CN113648937A - System for directly preparing liquid fuel by biomass integrated hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading - Google Patents
System for directly preparing liquid fuel by biomass integrated hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading Download PDFInfo
- Publication number
- CN113648937A CN113648937A CN202110995177.XA CN202110995177A CN113648937A CN 113648937 A CN113648937 A CN 113648937A CN 202110995177 A CN202110995177 A CN 202110995177A CN 113648937 A CN113648937 A CN 113648937A
- Authority
- CN
- China
- Prior art keywords
- unit
- biomass
- gas
- bed reaction
- communicated
- 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
- 239000002028 Biomass Substances 0.000 title claims abstract description 112
- 239000007788 liquid Substances 0.000 title claims abstract description 38
- 239000000446 fuel Substances 0.000 title claims abstract description 32
- 238000007233 catalytic pyrolysis Methods 0.000 title claims abstract description 29
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 29
- 238000006243 chemical reaction Methods 0.000 claims abstract description 124
- 239000007789 gas Substances 0.000 claims abstract description 113
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000012265 solid product Substances 0.000 claims abstract description 18
- 238000002407 reforming Methods 0.000 claims abstract description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000000629 steam reforming Methods 0.000 claims abstract description 12
- 238000004868 gas analysis Methods 0.000 claims abstract description 11
- 239000012263 liquid product Substances 0.000 claims abstract description 11
- 150000001721 carbon Chemical class 0.000 claims abstract description 8
- 230000010354 integration Effects 0.000 claims abstract description 8
- 239000000203 mixture Substances 0.000 claims abstract description 6
- 239000001257 hydrogen Substances 0.000 claims description 38
- 229910052739 hydrogen Inorganic materials 0.000 claims description 38
- 239000002245 particle Substances 0.000 claims description 33
- 238000003756 stirring Methods 0.000 claims description 15
- 230000008878 coupling Effects 0.000 claims description 9
- 238000010168 coupling process Methods 0.000 claims description 9
- 238000005859 coupling reaction Methods 0.000 claims description 9
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- 239000012528 membrane Substances 0.000 claims description 6
- 230000001502 supplementing effect Effects 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims 2
- 229930195733 hydrocarbon Natural products 0.000 abstract description 15
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 15
- 238000000034 method Methods 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 14
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 11
- 229910052799 carbon Inorganic materials 0.000 abstract description 7
- 238000000197 pyrolysis Methods 0.000 description 38
- 239000000047 product Substances 0.000 description 22
- 239000000463 material Substances 0.000 description 19
- 239000007787 solid Substances 0.000 description 19
- 239000001301 oxygen Substances 0.000 description 16
- 229910052760 oxygen Inorganic materials 0.000 description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 15
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 14
- 238000007789 sealing Methods 0.000 description 10
- 238000010521 absorption reaction Methods 0.000 description 9
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- 239000002994 raw material Substances 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 230000006872 improvement Effects 0.000 description 8
- 239000003921 oil Substances 0.000 description 8
- 239000000571 coke Substances 0.000 description 7
- 150000002431 hydrogen Chemical class 0.000 description 7
- 230000000087 stabilizing effect Effects 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000002253 acid Substances 0.000 description 6
- 239000012159 carrier gas Substances 0.000 description 6
- 239000000843 powder Substances 0.000 description 6
- 239000000741 silica gel Substances 0.000 description 6
- 229910002027 silica gel Inorganic materials 0.000 description 6
- 239000012075 bio-oil Substances 0.000 description 5
- 238000009826 distribution Methods 0.000 description 5
- 230000004048 modification Effects 0.000 description 5
- 238000012986 modification Methods 0.000 description 5
- 238000010926 purge Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000012544 monitoring process Methods 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 238000006068 polycondensation reaction Methods 0.000 description 3
- 239000012716 precipitator Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- WGECXQBGLLYSFP-UHFFFAOYSA-N 2,3-dimethylpentane Chemical compound CCC(C)C(C)C WGECXQBGLLYSFP-UHFFFAOYSA-N 0.000 description 2
- JVSWJIKNEAIKJW-UHFFFAOYSA-N 2-Methylheptane Chemical compound CCCCCC(C)C JVSWJIKNEAIKJW-UHFFFAOYSA-N 0.000 description 2
- GXDHCNNESPLIKD-UHFFFAOYSA-N 2-methylhexane Chemical compound CCCCC(C)C GXDHCNNESPLIKD-UHFFFAOYSA-N 0.000 description 2
- ZLCSFXXPPANWQY-UHFFFAOYSA-N 3-ethyltoluene Chemical compound CCC1=CC=CC(C)=C1 ZLCSFXXPPANWQY-UHFFFAOYSA-N 0.000 description 2
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- 239000000443 aerosol Substances 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- RBHJBMIOOPYDBQ-UHFFFAOYSA-N carbon dioxide;propan-2-one Chemical compound O=C=O.CC(C)=O RBHJBMIOOPYDBQ-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 description 2
- GDOPTJXRTPNYNR-UHFFFAOYSA-N methylcyclopentane Chemical compound CC1CCCC1 GDOPTJXRTPNYNR-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- BZHMBWZPUJHVEE-UHFFFAOYSA-N 2,3-dimethylpentane Natural products CC(C)CC(C)C BZHMBWZPUJHVEE-UHFFFAOYSA-N 0.000 description 1
- 239000010963 304 stainless steel Substances 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- 241000219000 Populus Species 0.000 description 1
- 108010001267 Protein Subunits Proteins 0.000 description 1
- 239000012494 Quartz wool Substances 0.000 description 1
- 229910000589 SAE 304 stainless steel Inorganic materials 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 206010057040 Temperature intolerance Diseases 0.000 description 1
- UOFACQRYBTYIPE-UHFFFAOYSA-N [Mo].[Ni].[Cu].[C] Chemical compound [Mo].[Ni].[Cu].[C] UOFACQRYBTYIPE-UHFFFAOYSA-N 0.000 description 1
- RAFNAMHEPCFDRC-UHFFFAOYSA-N [W].[Mo].[Co].[Ni] Chemical compound [W].[Mo].[Co].[Ni] RAFNAMHEPCFDRC-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000005899 aromatization reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000005465 channeling Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002657 fibrous material Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000008543 heat sensitivity Effects 0.000 description 1
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- -1 small molecule hydrocarbon Chemical class 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910000314 transition metal oxide Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
Images
Classifications
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
-
- 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
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
-
- 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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
-
- 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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
- C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
- C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
- C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
-
- 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
-
- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
-
- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
- C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals
- C10G2/332—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the iron-group
-
- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/341—Apparatus, reactors with stationary catalyst bed
-
- 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
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- 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
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
-
- 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
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
-
- 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
- C01B2203/063—Refinery processes
- C01B2203/065—Refinery processes using hydrotreating, e.g. hydrogenation, hydrodesulfurisation
-
- 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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Abstract
The invention relates to a system for directly preparing liquid fuel by biomass integration hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading, which comprises: the system comprises a biomass feeding unit, a fluidized bed reaction unit, a solid product collecting unit, an online quality-improving fixed bed reaction unit, a liquid product collecting unit, a gas analysis unit, a steam reforming unit and an air inlet unit which are sequentially connected, wherein the steam reforming unit receives and reforms a pyrolyzed non-condensable gas mixture, and molecular hydrogen generated after reforming enters the air inlet unit; the air inlet unit is divided into three air paths after passing through the air path switch; the catalyst used in the online upgrading fixed bed reaction unit is a modified carbon-based catalyst, and the carbon base in the modified carbon-based catalyst is derived from the solid product collected by the solid product collection unit. The liquid fuel has high conversion quality and short process flow, and can be directly prepared from biomass to liquid hydrocarbon on one device; the economic competitiveness is strong, and the economy is improved by comprehensively utilizing all the components of the biomass.
Description
Technical Field
The invention relates to the technical field of renewable energy sources, in particular to a system for directly preparing liquid fuel by biomass integration, hydrogenation, pressurization, catalytic pyrolysis and online upgrading.
Background
Biomass can be the only renewable energy source that can be directly converted into carbonaceous liquid fuels. Data show that the yield of only agriculture and forestry waste biomass in China is as high as 4.6 million tons of standard coal per year, but at present, the biomass is usually abandoned in a large amount or is incinerated in the open air, which causes a series of serious secondary pollution problems. The biomass replaces liquid fuel for petroleum production vehicles or aviation, which is not only beneficial to establishing a stable and reliable fuel supply system, but also can obviously reduce the emission of greenhouse gases.
Among the numerous biomass utilization technologies, fast pyrolysis has been used as a technique to densify biomass to produce liquid fuels, which can then be burned to generate electricity or transported to refineries for processing into alternative fuels or high-value chemicals. The biomass pyrolysis has the advantages of full component utilization, strong raw material adaptability, high conversion efficiency and the like. However, oils produced by the fast pyrolysis of biomass have many undesirable characteristics, including high total acid number, high viscosity, low calorific value, high oxygen content, complex composition, poor chemical stability, high water content up to 45%, and inherent incompatibility with petroleum fractions. Compared with liquid hydrocarbon compounds, the low energy density characteristic of the biomass pyrolysis oil makes the transportation link complicated and the cost high, the traditional transportation container and hydrofining conversion equipment of an oil refinery cannot bear the high corrosivity of the oil product, and the pyrolysis oil and the petroleum fraction are immiscible, so that smelting and refining cannot be carried out.
The products of the pyrolysis of the biomass still need to be subjected to further upgrading means such as hydrogenation, isomerization and the like to realize the key conversion from the complex oxygen-containing compounds to the high-grade liquid fuel for vehicles or aviation. The traditional upgrading technology mostly uses liquid bio-oil as a raw material, and the condensed bio-oil needs to be reheated to the reaction temperature required by upgrading. However, the difficulty of volatility of bio-oil, and the problems of polycondensation and coking deactivation of catalyst due to heat sensitivity limit further development.
Although the quality of the bio-oil can be improved by introducing the catalytic pyrolysis of the deoxidation catalysts such as molecular sieves and the like, the catalytic pyrolysis is limited by the hydrogen deficiency and oxygen enrichment characteristics of biomass, and the coking of the catalysts is serious. The improved catalytic system can inhibit coking to a certain extent, but the yield of target hydrocarbon products is still low, and the economy of biorefinery is improved by combining innovation of a pyrolysis conversion process.
Pyrolysis oil is upgraded to remove oxygenates and produce liquid fuels, often requiring additional sources of hydrogen (commonly hydrogen, methane, natural gas, etc.). Pyrolysis oil upgrading requires special reaction processes to achieve sufficiently long run times and avoids problems of reactor plugging and severe catalyst deactivation caused by biomass pyrolysis volatile polymerization.
Besides the quality of the bio-oil, the byproducts such as gas products and solid biochar generated in the biomass conversion process cannot be effectively utilized, and the proportion of the byproducts in the pyrolysis products is large, wherein the gas products (CO, CO)2，CH4And the like) yield is about 10-25 wt%, the yield of the biochar is about 10-30 wt%, the problems of low economy, potential environmental pollution and the like are caused, and the large-scale utilization of the biomass converted into the liquid fuel is limited.
Disclosure of Invention
Aiming at the problems, the invention provides a system for directly preparing liquid fuel by coupling biomass integration hydrogenation pressurization catalytic pyrolysis with online quality improvement, which has high conversion rate and short process flow; the high-temperature pyrolysis product is directly sent into the online quality-improving fixed bed reaction unit without cooling, so that the generation of unstable component condensation and polycondensation and the energy loss caused in the condensation and reheating process are avoided, the energy consumption and the cost are reduced, and the economic competitiveness is strong. And the liquid product, the solid product and the gas product generated by biomass pyrolysis can be comprehensively utilized in all components, the overall utilization efficiency of the biomass is effectively improved, the cost is reduced, and the biomass-prepared liquid fuel system for aviation can be promoted to realize economic and green circulation.
The invention provides a system for directly preparing liquid fuel by biomass integration hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading, which comprises: the system comprises a biomass feeding unit, a fluidized bed reaction unit, a solid product collecting unit, an online quality-improving fixed bed reaction unit, a liquid product collecting unit, a gas analysis unit, a steam reforming unit and an air inlet unit which are sequentially connected, wherein the steam reforming unit receives and reforms a non-condensable gas mixture subjected to hydrogenation catalytic pyrolysis by the fluidized bed reaction unit, and molecular hydrogen generated after reforming enters the air inlet unit; the air inlet unit is divided into three air paths after passing through the air path switch, the first air path is communicated with an inlet of the fluidized bed reaction unit, the second air path and the third air path are respectively communicated with a biomass bin of the biomass feeding unit and an outlet of a quantitative feeder of the biomass feeding unit, and an inlet of the quantitative feeder is communicated with an outlet at the bottom of the biomass bin; the catalyst used in the online upgrading fixed bed reaction unit is a modified carbon-based catalyst, and the carbon base in the modified carbon-based catalyst is derived from the solid product collected by the solid product collection unit.
According to the technical scheme, the gas inlet unit provides a hydrogen source required by the fluidized bed reaction unit through the gas preheater to realize hydrogenation catalytic pyrolysis; the air inlet unit is communicated with the biomass bin, so that pressure compensation can be performed on the biomass bin, the situation that the pressure in the biomass bin is too low is prevented, and the normal operation of discharging in the biomass bin is ensured; the air inlet unit is communicated with the outlet of the quantitative feeder, so that the purging biomass can be assisted to enter the fluidized bed reaction unit, the speed of the biomass material entering the fluidized bed reaction unit from the outlet of the quantitative feeder is increased, the biomass material is prevented from being blocked at the outlet of the quantitative feeder, and the normal operation of the whole reaction system is influenced.
According to the technical scheme, the biomass is subjected to hydrogenation, pressurization and catalytic pyrolysis to obtain pyrolysis volatile matters and coke with low oxygen content, the pyrolysis volatile matters enter an online quality-improving fixed bed reaction unit to carry out deep hydrodeoxygenation reaction, and the vehicle and aviation liquid fuel with high calorific value, ultralow acid value and ultralow oxygen content is directly produced. The required on-line upgrading catalyst is mainly derived from a charcoal-based catalyst obtained by fluidized bed reaction after modification of biochar, and hydrogen required by the system can be supplemented by reforming hydrogen production through micromolecular hydrocarbons in reaction tail gas so as to achieve the aim of circulation self-sufficiency of the whole hydrogen source of the reaction system.
In an optional technical scheme of the invention, the biomass feeding unit further comprises a feeder and a bridge breaker, the bridge breaker is connected with the top of the biomass bin, the bridge breaker comprises a rotary stirring screw rod extending into the biomass bin and stirring blades distributed in the axial direction of the rotary stirring screw rod, an outlet of the quantitative feeder is communicated with an inlet of the feeder, and an outlet of the feeder is communicated with an inlet of the fluidized bed reaction unit.
According to the technical scheme, the bridge breaker can fully stir the biomass in the biomass bin, and the biomass is regularly and quantitatively supplied to the fluidized bed reaction unit by combining with the quantitative feeder, so that the generation of catalytic reaction in the fluidized bed reaction unit is promoted; the feeder can supply the living beings of doser export for the fluidized bed reaction unit fast, guarantees the normal clear of the pyrolysis reaction in the fluidized bed reaction unit.
In an optional technical scheme of the invention, the solid product collecting unit comprises a cyclone separator and a particle filter, an inlet of the cyclone separator is communicated with an outlet of the fluidized bed reaction unit, a top outlet of the cyclone separator is communicated with a top inlet of the particle filter, the bottom of the cyclone separator is detachably connected with a first collecting tank communicated with the cyclone separator, and the bottom of the particle filter is detachably connected with a second collecting tank communicated with the particle filter.
According to the technical scheme, large solid particles and small solid particles at the outlet of the fluidized bed reaction unit can be filtered, the gas-solid separation of pyrolysis volatile components is realized, and the efficient implementation of the subsequent quality improvement reaction of the pyrolysis volatile components is ensured. The solid particles filtered by the cyclone separator and the particle filter are biochar, so that the obtained biochar is conveniently used for modification in the subsequent process, and the on-line quality-improving carbon-based catalyst is prepared and is required by the on-line quality-improving fixed bed.
In an optional technical scheme of the invention, the liquid product collecting unit comprises a condenser, a primary low-temperature condenser, a secondary low-temperature condenser, an electric tar supplementing device and a gas filter which are sequentially connected.
According to the technical scheme, the products at the outlet of the online quality-improving fixed bed reaction unit are subjected to multi-stage condensation, and liquid hydrocarbon products (including water and heavy tar) at the outlet of the online quality-improving fixed bed reaction unit are collected in a grading manner, so that the later-stage resource utilization is facilitated by adopting different utilization modes according to different components.
In an optional technical scheme of the invention, the gas analysis unit comprises a pressure reducing valve and a micro gas chromatograph, the pressure reducing valve is arranged on an outlet pipeline of the gas filter, and the micro gas chromatograph is arranged on the outlet pipeline.
According to the technical scheme, the gas components entering the micro gas chromatograph can be detected on line, and the pyrolysis hydrogenation, the catalytic upgrading and the catalyst state of the whole reaction system can be monitored in real time.
In an optional technical scheme of the invention, the steam reforming unit comprises a reforming reactor, a hydrogen filter membrane, a gas pressure stabilizing tank and a pressurizing device which are sequentially connected, wherein an inlet of the reforming reactor is communicated with an outlet of the gas analysis unit, and an outlet of the pressurizing device is communicated with an inlet of the gas inlet unit.
According to the technical scheme, a reforming reactor is adopted to reform light gases (C1-C3 hydrocarbon and CO) generated after reaction to produce hydrogen so as to supply hydrogen required by hydropyrolysis and on-line upgrading reaction; the reformed gas is selectively filtered by a hydrogen filter membrane to remove residual CO2And CO, etc. The gas pressure stabilizing tank is mainly used for storing hydrogen sources, including but not limited to hydrogen, methane, natural gas and the like, providing hydrogen required by the fluidized bed reaction unit, and can be supplemented through an external gas cylinder or a pipeline under the condition that the hydrogen source inventory is insufficient; the pressurizing device pressurizes the gas entering the gas preheater.
Drawings
FIG. 1 is a schematic structural diagram of a system for directly preparing liquid fuel by biomass integration hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading.
Reference numerals:
1-a biomass feed unit; 11-a biomass silo; 12-a doser; 13-a feeder; 14-a bridge breaker; 141 rotating the stirring screw; 142-a stirring blade; 2-a fluidized bed reaction unit; 21-air distribution plate; 3-a solid product collection unit; 4-online quality improvement fixed bed reaction unit; 5-a liquid product collection unit; 51-a condenser; 511-collection bottle; 52-first stage low temperature condenser; 521-an absorption bottle; 522-a cryogenic tank; 53-two-stage cryogenic condenser; 54-electric tar replenishing device; 541-a tar trap sleeve; 542-tar collector; 543-a high voltage power supply; 55-a gas filter; 6-a gas analysis unit; 61-a pressure reducing valve; 62-Micro GC; 63-a flow meter; 64-pneumatic back pressure valve; 7-a gas preheater; 8-a steam reforming unit; 9-air inlet unit.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a system for directly preparing liquid fuel by biomass integration hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading, which comprises: the system comprises a biomass feeding unit 1, a fluidized bed reaction unit 2, a solid product collecting unit 3, an online quality-improving fixed bed reaction unit 4, a liquid product collecting unit 5, a gas analysis unit 6, a steam reforming unit 8 and an air inlet unit 9 which are connected in sequence, wherein,
the steam reforming unit 9 receives and reforms the non-condensable gas mixture subjected to the hydro-catalytic pyrolysis in the fluidized bed reaction unit 2, and molecular hydrogen generated after reforming enters the gas inlet unit 9;
the air inlet unit 9 is divided into three air paths after passing through an air path switch (not shown), the first air path is communicated with an inlet of the fluidized bed reaction unit 2 through the air preheater 7, the second air path and the third air path are respectively communicated with a biomass bin 11 of the biomass feeding unit 1 and an outlet of a quantitative feeder 12 of the biomass feeding unit 1, and an inlet of the quantitative feeder 12 is communicated with an outlet at the bottom of the biomass bin 11;
the catalyst used in the online upgrading fixed bed reaction unit 4 is a metal-loaded modified carbon-based catalyst, and carbon groups in the modified carbon-based catalyst are derived from solid products collected by the solid product collection unit 3.
In the above manner, the gas inlet unit 9 provides a hydrogen source required by the fluidized bed reaction unit 2 through the gas preheater 7, so as to realize hydrogenation catalytic pyrolysis; the air inlet unit 9 is communicated with the biomass bin 11, so that pressure compensation can be performed on the biomass bin 11, the situation that the pressure in the biomass bin 11 is too low is prevented, and the normal operation of discharging in the biomass bin 11 is ensured; the air inlet unit 9 is communicated with the outlet of the quantitative feeder 12, and can assist in blowing the biomass into the fluidized bed reaction unit 2, improve the speed of the biomass entering the fluidized bed reaction unit 2 from the outlet of the quantitative feeder 12, and prevent the biomass from blocking the outlet of the quantitative feeder 12, so as to influence the normal operation of the whole reaction system.
Through the mode, the biomass is subjected to hydrogenation, pressurization and catalytic pyrolysis to obtain pyrolysis volatile matters with low oxygen content and a solid product-coke, the pyrolysis volatile matters enter the on-line upgrading fixed bed reaction unit 4 to be subjected to deep hydrodeoxygenation reaction, and the vehicle and aviation liquid fuel with high heat value, ultralow acid value and ultralow oxygen content is directly produced. Specifically, the on-line upgrading of the hydrocatalytic pyrolysis and the hydrofining conversion are completely integrated, and the two reaction paths are carried out under the atmosphere pressure of 0-5 MPa. In the process of hydrogenation catalytic pyrolysis, biomass is catalytically converted into biomass pyrolysis volatile matters with low oxygen content in a fluidized bed taking bed materials with the temperature of 350-600 ℃ as catalysts. Hydrogen is the fluidizing gas in the hydrocracking process. After the hydrogenation catalytic pyrolysis, the biochar particles are separated and removed through the solid product collecting unit 3, pyrolysis volatile components directly enter the online quality-improving fixed bed unit 4 to be subjected to the hydrofining conversion online quality-improving process, so that the generation of unstable component condensation and polycondensation and the energy loss caused in the condensation and temperature rise process are avoided, and the process energy consumption and the cost are reduced. On-line upgrading of integrated hydrogenation catalytic pyrolysis coupling can convert oxygen in biomass into H2O and COXHydrogen is added to the reactants to form hydrocarbons while minimizing unwanted acid-catalyzed polymerization, aromatization, coking, and the like. Through the on-line upgrading of the hydrogenation catalytic pyrolysis and the hydrofining conversion, the biomass can be directly converted into the vehicle and aviation liquid fuel with high heat value, ultralow acid value and ultralow oxygen content.
The required online quality-improving catalyst is a metal-loaded modified carbon-based catalyst, the carbon-based catalyst is mainly obtained by modifying biochar obtained by fluidized bed reaction, and the biochar has abundant functional groups on the surface and is a potential raw material for preparing the carbon-based catalyst. Design of biochar by activation modification and surface modificationDue to the physical and chemical properties and the pore structure, the low-cost, high-efficiency and stable hydrodeoxygenation catalyst is obtained by loading specific metal, can be applied to the processes of hydrogenation catalytic pyrolysis, online quality improvement, reforming hydrogen production and the like, can realize comprehensive utilization of all components of biomass, and promotes the biomass to prepare the liquid fuel system for aviation and vehicles to realize economic and green circulation. The hydrogen required by the system can be generated by non-condensable gas mixture (small molecule hydrocarbon (C1-C3 hydrocarbon) and CO generated after pyrolysis2CO, etc.) is introduced into a steam reformer for reforming, and the generated reformed molecular hydrogen is introduced into a fluidized bed reaction unit to participate in the reaction process, so that partial or all self-maintained hydrogen supply can be realized, the aim of self-sufficiency in circulation of the whole hydrogen source of the reaction system is fulfilled, and the efficient cyclic utilization of pyrolysis tail gas is realized.
In a preferred embodiment of the present invention, the biomass feeding unit 1 further includes a feeder 13 and a bridge breaker 14, the bridge breaker 14 is connected to the top of the biomass bin 11, the bridge breaker 14 includes a rotating stirring screw 141 extending into the biomass bin 11 and a plurality of stirring blades 142 distributed in an axial direction of the rotating stirring screw 141, an outlet of the doser 12 is communicated with an inlet of the feeder 13, specifically, an outlet of the doser 12 is communicated with an inlet of the feeder 13 through a pipeline, and an outlet of the feeder 13 is communicated with an inlet of the fluidized bed reaction unit 2.
Through the way, the bridge breaker 14 can fully stir the biomass in the biomass bin 11, and the biomass is regularly and quantitatively supplied to the fluidized bed reaction unit 2 by combining with the quantitative feeder 12, so that the generation of catalytic reaction in the fluidized bed reaction unit 2 is promoted; the feeder 13 can rapidly supply the biomass at the outlet of the doser 12 to the fluidized-bed reaction unit 2, ensuring the proper progress of the pyrolysis reaction in the fluidized-bed reaction unit 2.
Specifically, the biomass silo 11 adopts a set of 20L high-pressure stainless steel silo, the biomass silo 11 is made of 316L stainless steel, and is high-temperature and high-pressure resistant, high in strength, good in corrosion resistance and 5MPa in operating pressure of the biomass silo 11.
The quantitative feeder 12 is used for quantitatively controlling biomass powder, so as to avoid insufficient or excessive supply of biomass into the fluidized bed reaction unit 2, which results in insufficient pyrolysis reaction; the quantitative feeder 12 adopts magnetic coupling sealing, and the quantitative feeding requirement of 50-5000g/h is met.
The feeder 13 is used for rapidly conveying the biomass to the fluidized bed reaction unit 2 from the outlet of the quantitative feeder 12, so as to ensure the supply and reaction rate of the biomass in the fluidized bed reaction unit 2, the feeder 13 is sealed by magnetic coupling, the rotating speed of not less than 500rpm is met, and a water cooling jacket is designed in a high-temperature area of the feeder 13.
The bridge breaker 14 is used for rotationally stirring biomass powder in the biomass bin 11, and is sealed by magnetic coupling, so that the rotating speed of not less than 500rpm is met.
In the embodiment of the present invention, the doser 12 is a screw type doser, the feeder 13 is a screw type conveyor, the bridge breaker 14 is a screw type agitator, and the screw type doser, the screw type conveyor and the screw type agitator are all driven by a stepping motor.
In the preferred embodiment of the present invention, the water cooling jackets are designed inside the quantitative feeder 12, the feeder 13 and the bridge breaker 14 and inside the stepping motor, and are used for dissipating heat of the rotating stirring screw and the stepping motor, maintaining the constant output torque, and ensuring continuous, uniform and stable feeding.
Specifically, the front end and the rear end of the air path of the three air paths are respectively provided with an air filter (not shown in the figure) to prevent solid particles from entering the air path to pollute a valve (not shown in the figure) and an instrument (not shown in the figure); and a check valve (not shown in the figure) and a stop valve (not shown in the figure) are arranged at the downstream of the three air paths to prevent air from channeling.
In a preferred embodiment of the present invention, the downstream of each of the three gas paths is provided with a raw material gas mass flow controller, the raw material gas mass flow controllers are high pressure resistant mass flow controllers, and the gas in the three gas paths can be a majority of gas, such as N2、H2、CH4The gas entering the gas preheater 7 is hydrogen or hydrogen source gas such as methane; furthermore, the bypass design of the three-way raw material gas mass flow controller can quickly purge the system and establish the systemPressure, and the atmosphere is convenient to change; the measuring range is 300NL/min, and the precision meets +/-0.1 percent of F.S. Further, the third gas path is used for assisting the feeder 13 to purge the biomass rapidly, and the flow and pressure of the purge gas can be set independently by adjusting a pressure reducing valve and a gas mass flow controller on the third gas path.
Specifically, the fluidized bed reaction unit 2 includes a fluidized bed reactor and a fluidized bed reactor, the fluidized bed reactor provides the temperature required by the fluidized bed reactor, and the gas passing through the gas preheater 7 enters the fluidized bed reactor from the bottom of the fluidized bed reaction unit 2 through the air distribution plate 21.
The fluidized bed reactor is designed as a high-pressure fluidized bed reactor, the material is 310SS, the operation temperature is RT-700 ℃, and the operation pressure is 0.1-5 MPa. The air distribution plate 21 at the bottom of the fluidized bed reactor adopts a detachable design (graphite sealing), a section of pipeline (not shown in the figure) is reserved at the lower part of the air distribution plate 21 and is used for stabilizing the air flow coming in from the gas preheater 7, preventing the catalyst particles above from falling down and ensuring the good fluidization state in the fluidized bed reaction unit 2, bed materials in the fluidized bed reactor are mainly catalysts with a hydrodeoxygenation effect, including but not limited to catalysts with modified composite alumina as a carrier and carrying molybdenum-tungsten-cobalt-nickel metal components and auxiliaries, transition metal oxide catalysts and the like have excellent hydrogenation activity, and the catalyst has high compression resistance and wear resistance strength, can be recycled, cannot corrode the device, has good stability, long service life and wide application range, and can convert various types of biomass raw materials into pyrolysis volatile components and coke with low oxygen content. A pressure gauge and a differential pressure transmitter are designed at the top end of the fluidized bed reactor, and the differential pressure transmitter is used for monitoring the upper and lower differential pressures in the fluidized bed reactor and monitoring whether the feeding state is stable, uniform and continuous.
The fluidized bed reaction furnace adopts a five-section isothermal electric heating furnace, each section of hearth independently controls the temperature, the enough length of a constant temperature section of a reaction zone is ensured, the temperature programming can be realized, the hearth heat-insulating material adopts a high-temperature-resistant high-density ceramic fiber material, and the heat-insulating effect is good. The shell is isolated by a 304 stainless steel plate to ensure the operation safety; the operation temperature RT-800 ℃ of the heating furnace can be adjusted.
The fluidized bed reactor and the fluidized bed reactor are reaction vessels commonly used in the field, and the structure of the fluidized bed reactor and the fluidized bed reactor is not described in detail herein.
In the preferred embodiment of the present invention, the gas preheater 7 is a high-power spiral high-pressure gas heater, and is heated by a separate heating furnace. The material of the gas preheater 7 adopts 310SS, and the operating pressure: 0.1-5MPa, operating temperature: RT-1000 ℃. The gas preheater 7 meets the requirement that the temperature of the output gas is not lower than 700 ℃, the surface of a downstream pipeline of the gas preheater 8 is provided with a temperature measuring point, and the temperature of the fluidized gas entering the fluidized bed reaction unit 2 is monitored in real time.
Specifically, the solid product collecting unit 3 includes a cyclone 31 and a particulate filter 32, an inlet of the cyclone 31 is communicated with the fluidized-bed reaction unit 2, and an outlet of the cyclone 31 is communicated with the particulate filter 32. The cyclone separator 31 mainly separates larger solid particles in the pyrolysis volatile component flowing out of the fluidized bed unit, and the particle filter 32 mainly filters small solid particles which are not completely separated by the front-stage cyclone separator 31.
By the mode, larger solid particles and small solid particles at the outlet of the fluidized bed reaction unit 2 can be filtered, gas-solid separation of pyrolysis volatile components is realized, and the occurrence of subsequent quality improvement reaction of the pyrolysis volatile components is ensured.
Further, a first collection tank 311 communicating with the cyclone 31 is detachably connected to the bottom of the cyclone 31, and a second collection tank 321 communicating with the particulate filter 32 is detachably connected to the bottom of the particulate filter 32.
Specifically, the larger solid particles entering the cyclone separator 31 enter the first collection tank 311 from the bottom of the cyclone separator 31, the rest of the gas enters the particle filter 32 after passing through a section of electric heat tracing heat preservation pipeline, the pyrolysis volatile matter enters from the side end of the particle filter 32, is filtered by a 5nm ceramic filter column arranged at the upper end outlet of the particle filter 32, enters and exits the fixed bed unit 4 for quality improvement reaction, and the filtered small solid particles fall into the second collection tank 321 after gas-solid separation.
By the mode, the solid particles filtered by the cyclone separator 31 and the particle filter 32 can be collected, the solid particles are biochar, the obtained biochar can be conveniently and subsequently utilized for modification, and the online quality-improving carbon-based catalyst is prepared and is required by an online quality-improving fixed bed, so that the convenience of a system is improved.
Specifically, the online quality-improving fixed bed reaction unit 4 is a high-pressure fixed bed reactor, the material of the high-pressure fixed bed reactor is 316L stainless steel, the operating temperature is RT-800 ℃, and the operating pressure is 0.1-5 MPa. The feeding mode of the high-pressure fixed bed reactor is feeding at the upper end and discharging at the lower end; the upper part of the online upgrading fixed bed reaction unit 4 is provided with a thermocouple sleeve (not shown in the figure), a thermocouple (not shown in the figure) capable of moving up and down is inserted into the sleeve for monitoring the temperature of a catalyst bed layer, and the high-pressure fixed bed reactor is extruded and sealed by a flange plate matched with sealing elements such as graphite and the like. The catalyst used in the high-pressure fixed bed reactor is mainly a hydrofining catalyst which is mainly derived from a composite metal loaded carbon-based catalyst modified by the biochar obtained in the previous stage.
In the preferred embodiment of the invention, all pipelines from the fluidized bed reaction unit 2 to the cyclone separator 31, the cyclone separator 31 to the filter 32, the filter 32 to the online upgrading fixed bed reaction unit 4 are connected by using a large-diameter clamping sleeve, so that the disassembly and the cleaning are convenient, all pipelines are wound with high-temperature heat tracing bands, and the operating temperature is as follows: RT-700 ℃.
The liquid product collecting unit 5 comprises a condenser 51, a primary low-temperature condenser 52, a secondary low-temperature condenser 53, an electric tar supplementing device 54 and a gas filter 55 which are connected in sequence.
Through the mode, the products at the outlet of the online quality-improving fixed bed reaction unit 4 are subjected to multi-stage condensation, and the liquid hydrocarbon products (including water and heavy tar) at the outlet of the online quality-improving fixed bed reaction unit 4 are collected in a grading manner, so that the later-stage resource utilization is facilitated by adopting different utilization modes according to different components.
Specifically, the condenser 51 collects mainly water and a part of heavy tar in the high-temperature product discharged from the fixed-bed catalytic reactor. The condenser 51 is designed in a single-tube type, so that the cleaning and maintenance are convenient, and the condensing medium can be oil or water. The condenser 51 was made of 316L, the operating pressure was 5MPa, and the operating temperature: 0-400 ℃. Further, a collecting bottle 511 is connected to the bottom of the condenser 51 for collecting the gas condensed by the condenser 51.
The primary low-temperature condenser 52 is communicated with the collecting bottle 511, the primary low-temperature condenser 52 mainly comprises a high-pressure impact absorption bottle 521 and a low-temperature tank 522, and the absorption bottle 521 is arranged in the low-temperature tank 522 and mainly collects condensable gases in products. The condensing medium can adopt dry ice acetone or liquid nitrogen, the absorption bottle material adopts 316L, the operating pressure is 5MPa, and the operating temperature is as follows: -196-0 ℃. In order to facilitate the disassembly operation of the absorption bottle, the inlet and the outlet of the absorption bottle are connected by adopting high-pressure corrugated pipes.
The secondary low-temperature condenser 53 has the same structure as the primary low-temperature condenser 52, and the secondary low-temperature condenser 53 mainly collects condensable gases in the product. The condensing medium can adopt dry ice acetone or liquid nitrogen, the absorption bottle material adopts 316L, the operating pressure is 5MPa, and the operating temperature is as follows: -196-0 ℃. In order to facilitate the disassembly operation of the absorption bottle, the inlet and the outlet of the absorption bottle are connected by adopting high-pressure corrugated pipes.
The electrical tar precipitator 54 employs a high voltage electrical precipitator for trapping tar, which includes a tar trapping sleeve 541, a tar collector 542, and a high voltage power supply 543. Wherein the tar collecting sleeve 541 is made of 316L material with the operating pressure of 5MPa, the tar collector 542 is made of 316L material with the operating pressure of 5MPa, the high-voltage power supply can provide 0-500kV adjustable voltage, and the tar collecting sleeve is provided with overload automatic power-off protection.
The gas filter 54 is mainly used for collecting a very small amount of aerosol remaining in the gas, and a filter medium (not shown in the figure) is arranged in the gas filter 54 and comprises a 3A molecular sieve, quartz wool, absorbent cotton, silica gel and the like, so that the purity of the filtered gas can be effectively ensured.
The Gas analysis unit 6 includes a pressure reducing valve 61 and a Micro GC (Gas chromatograph)62, the pressure reducing valve 61 being provided on an outlet line of the Gas filter 54, and the Micro GC being provided on the outlet line of the Gas filter 54. By the mode, gas components entering the micro gas chromatograph can be detected on line, and pyrolysis hydrogenation, catalytic upgrading and catalyst states of the whole reaction system can be monitored in real time.
Specifically, the number of the pressure reducing valves 61 is multiple, the pressure reducing valves 61 are used for controlling gas outlet pressure, a pneumatic back pressure valve 64 is arranged on an outlet pipeline of the gas filter 54, the pneumatic back pressure valve 64 is used for adjusting gas path flow, branch pipes are connected in parallel to two sides of the pneumatic back pressure valve 64, Micro GC are arranged on the branch pipes, and the pressure reducing valves 61 are respectively connected in series to two sides of the Micro GC.
Further, the lower end of the outlet of the pneumatic back pressure valve 64 is also provided with a pressure reducing valve 61 and a flow meter 63 connected with the pressure reducing valve 61 in parallel, and the flow meter 63 counts the gas flow discharged from the outlet pipeline.
The steam reforming unit 8 comprises a reforming reactor, a hydrogen filter membrane, a gas pressure stabilizing tank and a pressurizing device which are sequentially connected, wherein the inlet of the reforming reactor is communicated with the outlet of the gas analysis unit 6, and the outlet of the pressurizing device is communicated with the inlet of the gas inlet unit 9.
In particular, the reforming reactor is mainly used for the light gases (C1-C3 hydrocarbon and CO, CO) generated after the reaction2) Reforming to produce hydrogen to supply hydrogen needed by hydropyrolysis and on-line upgrading reaction. The hydrogen filter membrane is mainly used for selectively filtering the reformed gas to remove residual gases such as CO2 and CO. The gas surge tank is mainly used for storing hydrogen sources, including but not limited to hydrogen, methane, natural gas and the like, and supplying the hydrogen sources required by the fluidized bed reaction unit 2, and if the hydrogen sources are not stored enough, the hydrogen sources can be supplemented through an external gas cylinder or a pipeline. The pressurizing means is mainly operated to pressurize the gas entering the gas intake unit 9, the operating pressure: 0-10Mpa to ensure the stable gas pressure in the system.
The tail end of the system (the outlet pipeline of the gas filtering tank 55) is provided with a pneumatic back pressure valve 64, after rated gas flow and device pressure are set, the valve of the pneumatic back pressure valve 64 is closed, the system is boosted, after the rated pressure is reached, the pneumatic back pressure valve 64 is opened, redundant pressure is released, and the internal pressure of the system is maintained to be stable.
The system of the invention involves a plurality of sub-units, each of which is specially designed to ensure stable operation under pressurized conditions. Specifically, the biological feeding unit 1 adopts a magnetic coupling sealing structure, so that the air tightness of a moving structure is ensured; the position department of the top apron A of living beings feed bin 11 adopts the tetrafluoro packing ring to add ring flange connection structure, fluidized bed reaction unit 2's top B position department adopts bulb-conical surface seal structure, 800 ℃ of resistant high temperature, convenient dismantlement, and be convenient for load fluidized bed material (catalyst), fluidized bed reaction unit 2's bed upper end adopts the cutting ferrule structure, connect differential pressure transmitter (not shown in the figure), fluidized bed reaction unit 2's below C position department adopts silica gel pad thread sealing mode, install metal block isolation furnace body high temperature additional in the middle of bottom screw thread and the grid plate 21, guarantee silica gel pad thread sealing structure's durability.
In order to ensure continuous, uniform and stable feeding in the system operation process, a pipeline D position between the outlet of the quantitative feeder 12 and the inlet of the feeder 13 is sealed by a silica gel pad thread, so that the feeding condition is convenient to disassemble and observe;
furthermore, a metal winding gasket flange sealing structure is adopted at the position E at the upper end of the fixed bed reaction unit 4, and the fixed bed reaction unit can resist the high temperature of 500 ℃. The position F at the lower end of the fixed bed reaction unit 4 adopts a silica gel pad flange sealing structure and resists high temperature of 150 ℃.
The joints of the liquid product collecting unit 5 are all in a silica gel gasket thread sealing structure, the upper end and the lower end of the electric tar precipitator 54 are both in a tetrafluoro gasket flange sealing structure, and the rest joints of the system are all in a clamping sleeve connecting structure.
The biomass integrated hydrogenation, pressurization, catalytic pyrolysis and online upgrading coupled system for directly preparing liquid fuel is specifically described above, and the working process is described below.
The air inlet unit 9 is mainly divided into three paths, a first air path enters the air preheater 7 to be preheated, a second air path is communicated with an inlet at the top of the biomass bin 11 and used for supplementing pressure to the biomass bin 11, a third air path is communicated with the upper end of an outlet of the quantitative feeder 12, and air-assisted purging is carried out on the biomass material entering the feeder 13. After the gas pressure is adjusted to a set value, the feeder 13, the quantitative feeder 12 and the bridge breaker 14 are started, the bridge breaker 14 performs rotary vibration on the biomass powder in the biomass bin 11, the quantitative feeder 12 performs quantitative output on the biomass powder from the biomass bin 11, and the feeder 13 rapidly conveys the biomass powder to the fluidized bed reaction unit 2.
The catalyst bed material is added into the fluidized bed reaction unit 2 before the device operates, the catalyst bed material is spherical, the gas (carrier gas) in the gas preheater 7 enters the fluidized bed reaction unit 2 after being preheated to a set temperature, the gas is heated to the set temperature, the gas and the catalyst bed material form a stable and uniform fluidized state after passing through the air distribution plate 21, and the carrier gas flow ensures that the catalyst bed material is not blown out. The biomass raw material enters a fluidized bed reactor to fully contact and react with catalyst bed materials and carrier gas to generate biomass pyrolysis volatile matters and coke with low oxygen content.
Under the carrying of carrier gas, reaction products are wrapped into the cyclone separator 31, large-particle solid coke is separated and is deposited into the first collecting tank 311 below, other products are continuously carried into the particle filter 32 by the carrier gas, small-particle coke is filtered by a ceramic filter column in the particle filter and then falls into the second collecting tank 321 below, and after gas-solid separation, low-oxygen content biomass pyrolysis volatile matter continuously enters and exits the online quality-improving fixed bed reaction unit 4 for quality-improving reaction; the filtered coke particles can be modified to obtain the supported metal modified carbon-based catalyst.
The catalyst in the online quality-improving fixed bed reaction unit 4 is placed in a bed in advance before reaction and is mainly a columnar hydrofining catalyst, the columnar hydrofining catalyst is mainly a biochar-based catalyst obtained in the fluidized bed reaction unit 2 after being modified by biochar, and biomass pyrolysis volatile matters with low oxygen content are subjected to quality-improving reaction with the hydrofining catalyst in the online quality-improving fixed bed reaction unit 4 to generate a completely deoxidized hydrocarbon product.
The product and carrier gas enter a condenser 51 to trap heavy tar and water phase, enter a primary low-temperature condenser 52 and a secondary low-temperature condenser 53 to trap condensable gas, enter an electric tar supplementing device 54 to trap residual tar, and enter a gas filter tank 55 to trap residual aerosol substances.
And a small part of the non-condensable gas after reaction condensation enters a Micro GC to be analyzed in gas components, and the state and the reaction activity of the hydropyrolysis and the catalyst are monitored in real time. The remaining non-condensable gases (mainly C1-C3 hydrocarbons and CO)2CO) enters a reforming reactor to be reformed to produce hydrogen, then enters a hydrogen filter membrane, and the reformed gas is selectively filtered to remove the residual CO2And CO and other gases enter a gas pressure stabilizing tank for storage, the gas pressure stabilizing tank can supply hydrogen sources required by the reaction device and maintain a certain pressure, and if the gas storage is insufficient, the gases can be supplemented through an external gas bottle or a pipeline. The gas from the gas pressure stabilizing tank is pressurized and output through the pressurizing device, and the stability of the gas pressure required in the system is ensured.
The high-value hydrocarbon products collected after the reaction can be directly separated into vehicle and aviation liquid fuels or used as additive components of the vehicle and aviation liquid fuels.
Test example
Raw material, 100 meshes of poplar powder; atmosphere, hydrogen, pressure 3 MPa; fluidized bed material, 40-60 mesh spherical alumina supported nickel molybdenum catalyst; a quality-improving catalyst, namely a 3mm columnar biochar loaded copper-nickel-molybdenum-carbon-based catalyst; the pyrolysis temperature of the fluidized bed reaction unit is 450 ℃; the quality improvement temperature of the fixed bed reaction unit is 380 ℃; the temperature of the condenser is 5 ℃, the primary low-temperature condensation temperature is-170 ℃; secondary low temperature condensation temperature, -170 ℃; the voltage is compensated electrically, 50 kV.
Based on the biomass feeding amount, the obtained product contains 30 wt% of liquid hydrocarbons, 9 wt% of biochar, 17 wt% of water and 44 wt% of gas. The liquid products were analyzed by tests, and the products were mainly n-pentane, n-heptane, butane, cyclohexane, octane, benzene, toluene, cyclopentane, p-xylene, methylcyclopentane, 2-methylhexane, 2, 3-dimethylpentane, methylcyclohexane, 2-methylheptane, ethylbenzene, p-xylene, 1-ethyl-3-methylbenzene, etc. Total Acid Number (TAN) of the whole hydrocarbon product is less than 0.2, and oxygen content is less than 0.1 wt%. The system is proved to be capable of directly producing the liquid fuel for vehicles and aviation with high heat value, ultralow acid value and ultralow oxygen content.
The present invention is not limited to the above preferred embodiments, and any modifications, equivalent substitutions and improvements made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A biomass integrated hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading direct liquid fuel preparation system is characterized by comprising: a biomass feeding unit, a fluidized bed reaction unit, a solid product collecting unit, an online quality-improving fixed bed reaction unit, a liquid product collecting unit, a gas analysis unit, a steam reforming unit and an air inlet unit which are connected in sequence, wherein,
the steam reforming unit receives and reforms the non-condensable gas mixture subjected to the hydrogenation catalytic pyrolysis by the fluidized bed reaction unit, and molecular hydrogen generated after reforming enters the air inlet unit;
the air inlet unit is divided into three air paths after passing through an air path switch, a first air path is communicated with an inlet of the fluidized bed reaction unit, a second air path and a third air path are respectively communicated with a biomass bin of the biomass feeding unit and an outlet of a quantitative feeder of the biomass feeding unit, and an inlet of the quantitative feeder is communicated with an outlet at the bottom of the biomass bin;
the catalyst used in the online upgrading fixed bed reaction unit is a metal-loaded modified carbon-based catalyst, and carbon groups in the modified carbon-based catalyst are derived from solid products collected by the solid product collection unit.
2. The system for directly preparing liquid fuel through online upgrading coupled with biomass integrated hydrogenation, pressurization, catalytic pyrolysis and coupling as claimed in claim 1, wherein the biomass feeding unit further comprises a feeder and a bridge breaker, the bridge breaker is connected with the top of the biomass bin, the bridge breaker comprises a rotary stirring screw extending into the biomass bin and stirring blades distributed in the axial direction of the rotary stirring screw, an outlet of the doser is communicated with an inlet of the feeder, and an outlet of the feeder is communicated with an inlet of the fluidized bed reaction unit.
3. The biomass-integrated hydropressing catalytic pyrolysis coupled online upgrading direct liquid fuel production system according to claim 1, wherein the solid product collection unit comprises a cyclone separator and a particle filter, an inlet of the cyclone separator is communicated with an outlet of the fluidized bed reaction unit, a top outlet of the cyclone separator is communicated with a top inlet of the particle filter, a first collection tank communicated with the cyclone separator is detachably connected to the bottom of the cyclone separator, and a second collection tank communicated with the particle filter is detachably connected to the bottom of the particle filter.
4. The biomass integrated hydrogenation pressurized catalytic pyrolysis coupled online upgrading direct liquid fuel preparation system according to claim 1, wherein the liquid product collection unit comprises a condenser, a primary low-temperature condenser, a secondary low-temperature condenser, an electric tar supplementing device and a gas filter which are connected in sequence.
5. The system for directly preparing the liquid fuel by coupling biomass integration hydrogenation, pressurization, catalytic pyrolysis and online upgrading as claimed in claim 4, wherein the gas analysis unit comprises a pressure reducing valve and a micro gas chromatograph, the pressure reducing valve is arranged on an outlet pipeline of the gas filter, and the micro gas chromatograph is arranged at the lower end of the pressure reducing valve.
6. The system for directly preparing the liquid fuel by coupling biomass integration hydrogenation pressurized catalytic pyrolysis with online upgrading as claimed in claim 1, wherein the steam reforming unit comprises a reforming reactor, a hydrogen filter membrane, a gas surge tank and a pressurizing device which are connected in sequence, an inlet of the reforming reactor is communicated with an outlet of the gas analysis unit, and an outlet of the pressurizing device is communicated with an inlet of the gas inlet unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110995177.XA CN113648937A (en) | 2021-08-27 | 2021-08-27 | System for directly preparing liquid fuel by biomass integrated hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110995177.XA CN113648937A (en) | 2021-08-27 | 2021-08-27 | System for directly preparing liquid fuel by biomass integrated hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113648937A true CN113648937A (en) | 2021-11-16 |
Family
ID=78493088
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110995177.XA Pending CN113648937A (en) | 2021-08-27 | 2021-08-27 | System for directly preparing liquid fuel by biomass integrated hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113648937A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113999697A (en) * | 2021-11-29 | 2022-02-01 | 上海交通大学 | Device and method for improving quality of bio-oil by using Fe/Ni bimetallic modified ZSM-5 catalyst |
| CN115463613A (en) * | 2022-10-20 | 2022-12-13 | 浙江大学 | Vertical multifunctional fixed bed device capable of quickly and controllably reacting at high temperature and high pressure |
| CN115779632A (en) * | 2022-12-01 | 2023-03-14 | 华中科技大学 | Charcoal capture CO 2 Method and system for preparing combustible gas by coupling photo-thermal catalytic conversion |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101624531A (en) * | 2009-08-06 | 2010-01-13 | 东南大学 | Device for preparing bio-oil by utilizing biomass spouted fluidized bed through pyrolysis and fractional condensation |
| CN102378748A (en) * | 2009-04-07 | 2012-03-14 | 瓦斯技术研究所 | Hydropyrolysis of biomass for producing high quality liquid fuels |
| CN113214856A (en) * | 2021-04-26 | 2021-08-06 | 浙江大学 | Biomass catalytic pyrolysis coupled reaction device for preparing liquid fuel by online upgrading |
-
2021
- 2021-08-27 CN CN202110995177.XA patent/CN113648937A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102378748A (en) * | 2009-04-07 | 2012-03-14 | 瓦斯技术研究所 | Hydropyrolysis of biomass for producing high quality liquid fuels |
| CN101624531A (en) * | 2009-08-06 | 2010-01-13 | 东南大学 | Device for preparing bio-oil by utilizing biomass spouted fluidized bed through pyrolysis and fractional condensation |
| CN113214856A (en) * | 2021-04-26 | 2021-08-06 | 浙江大学 | Biomass catalytic pyrolysis coupled reaction device for preparing liquid fuel by online upgrading |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113999697A (en) * | 2021-11-29 | 2022-02-01 | 上海交通大学 | Device and method for improving quality of bio-oil by using Fe/Ni bimetallic modified ZSM-5 catalyst |
| CN115463613A (en) * | 2022-10-20 | 2022-12-13 | 浙江大学 | Vertical multifunctional fixed bed device capable of quickly and controllably reacting at high temperature and high pressure |
| CN115779632A (en) * | 2022-12-01 | 2023-03-14 | 华中科技大学 | Charcoal capture CO 2 Method and system for preparing combustible gas by coupling photo-thermal catalytic conversion |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113648937A (en) | System for directly preparing liquid fuel by biomass integrated hydrogenation, pressurization, catalytic pyrolysis and on-line upgrading | |
| US8541637B2 (en) | Process and system for thermochemical conversion of biomass | |
| RU2535343C2 (en) | Biomass hydrolysis for obtaining high quality liquid fuel | |
| US8492600B2 (en) | Hydropyrolysis of biomass for producing high quality fuels | |
| Bridgwater | Review of fast pyrolysis of biomass and product upgrading | |
| JP7220021B2 (en) | Co-treatment and its products for the control of hydropyrolysis processes | |
| US9447328B2 (en) | Hydropyrolysis of biomass for producing high quality liquid fuels | |
| CA2959802C (en) | Use of carbon dioxide generated by hydropyrolysis for process inertization | |
| CN101107056A (en) | Control of hydrogen in hydrogen-containing streams from hydrogen sources | |
| CN110511776B (en) | Device and method for producing biodiesel through biomass pyrolysis | |
| Kaur et al. | Commercial or pilot-scale pyrolysis units for conversion of biomass to bio-oils: state of the art | |
| Amin et al. | In situ catalytic pyrolysis of low-rank coal for the conversion of heavy oils into light oils | |
| CN102268291B (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| US11198820B2 (en) | Conversion process for an organic material | |
| CN116004279A (en) | Hydrogen production and CO enrichment from hydrocarbon raw materials 2 Is a method of (2) | |
| CN116002614A (en) | Hydrogen production method by using inferior heavy oil | |
| CN109749758B (en) | Tar quality improvement treatment method | |
| CN110511773B (en) | Device and method for coupling biomass pyrolysis and catalytic cracking reaction | |
| US20150051427A1 (en) | Integrated process for the production of renewable drop-in fuels | |
| RU2674158C1 (en) | Installation for producing liquid hydrocarbons from biomass | |
| CN116879342A (en) | Testing device for directional production of target product by catalytic pyrolysis gasification of carbon-based fuel pressurized fluidized bed coupled fixed bed | |
| WO2023247759A1 (en) | A process for stabilization of an unstable raw hydrocarbonaceous product | |
| CN116002616A (en) | Method and device for producing hydrogen from hydrocarbons | |
| LL et al. | 97101799 Mechanism of transformations of model hetero-cyclic compounds in hydrorefining reactions | |
| WO2010024792A1 (en) | Reformer for converting biomass into synthesis gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20211116 |
|
| RJ01 | Rejection of invention patent application after publication |