one metal from group VIII of the periodic table, preferably nickel and/or cobalt, deposited on a porous support comprising at least one refractory oxide, crystalline or not, with structured porosity or not.
- the Group VIII metal is nickel.
- the presence of a promoter (Group VIB VI IB VIII IB 11 B) is also possible.
- the catalyst is supported on a refractory oxide (eg alumina, silica), optionally treated with a base to neutralize it.
- the hydrogenolysis reactor is of the fixed bed type, and the catalyst support is in the form of extrudates.
- the hydrogenolysis reactor is of the moving bed type, and the catalyst support is in the form of approximately spherical balls.
- a moving bed can be defined as being a bed with gravity flow, such as those encountered in the catalytic reforming of gasolines.
- the second hydrocarbon charge 30 is a mixture of hydrocarbon compounds having an elemental oxygen content at least greater than 1% by weight, preferably 3% by weight, very preferably 5% by weight relative to the total weight of said charge.
- the second hydrocarbon feedstock 30 comprises or consists of lignocellulosic biomass or of one or more lignocellulosic biomass constituents chosen from the group formed by cellulose, hemicellulose and lignin.
- Lignocellulosic biomass can consist of wood, agricultural waste or vegetable waste.
- Other non-limiting examples of lignocellulosic biomass material are agricultural residues (straw, corn stalk%), forestry residues (products of first thinning), forestry products, crops (short-rotation coppice), residues from the agro-food industry, household organic waste, waste from wood processing facilities, used construction wood, paper, whether recycled or not.
- Lignocellulosic biomass can also come from by-products of the paper industry such as Kraft lignin, or black liquors from the manufacture of paper pulp.
- the lignocellulosic biomass can advantageously undergo at least one pretreatment step before its introduction into the process according to the invention.
- the biomass is ground and dried, until the desired particle size is obtained.
- a filler having a particle diameter of between 0.3 and 0.5 mm can advantageously be obtained.
- the particle size of the lignocellulosic biomass to be pyrolyzed is a particle size sufficient to pass through a 1 mm sieve up to a particle size sufficient to pass through a 30 mm sieve.
- the second hydrocarbon charge 30 to be pyrolyzed is advantageously loaded into a drive or pneumatic transport compartment so as to be driven in a fluid pyrolysis reactor of training.
- the drive fluid used is nitrogen gas.
- other non-oxidizing drive fluids may be used.
- part of the pyrolysis gas produced during the process can be recycled and used as driving fluid.
- Said pyrolysis gas mainly consists of an incondensable gaseous effluent comprising at least carbon monoxide (CO) and carbon dioxide (CO2) and also advantageously comprising light olefins comprising from 2 to 4 carbon atoms.
- CO carbon monoxide
- CO2 carbon dioxide
- the second hydrocarbon charge 30 can be loaded into a feed hopper or other device which allows said charge to be fed into the entrainment compartment in an appropriate quantity. In this way, a constant amount of charge is delivered to the drive compartment.
- the entrainment fluid advantageously carries the second hydrocarbon charge 30 from the entrainment compartment into the pyrolysis reactor through a feed tube.
- the feed tube is cooled to maintain the temperature of the second hydrocarbon charge 30 at a required level before it enters the pyrolysis reactor.
- the feed tube can be cooled by jacketing the tube, typically with an air-cooled or liquid-cooled jacket. However, it is also contemplated that the feed tube is not cooled.
- the pyrolysis unit 13 comprises at least one pyrolysis reactor (e.g. fluidized bed) adapted to be used under at least one of the operating conditions listed below.
- pyrolysis reactor e.g. fluidized bed
- the pyrolysis step is carried out at a temperature of between 400 and 1000° C., preferably between 400 and 650° C., preferably between 450 and 600° C. and preferably between 450 and 590°C.
- the use of hot regenerated catalyst from a catalyst regeneration step can make it possible to ensure reactor temperature ranges.
- the pyrolysis step is also advantageously carried out at an absolute pressure of between 0.1 and 0.5 MPa and at a WH of between 0.01 and 10 h 1 , preferably between 0.01 and 5 h 1 , and very preferably between 0.1 and 3lr 1 .
- the WH is the ratio of the volume flow rate of charge to the volume of catalyst used.
- the pyrolysis step is catalytic and carried out in the presence of a catalyst.
- said step operates in the presence of a zeolite catalyst comprising and preferably consisting of at least one zeolite chosen from ZSM-5, ferrierite, Beta zeolite, Y zeolite, mordenite, ZSM-23, ZSM-57, EU-1, ZSM-11 and preferably the catalyst is a catalyst comprising only ZSM-5.
- the zeolite used in the catalyst used in the catalytic pyrolysis step can advantageously be doped preferably with a metal chosen from iron, gallium, zinc and lanthanum.
- the second hydrocarbon charge 30 will first of all undergo rapid pyrolysis in the reactor by contacting the hot catalyst coming from the regenerator which in this stage acts as a thermal vector.
- the gases resulting from this pyrolysis will then react on the catalyst which this time plays its role of catalyst making it possible to catalyze the reactions producing the desired chemical intermediates.
- the second hydrocarbon charge 30 is in particular converted at least partially into a pyrolysis effluent 31 comprising hydrocarbon compounds whose carbon number ranges from 6 to 10 carbon atoms, a pyrolysis gas 32 and by-products 33.
- the pyrolysis effluent 31 feeds the first hydrocarbon charge 2 of the aromatic complex.
- the pyrolysis unit 13 also produces a pyrolysis gas 32 comprising CO, CO2 and H2, and by-products 33.
- the products obtained at the end of the pyrolysis step are advantageously recovered in the form of a gaseous effluent comprising BTX.
- a gaseous fraction of incondensables comprising at least carbon monoxide (CO), and carbon dioxide (CO2),
- BTX a liquid cut called BTX, comprising hydrocarbon compounds whose carbon number ranges from 6 to 10 carbon atoms,
- gaseous fraction of incondensables can also advantageously comprise light olefins comprising from 2 to 4 carbon atoms.
- the coked catalyst as well as the second unconverted hydrocarbon charge usually called “char” are advantageously withdrawn from the reactor and preferably sent to a stripper so as to eliminate the potentially adsorbed hydrocarbons and thus avoid their combustion in the regenerator and this by contacting with at least one gas chosen from water vapour, an inert gas such as for example nitrogen, and part of the gaseous fraction of incondensables resulting from the fractionation of the gaseous effluent resulting from the pyrolysis stage .
- a stripper so as to eliminate the potentially adsorbed hydrocarbons and thus avoid their combustion in the regenerator and this by contacting with at least one gas chosen from water vapour, an inert gas such as for example nitrogen, and part of the gaseous fraction of incondensables resulting from the fractionation of the gaseous effluent resulting from the pyrolysis stage .
- Said coked catalyst and the second unconverted hydrocarbon charge, optionally stripped, are advantageously sent to a regenerator where coke and char are burned by adding air or oxygen, thus producing regenerated catalyst and a CO2-rich combustion gas.
- the regenerated catalyst is advantageously recycled in the reactor of the pyrolysis step in order to undergo another cycle.
- the pyrolysis step of the process according to the invention allows the production of at least 10% by weight and preferably at least 15% by weight of aromatic with respect to the total mass of the reaction products obtained, with a selectivity of at least 65% and preferably at least 70% for BTX.
- the process thus comprises at least one pyrolysis step producing at least one BTX cut (pyrolysis effluent 31) and a gaseous fraction of incondensables (pyrolysis gas 32) comprising at least carbon monoxide and carbon dioxide.
- the process also makes it possible to obtain, in addition to the BTX cut, a heavier liquid fraction, mainly aromatic called “C9+ cut” which can advantageously be recovered in a process outside the process according to the invention.
- At least part of the gaseous fraction of incondensables is recycled, preferably via a compressor, into the reactor of the pyrolysis step.
- This gaseous flow then serves as a driving fluid for the charge in said reactor.
- said recycle gaseous effluent is preferably purged, preferably either upstream or downstream of said compressor.
- the pyrolysis effluent 31 is a hydrocarbon fraction containing mainly (ie, > 50% by weight) molecules whose number of carbon extends from 6 to 10 carbon atoms.
- the pyrolysis effluent 31 can also contain molecules having more than 10 carbon atoms and/or molecules with 5 carbon atoms.
- the pyrolysis effluent 31 is rich in aromatics (eg>50% by weight) and preferably contains at least 20% by weight of benzene, preferably at least 30% by weight, very preferably at least 40% by weight of benzene.
- the pyrolysis effluent 31 is treated to meet the specifications required of the first hydrocarbon charge 2 as described above in order to present contents of sulphurous, nitrogenous and oxygenated elements compatible with an aromatic complex. .
- the pyrolysis gas 32 comprises at least part of the gaseous fraction of incondensables and preferably comprises at least part of the CO2-rich combustion gas.
- the pyrolysis gas 32 produced by the pyrolysis unit 13 comprises a mixture mainly containing (e.g. comprising at least 50% by weight) hydrogen, CO and CO2.
- the pyrolysis gas 32 comprises at least 20% by weight of CO, preferably at least 30% by weight of CO, very preferably at least 40% by weight of CO (e.g. at least 50% by weight of CO).
- the pyrolysis gas 32 comprises at least 0.2% by weight of H2, preferably at least 0.5% by weight of H2, very preferably at least 0.8% by weight of H2. According to one or more embodiments, the pyrolysis gas 32 at the outlet of the pyrolysis unit 13 contains at least 20% by weight of CO2. According to one or more embodiments, the pyrolysis gas 32 at the outlet of the pyrolysis unit 13 contains approximately 30% (e.g. ⁇ 10% by weight) by weight of CO2. According to one or more embodiments, the pyrolysis gas 32 contains methane, ethylene and propylene (e.g. less than 10% by weight) as well as ethane, propane and water (e.g. less than 3% by weight).
- the by-products 33 comprise the C9+ fraction mainly consisting of more or less alkylated di and tri aromatics. This cut can be upgraded directly to bunker fuel, for example, or undergo hydrotreatment and/or hydrocracking to improve its properties and upgrade it to Jet Fuel or diesel.
- an H2 supply fed by the optional make-up line 34 is added to the pyrolysis gas 32 so that the H2/CO2 molar ratio of the pyrolysis gas 32 at the inlet of the RWGS reaction section 50, or between 1 and 10, preferably between 1 and 8, very preferably between 1 and 5.
- the hydrogen content of the pyrolysis gas 32 is preferably modified by adding hydrogen, so as to at least reach the stoichiometry of the RWGS reaction: CO2 + H2 -> CO + H2O.
- the pyrolysis gas 32 optionally enriched by an H2 supply is converted at least partially into an RWGS 51 gas enriched in CO and in water (and thus depleted in CO2 and in H2).
- the RWGS reaction corresponds to the reaction of CO2 and H2 to form CO and water.
- reaction section of RWGS 50 is adapted to be operated under at least one of the following operating conditions:
- the space velocity of the gas at the inlet of the reactor is between 5000 and 20000 mL/gcata/h.
- the catalyst used in the reaction section of RWGS 50 is chosen from the list consisting of catalysts based on iron or alkali metals (eg potassium).
- the catalyst for the RWGS reaction is chosen from the list consisting of catalysts based on Fe/Al2O3, Fe-Cu/Al2O3, Fe-Cs/Al2O3 and CuO-Fe2O3 doped with Cs. Conversions of 70% by weight of CO2 are commonly obtained with the operating conditions described above.
- the reaction section of RWGS 50 is adapted to operate in a fluid bed or a fixed bed.
- the reaction section of RWGS 50 is adapted to produce a gas of RWGS 51 comprising at least 48% by weight of CO in the mixture of CO, CO2 and H2O, preferably at least 54% by weight of CO, most preferably at least 63% by weight CO.
- the pyrolysis gas 32 and/or the RWGS gas 51 can be purified before being converted into ethanol in the fermentation reaction section 52.
- the purification of the synthesis gas aims to eliminate the compounds sulfur, nitrogen, halogens, heavy metals and transition metals.
- the main syngas purification technologies are: adsorption, absorption, catalytic reactions.
- the method comprises a step of sending (preferably all) of the CO and water-enriched RWGS 51 gas resulting from the RWGS step into a fermentation step producing a fermentative liquid stream comprising ethanol.
- the RWGS gas enriched in CO and water comprises a carbon monoxide (CO) content of between 48 and 63% by weight of CO, and preferably between 54 and 63% by weight, the percentages being expressed as a percentage mass relative to the total mass of said RWGS gas.
- CO carbon monoxide
- the fermentation step is advantageously carried out in the presence of at least one microorganism also called acetogenic strain.
- fermentation refers to the conversion of H2, CO and/or CO2 gases and encompass both the growth phase of the fermentative microorganism and the phase of production of the molecules of interest, such as alcohols, acids, acid alcohols and/or carboxylic acids by this microorganism.
- microorganisms capable of carrying out this fermentation process are mainly derived from the genus Clostridium, but other microorganisms, such as those derived for example from the genera Aceto bacteria, Butyribacterium, Desulfobactrium, Moorella, Oxobacter or even Eubacteria can also be used to carry out this fermentation process. .
- microorganisms are therefore chosen in such a way as to direct the production of the desired products during the fermentation stage.
- Fermentation products can include, for example, alcohols and acids.
- various patents describe strains capable of producing the products of interest mentioned above and this from synthesis gas.
- patent US5173429 describing a strain of Clostridium ljungdahlii (ATCC 49587) producing ethanol and acetate.
- Other strains of the same species are described in documents WO 2000/68407, EP117309, patents US5173429, US5593886 and US6368819, WO1998/00558 and WO2002/08438.
- the said acetogenic microorganism(s) or strains used in the fermentation stage of the process according to the invention are preferably chosen from the following microorganisms: Acetogenium kivui, Acetoanaerobium noterae, Aceto bacterium woodii, Alkalibaculum bacchi CP11 (ATCC BAA-1772), Blautia producta , Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter paci/icus subterraneous, hydrogeno/ormans Carboxydothermus, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19630 from DSMZ Germany), Clostridium autoethanogenum (DSM 19630 from DSMZ Germany), Clostridium autoethanum1006 (DSMZ Germany) from DSMZ Germany), Clostridium autoethanogenum (DSM
- microorganisms capable of assimilating H2, CO (otherwise called carboxydotrophs) and/or CO2 as a carbon source can also be used in the fermentation step of this invention. All of the microorganisms mentioned above are said to be anaerobic, that is to say incapable of growing in the presence of oxygen. But aerobic microorganisms can also be used, such as microorganisms belonging to the species Escherichia coli.
- the microorganisms are chosen from Clostridium autoethanogenum, Clostridium ljungdahlii, Clostridium aceticum, Morelia thermoacetica, Acetobacterium woodi and Alkalibaculum bacchi for the production of ethanol and/or acetate, Clostridium autoethanogenum, Clostridium ljungdahlii and C. ragdalei for the production of 2,3 Butanediol and Clostridium carboxidivorans, Clostridium drakei, Clostridium scatologenes or Butyribacterium methylotrophicum for the production of butyrate and butanol.
- Cultures comprising a mixture of two or more microorganisms can also be used.
- the fermentation step can advantageously be carried out aerobically or anaerobically and preferably anaerobically.
- the fermentation stage is advantageously implemented in one or more reactors or “bioreactors”.
- biomass includes a fermentation device consisting of one or more tanks or tube reactors, including devices of the CSTR type or “Continuous Stirred Reservoir Reactor” according to the Anglo-Saxon terminology, ICR or “Immobilized Cell Reactor” according to the Anglo-Saxon terminology, TBR or “Trickle Bed Reactor” according to the Anglo-Saxon terminology, Gas Lift type fermenter, bubble columns, or membrane reactor such as the HFMBR system or "Hollow Fiber membrane Bio-Reactor” according to the terminology Anglo-Saxon, a static mixer, or any other suitable device for gas-liquid contact.
- the required concentration of CO and/or CO2 in the culture medium of said fermentation reactor(s) is at least 2.5 mmol/L of CO and/or CO2.
- Said RWGS gas enriched in CO and water coming from the RWGS unit used as a feed of the fermentation stage, and containing CO, CO2 and H2O is fed into the fermentation reactor(s) in the form of a substrate advantageously containing a CO content of between 48 and 63% by weight of CO, and preferably between 54 and 63% by weight and an H2O content of between 16 and 31% by weight and preferably between 16 and 24% by weight , the percentages being expressed as mass percentage relative to the total mass of said RWGS gas.
- the fermentation step comprises a chain of propagation of an acetogenic strain in order to provide a sufficient quantity of cells to inoculate a main reactor, said propagation chain comprising: i) the inoculation of the acetogenic strain in a first propagation reactor providing a minimum viable cell density for a second propagation reactor having a larger volume, and ii) growing said acetogenic strain in the second reactor to provide a suitable cell density to inoculate a third reactor of propagation, the most important in terms of volume.
- the propagation chain can include a larger number of propagation reactors.
- the fermentation stage also includes a production stage in which the fermentation process is optimal, i.e. in which the molecules of interest are produced in large quantities.
- the stream comprising at least one oxygenated compound as claimed is therefore produced in said production step.
- the propagation step can be implemented in one or more microorganism propagation reactors, all of these reactors being connected to allow the transfer of the microbial culture.
- One or more "production” reactors in which the fermentation process takes place are also implemented.
- Acetogenic microorganisms or strains are usually cultured until optimal cell density is achieved to inoculate production reactors.
- This rate of inoculum can vary from 0.5 to 75%, which makes it possible to have larger production reactors than propagation reactors.
- the propagation reactor can be used to seed several other larger production reactors.
- the RWGS gas enriched in CO and in water can advantageously be introduced into the fermentation stage at the level of the reactors of the production stage.
- At least one additional carbonaceous substrate can advantageously be used in association with the CO-enriched RWGS gas, to grow the microorganisms in the propagation step.
- Said carbon substrate can advantageously be chosen from n monosaccharides such as glucose, fructose or xylose, polysaccharides such as starch, sucrose, lactose or cellulose, metabolic intermediates such as pyruvate or any other carbon substrate known to those skilled in the art as being able to be assimilated by the microorganisms used in the method.
- Said carbonaceous substrate can also be a mixture of two or more of these carbonaceous substrates.
- the control of the operating conditions is also necessary to optimize the implementation of the fermentation stage.
- Lowe et al (Microbiological Review, 1993 57: 451 -509), or Henstra et al (Current Opinion in Biotechnology 2007, 18:200-206), summarize the optimal operating conditions in terms of temperatures and pH, to grow the microorganisms that can be used in the fermentation process.
- the pH is one of the most important factors for the fermentation activity of the microorganisms used in the process.
- said fermentation step is carried out at a pH comprised between 3 and 9, preferably between 4 and 8, and more preferably between 5 and 7.5.
- Temperature is also an important parameter to improve fermentation because it influences both microbial activity and the solubility of gases used as substrate.
- the choice of temperature depends on the microorganism used, some strains being able to grow in moderate temperature conditions (so-called mesophilic strains) and others in high temperature conditions (thermophilic microorganisms).
- said fermentation step is carried out at a growth temperature of between 20 and 80°C.
- said fermentation step is carried out at a growth temperature of between 20 and 40° C. for mesophilic strains and preferably between 25 and 35 and between 40 and 80° C. for thermophilic strains and preferably between 50 and 60°C.
- the oxidation-reduction potential (in other words “redox” potential) is also an important parameter to control in the fermentation process.
- the redox potential is preferably greater than -450 mV and preferably between -150 and -250 mV.
- Said fermentation step is also advantageously carried out at a pressure of between 0.1 and 0.4 MPa.
- the nutrient medium or culture medium of the fermentation stage can advantageously contain at least one reducing agent so as to improve the performance of the fermentation process by controlling the redox potential of the fermentation stage.
- the nutrient medium can also comprise minerals, vitamins, metal co-factors or metals specific to the metalloenzymes involved in the pathways for converting gas into products of interest.
- Suitable anaerobic nutrient media for the fermentation of ethanol using CO and/or CO2 as the sole carbon source(s) are known to those skilled in the art.
- suitable media are described in patents US5173429 and US5593886 and WO02/08438, WO2007/115157 and WO2008/115080 or the publication JR Phillips et al. (Bioresource Technology 190 (2015) 114-121).
- composition of the nutrient medium must allow efficient conversion of the substrate (CO and CO2) into the molecule of interest.
- This conversion of the substrate is advantageously at least 5% and it can range up to 99%, preferably from 10 to 90%, and more preferably 40 to 70%.
- the nutrient medium may contain at least one or more of a nitrogen source, one or more of a phosphorus source and one or more of a potassium source.
- the nutrient medium can comprise any of these three compounds, or any combination of the three, and in one important aspect the medium should comprise all three compounds.
- the nitrogen source can be selected from ammonium chloride, ammonium phosphate, ammonium sulphate, ammonium nitrate, and mixtures thereof.
- the source of phosphorus can be selected from phosphoric acid, ammonium phosphate, potassium phosphate, and mixtures thereof.
- the potassium source may perhaps be selected from potassium chloride, potassium phosphate, potassium nitrate, potassium sulfate, and mixtures thereof.
- the nutrient medium can also comprise: one or more metals such as iron, tungsten, nickel, cobalt, magnesium; and/or sulfur; and/or thiamine.
- the medium can include any of these components, or any combination and in an important aspect, includes all of these components.
- the source of iron may be chosen from ferrous chloride, ferrous sulphate and mixtures thereof.
- the source of tungsten can be chosen from sodium tungstate, calcium tungstate, potassium tungstate and mixtures thereof.
- the nickel source can include a nickel source selected from the group consisting of nickel chloride, nickel sulfate, nickel nitrate, and mixtures thereof.
- the source of cobalt can be selected from cobalt chloride, cobalt fluoride, cobalt bromide, cobalt iodide and mixtures thereof.
- the magnesium source can be selected from magnesium chloride, magnesium sulfate, magnesium phosphate, and mixtures thereof.
- the sulfur source can include cysteine, sodium sulfide, and mixtures thereof.
- the fermentation stage can also advantageously be implemented as described in patent applications W02007/117157, W02008/115080, US6340581, US6136577, US 5593886, US5807722 and US58211 11.
- the optimal operating conditions for carrying out this fermentation step depend in part on the microorganism(s) used.
- the most important parameters to control include pressure, temperature, gas and liquid flow, medium pH, redox potential, agitation speed and inoculum level. It must also be ensured that the contents of gaseous substrates in the liquid phase are not limiting. Examples of suitable operating conditions are described in patents WO02/08438, WO07/117157 and WO08/115080.
- the ratio between H2 and the gaseous substrates CO and CO2 can also be important to control the nature of the alcohols produced by the fermentative microorganisms.
- the fermentation should be carried out at a pressure above ambient pressure.
- Putting an increased pressure makes it possible to substantially increase the rate of gas transfer in the liquid phase so that it is assimilated by the microorganism as a source of carbon.
- This operation allows in particular a reduction in the retention time (defined as the volume of liquid in the bioreactor divided by the inlet gas flow rate) in the bioreactor and therefore better productivity (defined as the number of grams of molecules of interest produced per liter and per day of production) of the fermentation process. Examples of productivity improvements are described in patent WO02/08438.
- said fermentation step produces a fermentation liquid stream comprising ethanol.
- the fermentation liquid stream comprises at least 80%, preferably at least 90%, very preferably at least 95% by weight of ethanol relative to the total weight of the fermentation liquid stream, for example after concentration in ethanol fermentative liquid stream, for example by distillation.
- the fermentation liquid stream produced by the fermentation step can also contain nutrient medium, molecules of interest (alcohols, alcohols acids, acids), i.e. a flow of oxygenated compounds as described below and bacterial cells.
- molecules of interest alcohols, alcohols acids, acids
- the fermentation liquid stream comprises ethanol and at least one other oxygenated compound chosen from alcohols having 2 to 6 carbon atoms, diols having 2 to 4 carbon atoms, acid alcohols having 2 to 4 carbon atoms, carboxylic acids having 2 to 6 carbon atoms, aldehydes having 2 to 12 carbon atoms and esters having 2 to 12 carbon atoms, alone or as a mixture.
- the alcohols having 2 to 6 carbon atoms are chosen from n-propanol, isopropanol, butanol, isobutanol, hexanol, the diols having 2 to 4 carbon atoms are chosen from 2,3-butylene glycol (butane-2,3-diol), the alcohol acids having 2 to 4 carbon atoms is preferably lactic acid, the carboxylic acids having 2 to 6 carbon atoms are chosen from acetic acid, butyric acid, hexanoic acid, the aldehydes having 2 to 12 carbon atoms are chosen from ethanal, propanal, butanal, pentanal, 3-methylbutanal, hexanal, furfural and glyoxal alone or as a mixture and the esters having 2 to 12 carbon atoms and preferably 2 to 6 carbon atoms are chosen from methyl formate, methyl acetate, methyl propanoate, methyl butan
- the fermentation liquid stream comprises at least one oxygenated compound chosen from n-propanol, isopropanol, butanol, isobutanol, hexanol, acetic acid, butyric acid, hexanoic acid, lactic acid and 2,3-butylene glycol (butane-2,3-diol), alone or as a mixture.
- oxygenated compound chosen from n-propanol, isopropanol, butanol, isobutanol, hexanol, acetic acid, butyric acid, hexanoic acid, lactic acid and 2,3-butylene glycol (butane-2,3-diol), alone or as a mixture.
- Additional hydrogen can advantageously be introduced or not into said fermentation stage in the case where the composition of the feedstock supplying said stage does not include a sufficient quantity of hydrogen.
- the use of a substrate low in H2 leads to the production of significant acids. Indeed, as mentioned previously, the supply of additional hydrogen makes it possible to improve the conversion of the CO present in the fermentation medium into alcohols (according to the balance equations of Bertsch and Müller Biotechnol Biofuels (2015) 8:210) and of promote the conversion of CO2.
- the make-up hydrogen can advantageously come from any process allowing the production of hydrogen, such as for example from a steam reforming process or from a catalytic reforming process, from the electrolysis of water, of the dehydrogenation of alkanes, and its hydrogen purity is usually between 75 and 99.9% by volume.
- This make-up hydrogen is supplied via line 34.
- CO2 is recycled via line 54 to the inlet of the RWGS reaction section 50, and/or the water produced by line 55.
- reaction section of RWGS 50 followed by a fermentation section 52 allows a co-production of ethanol and aromatics while converting all the CO and CO2 by-products of the unit of pyrolysis 13.
- the ethanol from the fermentation effluent 53 into ethylene is sent to an optional dehydration unit (not shown) suitable for dehydrating the ethanol into ethylene.
- the dehydration unit comprises at least one dehydration reactor (e.g. adiabatic reactor containing at least one fixed bed) adapted to be used under at least one of the following operating conditions:
- dehydration reactor e.g. adiabatic reactor containing at least one fixed bed
- the dehydration catalyst is an amorphous acid catalyst or a zeolitic acid catalyst, such as a zeolite having at least pore openings containing 8, 10 or 12 oxygen atoms (8 MR, 10MR or 12 MR).
- said zeolite dehydration catalyst comprises at least one zeolite having a structural type chosen from the structural types MFI, MEL, EAU, MOR, FER, SAPO, TON, CHA, EUO and BEA.
- said zeolite dehydration catalyst comprises a zeolite with structural type MPI and preferably a ZSM-5 zeolite.
- the benzene of the cut comprising benzene 22 is at least partially alkylated by ethylene to ethylbenzene in an optional alkylation reaction section (not shown) to produce a cut enriched in ethylbenzene.
- the alkylation reaction section comprises at least one reactor (eg in a fixed bed) for alkylation adapted to be used under at least one of the following operating conditions:
- a catalyst comprising a zeolite (e.g. optionally dealuminated Y zeolite).
- the cut enriched in ethylbenzene is sent to a fractionation unit to produce an ethylbenzene cut, a benzene cut which can for example be recycled at least in part to the alkylation reaction section, and optionally one or more polyethylbenzene cuts.
- the ethylbenzene cut feeds the isomerization unit 11. In this way, all the ethylbenzene, initially present in the charge and produced by alkylation in the alkylation reaction section, is introduced and converted into paraxylene in the aromatic loop containing the isomerization unit 11 and the xylene separation unit 10.
- group VIII according to the CAS classification corresponds to the metals of columns 8, 9 and 10 according to the new IUPAC classification
- group Vlb according to the CAS classification corresponds to the metals of column 6 according to the new IUPAC classification.
- An example of a reference device for converting a feed comprising a mixture of aromatic compounds resulting from a process for converting lignocellulosic biomass based on conversion by catalytic pyrolysis is used.
- the exemplary reference device is similar to the device represented in FIG. 1 except that the transalkylation unit 8 is replaced by a disproportionation unit.
- the example reference device does not implement the following units:
- the pyrolysis reaction section produces CO and CO2, which are not converted into other chemical compounds.
- the flow of CO produced is 22.25 t/h, the flow of CO2 15.99 t/h.
- the example of device according to the invention makes it possible to increase the production of both benzene and paraxylene and ethanol while recovering all the biosourced carbon lost in the form of CO and CO2 of the example of the reference device .
- the reaction section of RWGS 50 the reaction section of fermentation 52
- Ethanol is produced by line 53.
- the pyrolysis gas 32 coming from the catalytic pyrolysis unit 13 containing CO, CO2 and hydrogen, is introduced into the reaction section of RWGS 50, with a hydrogen make-up via line 34.
- the RWGS gas 51 is introduced into a fermentation reaction section 52.
- the CO2 is recycled to the inlet of the RWGS reaction section 50, and the water produced is purged via line 55.
- the ethanol produced by the fermentation is extracted via line 53.
- the conversion thanks to this process of CO and CO2, is complete.
- the water formed can advantageously be used upstream of the pyrolysis unit 13 for the biomass pretreatment operations.
- the fermentation thus makes it possible to produce 61.52 t/h of ethanol.
- Table 1 shows that the implementation according to the invention makes it possible to produce 11.98 t/h of aromatics and 61.52 t/h of ethanol. All of the carbon present in the CO and CO2 is thus recovered in the form of ethanol
- a quantity of water equal to 58.12 t/h is also produced, it can be used in the biomass pretreatment stages upstream of the pyrolysis unit.
Abstract
Description
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PCT/EP2021/075177 WO2022069211A1 (en) | 2020-09-29 | 2021-09-14 | Production of aromatics and ethanol by pyrolysis, reverse water-gas shift reaction, and fermentation. |
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EP21773411.0A Pending EP4222232A1 (en) | 2020-09-29 | 2021-09-14 | Production of aromatics and ethanol by pyrolysis, reverse water-gas shift reaction, and fermentation |
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US (1) | US20230374555A1 (en) |
EP (1) | EP4222232A1 (en) |
JP (1) | JP2023542421A (en) |
FR (1) | FR3114594B1 (en) |
WO (1) | WO2022069211A1 (en) |
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US4533211A (en) | 1983-01-31 | 1985-08-06 | International Business Machines Corporation | Frequency multiplexed optical spatial filter based upon photochemical hole burning |
US5173429A (en) | 1990-11-09 | 1992-12-22 | The Board Of Trustees Of The University Of Arkansas | Clostridiumm ljungdahlii, an anaerobic ethanol and acetate producing microorganism |
US6136577A (en) | 1992-10-30 | 2000-10-24 | Bioengineering Resources, Inc. | Biological production of ethanol from waste gases with Clostridium ljungdahlii |
US5593886A (en) | 1992-10-30 | 1997-01-14 | Gaddy; James L. | Clostridium stain which produces acetic acid from waste gases |
US5807722A (en) | 1992-10-30 | 1998-09-15 | Bioengineering Resources, Inc. | Biological production of acetic acid from waste gases with Clostridium ljungdahlii |
US5821111A (en) | 1994-03-31 | 1998-10-13 | Bioengineering Resources, Inc. | Bioconversion of waste biomass to useful products |
JP4101295B2 (en) | 1996-07-01 | 2008-06-18 | バイオエンジニアリング・リソーシズ・インコーポレーテツド | Biological production of acetic acid from waste gas |
UA72220C2 (en) | 1998-09-08 | 2005-02-15 | Байоенджініерінг Рісорсиз, Інк. | Water-immiscible mixture solvent/cosolvent for extracting acetic acid, a method for producing acetic acid (variants), a method for anaerobic microbial fermentation for obtaining acetic acid (variants), modified solvent and a method for obtaining thereof |
AU764291B2 (en) | 1999-05-07 | 2003-08-14 | Emmaus Foundation, Inc. | Clostridium strains which produce ethanol from substrate-containing gases |
DE60121335T2 (en) | 2000-07-25 | 2007-08-02 | Emmaus Foundation, Inc., Fayetteville | PROCESS FOR INCREASING ETHANOL PRODUCTION IN MICROBIAL FERMENTATION |
US7588399B2 (en) | 2005-09-16 | 2009-09-15 | Black & Decker Inc. | PTO selector mechanism for parallel axis transmission |
NZ546496A (en) | 2006-04-07 | 2008-09-26 | Lanzatech New Zealand Ltd | Gas treatment process |
US7623909B2 (en) | 2006-05-26 | 2009-11-24 | Cameron Health, Inc. | Implantable medical devices and programmers adapted for sensing vector selection |
US7704723B2 (en) | 2006-08-31 | 2010-04-27 | The Board Of Regents For Oklahoma State University | Isolation and characterization of novel clostridial species |
NZ553984A (en) | 2007-03-19 | 2009-07-31 | Lanzatech New Zealand Ltd | Alcohol production process |
CN107090424A (en) | 2008-01-22 | 2017-08-25 | 基因组股份公司 | Utilize the method and organism of synthesis gas or other gaseous carbon sources and methanol |
EP2307556B1 (en) | 2008-06-09 | 2020-08-05 | Lanzatech New Zealand Limited | Production of butanediol by anaerobic microbial fermentation |
BRPI0922276A2 (en) | 2008-12-16 | 2015-08-04 | Genomatica Inc | "unnaturally occurring microbial organism, and method for producing isopropanol, 4-hydroxybutyrate, and 1,4-butanediol." |
US9365868B2 (en) | 2011-02-25 | 2016-06-14 | Lanzatech New Zealand Limited | Fermentation process for producing isopropanol using a recombinant microorganism |
TWI537389B (en) | 2011-03-31 | 2016-06-11 | 藍瑟科技紐西蘭有限公司 | A fermentation process for controlling butanediol production |
EP3233770B1 (en) * | 2014-12-17 | 2020-07-15 | King Abdullah University Of Science And Technology | Xylene isomerization |
FR3051800B1 (en) * | 2016-05-31 | 2018-06-15 | IFP Energies Nouvelles | PROCESS FOR PRODUCING BTX BY CATALYTIC PYROLYSIS FROM NON-RECYCLED BIOMASS OF OXYGEN COMPOUNDS |
-
2020
- 2020-09-29 FR FR2009869A patent/FR3114594B1/en active Active
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- 2021-09-14 US US18/028,266 patent/US20230374555A1/en active Pending
- 2021-09-14 EP EP21773411.0A patent/EP4222232A1/en active Pending
- 2021-09-14 WO PCT/EP2021/075177 patent/WO2022069211A1/en unknown
- 2021-09-14 JP JP2023519211A patent/JP2023542421A/en active Pending
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FR3114594A1 (en) | 2022-04-01 |
FR3114594B1 (en) | 2023-11-10 |
US20230374555A1 (en) | 2023-11-23 |
JP2023542421A (en) | 2023-10-06 |
WO2022069211A1 (en) | 2022-04-07 |
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