CN115521803A - Method for continuous hydrothermal treatment of organic waste - Google Patents
Method for continuous hydrothermal treatment of organic waste Download PDFInfo
- Publication number
- CN115521803A CN115521803A CN202110707722.0A CN202110707722A CN115521803A CN 115521803 A CN115521803 A CN 115521803A CN 202110707722 A CN202110707722 A CN 202110707722A CN 115521803 A CN115521803 A CN 115521803A
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- China
- Prior art keywords
- organic waste
- tubular reactor
- water
- supercritical water
- reactor
- Prior art date
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- 239000010815 organic waste Substances 0.000 title claims abstract description 103
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000010335 hydrothermal treatment Methods 0.000 title claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 95
- 239000002002 slurry Substances 0.000 claims abstract description 34
- 239000007787 solid Substances 0.000 claims abstract description 31
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000010779 crude oil Substances 0.000 claims abstract description 26
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 15
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 15
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 15
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 48
- 239000007788 liquid Substances 0.000 claims description 36
- 238000000926 separation method Methods 0.000 claims description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- 239000001301 oxygen Substances 0.000 claims description 16
- 229910052760 oxygen Inorganic materials 0.000 claims description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 229930195733 hydrocarbon Natural products 0.000 claims description 8
- 150000002430 hydrocarbons Chemical class 0.000 claims description 8
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 4
- 239000003570 air Substances 0.000 claims description 4
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 claims description 2
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 claims description 2
- 239000005751 Copper oxide Substances 0.000 claims description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 claims description 2
- 229910000431 copper oxide Inorganic materials 0.000 claims description 2
- SZVJSHCCFOBDDC-UHFFFAOYSA-N ferrosoferric oxide Chemical compound O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 claims description 2
- 235000019253 formic acid Nutrition 0.000 claims description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 2
- 239000012528 membrane Substances 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 2
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims description 2
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 2
- 229910000027 potassium carbonate Inorganic materials 0.000 claims description 2
- 229910052814 silicon oxide Inorganic materials 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 claims description 2
- 239000010457 zeolite Substances 0.000 claims description 2
- 239000011787 zinc oxide Substances 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- 238000004821 distillation Methods 0.000 claims 1
- 239000002904 solvent Substances 0.000 claims 1
- 230000032258 transport Effects 0.000 claims 1
- 238000002309 gasification Methods 0.000 abstract description 9
- 238000001027 hydrothermal synthesis Methods 0.000 abstract description 7
- 239000007864 aqueous solution Substances 0.000 abstract description 5
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- -1 syngas Substances 0.000 abstract 1
- 239000002028 Biomass Substances 0.000 description 21
- 238000011282 treatment Methods 0.000 description 16
- 239000010813 municipal solid waste Substances 0.000 description 15
- 239000003921 oil Substances 0.000 description 15
- 239000010802 sludge Substances 0.000 description 10
- 238000007599 discharging Methods 0.000 description 9
- 239000002699 waste material Substances 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 239000003245 coal Substances 0.000 description 6
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- 238000001035 drying Methods 0.000 description 6
- 238000010248 power generation Methods 0.000 description 6
- 238000003860 storage Methods 0.000 description 6
- 239000002689 soil Substances 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000003610 charcoal Substances 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 4
- 239000002361 compost Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000006188 syrup Substances 0.000 description 3
- 235000020357 syrup Nutrition 0.000 description 3
- 238000004227 thermal cracking Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 238000009264 composting Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000010806 kitchen waste Substances 0.000 description 2
- 239000002906 medical waste Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000003809 water extraction Methods 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 238000009360 aquaculture Methods 0.000 description 1
- 244000144974 aquaculture Species 0.000 description 1
- 239000012075 bio-oil Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000013072 incoming material Substances 0.000 description 1
- 239000010871 livestock manure Substances 0.000 description 1
- 238000003754 machining Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 235000010446 mineral oil Nutrition 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 238000009284 supercritical water oxidation Methods 0.000 description 1
- 239000010913 used oil Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Images
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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- 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
- C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
-
- 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
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
-
- 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
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
-
- 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
- C10J3/72—Other features
-
- 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
- C10G2300/1003—Waste materials
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/0923—Sludge, e.g. from water treatment plant
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0926—Slurries comprising bio-oil or bio-coke, i.e. charcoal, obtained, e.g. by fast pyrolysis of biomass
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Processing Of Solid Wastes (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention discloses a method for continuously hydrothermally treating organic waste, which comprises the following steps: the organic waste is first comminuted and then mixed with water to form a pumpable organic waste slurry. The organic waste slurry is then injected into the tubular reactor by a high pressure pump. In the pipe reactor, the organic waste slurry is converted into crude oil, synthesis gas, organic waste solids insoluble to supercritical water, and remaining aqueous solution as organic waste through hydrothermal reaction or hydrothermal oxidation reaction. The organic waste crude oil, syngas, and organic waste solids can be used for gasification to produce more syngas. The syngas, biocrude, may also be collected, separated for downstream use and carbon dioxide capture.
Description
Technical Field
The invention relates to a method for continuous hydrothermal treatment of organic waste. The main application is to perform harmless treatment on organic wastes, particularly organic wastes with high water content, and convert the organic wastes into fuels.
Background
With the increasing emphasis on sustainable development and ecological civilization construction, environmental protection and carbon neutralization in China, the demand of the whole society on resource utilization of the existing garbage, particularly organic waste, is more and more urgent. However, the existing organic waste garbage disposal technology still has no way to meet the requirement of environmental protection in China.
The organic waste treatment available in agriculture in China mainly comprises treatment methods of feed, compost, methane, biomass dry granular fuel and the like. At present, the methods can not meet the higher environmental protection requirements of China more and more. In fact, most of the biogas residues and biogas slurry remained at the end of the biogas process are difficult to be utilized by farmers (the biogas residues and biogas slurry are not well applied and hardly reach the national standard of organic fertilizers), so that secondary pollution is caused. The odor pollution of the compost and the aerobic aeration and the emission of methane and carbon dioxide are not low, and the compost and the aerobic aeration are difficult to collect. The organic waste dry particles need drying and energy consumption, and if a special boiler and tail gas treatment equipment are not available, the standard of directly burning oxynitride can be exceeded.
For municipal solid waste (especially kitchen waste), medical waste, sewage plant sludge, river sludge, aquaculture sludge and other organic waste garbage with extremely high water content cannot be directly used for incineration or power generation, and can be solved only by means of landfill, composting and thermal cracking. And a large amount of waste gas is generated in landfill and composting, so that secondary pollution is caused. The thermal cracking process has very high requirements on the incoming materials, otherwise the energy consumption is too high.
The organic wastes produced by industries are also very numerous, such as oil exploitation, petrochemical industry and the like, and a large amount of waste oil sludge is produced every year; the machining industry has a large number of used oils, emulsions, etc. every year. In the face of the organic wastes, many of the organic wastes belong to hazardous wastes, and the organic wastes are usually directly discharged or discarded in the past. This is conventionally because of the difficulty and cost of organic waste treatment.
In conclusion, the development of a technical scheme for reducing, recycling and harmlessly treating organic wastes is urgently needed in China, and meanwhile, the technical scheme is more energy-saving and environment-friendly and has a higher output added value.
The bottleneck in utilizing organic waste, particularly organic solid waste, is often high water content. For organic wastes with higher water content and relatively lower calorific value, direct incineration, thermal cracking and direct gasification consume a large amount of heat in the latent heat of steam, resulting in a reduction in the amount of high grade calorific value that can be truly utilized. The garbage classification can greatly reduce the water content of partial garbage, thereby increasing the heat value of the partial garbage, and reducing the treatment cost of garbage incineration and garbage power generation. This is also the reason why China has been always striving to push garbage classification. However, for some organic wastes with high water content (> 80%), mechanical dehydration is difficult to directly reduce the water content to below 60%, and mechanical dehydration is only possible to reduce the water content to below 40% after drying or fermentation. Therefore, it is difficult to treat such garbage without additional use of energy by ordinary incineration or garbage power generation. Therefore, after the high-humidity garbage is subjected to anaerobic fermentation, the biogas is used for power generation, and the treated residues are used for incineration. This method is however slow to process.
One new direction for the utilization of high-humidity organic waste is to utilize biomass oil formed by hydrothermal carbonization and biomass oil formed by hydrothermal liquefaction and synthesis gas generated by hydrothermal supercritical gasification. Compared with other treatment methods, the hydrothermal method can utilize organic waste without dehydration, and can save a large amount of drying energy while generating economic products such as biomass oil, biochar, synthesis gas and the like, so that the hydrothermal method is widely researched. However, the prior proposed processes of this type still have some problems, such as: although the treatment process does not require dehydration, a large amount of water in the high-humidity waste still needs to be heated; although the wet waste is reduced, the separation of the biomass oil and the hydrothermal residual water solution still have the possibility of generating pollutants.
The product yields for different wet waste feedstocks are not consistent. Since the hydrothermal method usually requires a high-temperature and high-pressure reactor, the cost of the reactor is increased dramatically due to the excessively long treatment time, the excessively high reaction temperature and the excessively slow treatment speed. Moreover, the existing research mostly focuses on how to improve the conversion rate of a certain product of a certain raw material, and the practicability of the process parameters is very limited and the universality is lacked.
From the market perspective, the bio-oil, the bio-char and the syngas produced by the hydrothermal process studied by the academia at present are not products that can be directly sold as commodities, and often need to be subjected to additional processing, treatment or conversion to be products that can be sold in the market. The biomass oil has high nitrogen and sulfur contents and can be used as fuel after being treated by methods such as hydrogenation and the like. The biochar also needs to be extracted and eluted to be used as an organic carbon fertilizer or an adsorbent.
Although the hydrothermal method for treating organic waste still has many defects, the moisture content of the wet waste product can be greatly reduced by only utilizing some characteristics of the hydrothermal method, so that the wet waste product can be treated as peat and coal with lower heat value. The subsequent comprehensive utilization modes of coal are very many. For example, after the moisture content of the high-humidity garbage is reduced, the high-humidity garbage can be normally incinerated to generate electricity. Or the biomass coal is converted into biological coke and synthesis gas, is applied to coal chemical industry, steel industry, IGCC (integrated gasification combined cycle power generation system) and the like, replaces the existing coal, and reduces carbon emission. Therefore, it is recognized that the key to the high humidity waste treatment is the dehydration reduction while avoiding the drying heat in the hydrothermal treatment of organic waste.
Supercritical water is water in which the density of water expanded by high temperature and the density of water vapor compressed by high pressure are exactly the same when the gas pressure and temperature reach a certain value. At this time, the liquid and the gas of water are not distinguished from each other and are completely mixed together, and a new fluid in a high-pressure and high-temperature state is obtained. There is a great difference in the density between supercritical water and subcritical water (supercritical water density at 400 c and 23Mpa is about one-seventh at normal temperature). Because there is no latent heat of vaporization, supercritical water can be converted to liquid water by releasing less heat. Thus, the supercritical fluid can be completely liquefied by using the material to be heated, and the liquefied supercritical fluid does not need to be cooled by external circulating water. The characteristics can be fully utilized to reduce the water in the solid matter, and simultaneously, the drying heat is reduced, and the heat exchange efficiency is improved.
However, supercritical water is not limited to dehydration for the treatment of organic waste. The supercritical water temperature is higher, and organic matters can be gasified into synthesis gas and biomass oil can be upgraded. The supercritical water has high enthalpy and can directly participate in biomass charcoal gasification as steam. Supercritical water drying can reduce the free water content of the biomass charcoal to below 5%. In addition, when the organic matter content in supercritical water or subcritical water reaches a certain concentration, oxidant such as oxygen is introduced, and the organic matter is hydrolyzed, oxidized and released heat. Based on the characteristic, the supercritical water oxidation and the subcritical water oxidation can realize the autothermal continuous reaction by adding the oxidant without external heating and additional energy consumption.
Disclosure of Invention
The object of the present invention is to provide a method for continuous hydrothermal treatment of organic waste, which is simple in operation process, can treat organic waste, especially organic waste with high water content, harmlessly, and can recover fuel by recycling the organic waste.
In order to achieve the purpose, the technical scheme adopted by the invention comprises the following steps:
in a first step, the organic waste is comminuted and then mixed with water to form a pumpable organic waste slurry.
The organic waste comprises urban organic waste, such as household kitchen waste, medical waste, sludge of sewage treatment plants, sludge of rivers and lakes and activated carbon which is saturated by adsorption; agricultural organic waste such as straw, rice hulls, biogas residue, pond culture sludge, and livestock manure; industrial organic waste, such as oil sludge.
The organic waste slurry can contain a catalyst, which comprises one or a combination of more of sodium hydroxide, potassium hydroxide, calcium hydroxide, sodium carbonate, potassium carbonate, calcium carbonate, formic acid, acetic acid, sulfuric acid, ferric chloride, zinc oxide, copper oxide, ferric oxide, ferroferric oxide, aluminum oxide, titanium oxide, silicon oxide, nickel oxide, molecular sieves and zeolite.
In the second step, the organic waste slurry is injected into the tubular reactor by a high pressure pump.
The pressure in the tubular reactor is 22.1MPa higher than the critical pressure of water, and the temperature in the high-temperature area is 374.3 ℃ higher than the critical temperature of water.
Organic waste slurries that can be pumped can increase slurry solids by decreasing the viscosity by increasing the temperature.
And thirdly, one end of the tubular reactor, which is injected into the organic waste slurry, is a low-temperature region, gas generated in the organic waste slurry and organic waste solids which cannot be dissolved are discharged from the other end of the tubular reactor, and the organic waste solid and gas discharge end is a high-temperature region.
The heat of the high-temperature area comes from a heating device outside the tubular reactor or is generated by the reaction of high-pressure air, oxygen and hydrogen peroxide injected into the tubular reactor and organic waste.
The high pressure oxygen, air and hydrogen peroxide can be injected into the tubular reactor together with the organic waste slurry, can also be injected into the moving bed or fluidized bed reactor together with the supercritical water mentioned in the sixth step, and can also be directly injected into the tubular reactor through a pipeline.
And fourthly, conveying the organic waste slurry from the low-temperature area at one end of the tubular reactor to the high-temperature area at the other end of the tubular reactor by a spiral feeding device in the tubular reactor.
Due to the presence of the high temperature zone and the low temperature zone, a temperature gradient exists in the tubular reactor. The direction of the screw feed is consistent with the direction of the temperature rise, and the speed of the screw feed determines the rate of heating of the organic waste solids. The spiral feeding device can be used for stirring besides conveying organic waste solids, so that the radial convection heat exchange effect of the tubular reactor is increased, and the axial convection effect of the tubular reactor is reduced. The spiral can increase the solid content proportion in the space of the high-temperature area in the tubular reactor by gradually reducing the pitch from the low-temperature area to the high-temperature area.
And fifthly, in the process of conveying the organic waste slurry from the low-temperature area to the high-temperature area, the organic waste is gradually subjected to hydrolysis, cracking, polymerization and other reactions to generate water-soluble substances and crude oil of the organic waste, and the water-soluble substances and the crude oil of the organic waste are dehydrated, carbonized, changed into solid organic waste and gasified to be changed into synthesis gas.
The organic waste crude oil is partially soluble in high temperature subcritical water and supercritical water. In addition to supercritical water, the syngas generated here is mostly carbon dioxide, the rest being hydrogen, carbon monoxide, methane and other hydrocarbons.
And sixthly, discharging the water-soluble organic matters and part of the crude oil of the organic waste in the tubular reactor out of the tubular reactor from a liquid outlet of the low-temperature area of the tubular reactor, and conveying the organic waste solids to a discharge outlet of the high-temperature area to discharge the organic waste solids out of the tubular reactor.
The included angle between the local area of the tubular reactor and the horizontal plane is larger than 5 degrees, so that a liquid state interface and a supercritical state interface of water in the tubular reactor form a liquid seal, and the liquid seal interface ensures that supercritical water and synthesis gas cannot be discharged from a liquid outlet of a low-temperature area.
The organic waste solid can be connected with a moving bed reactor or a fluidized bed reactor at the discharge port of the tubular reactor, and the organic waste solid enters the lower part of the moving bed reactor or the fluidized bed reactor and is discharged; supercritical water is discharged from the lower part of the moving bed or fluidized bed reactor into the upper part and then enters the tubular reactor.
Supercritical water injected from the lower part performs a counter-current extraction of organic waste solids in a moving bed or fluidized bed reactor. The main purpose is to extract soluble or cleavable hydrocarbon adsorbed on the surface of the organic waste solid, and reduce the content of mineral oil in the organic waste solid which can be extracted by an organic solvent at normal temperature. The organic waste solids subjected to supercritical water extraction can be directly and safely disposed of, used as an adsorbent or used as solid fuel like coal.
The discharged liquid from the low-temperature area may contain a large amount of particles, and the discharged liquid can be filtered by adopting filtering equipment such as a stacked spiral sludge dewatering machine and a high-pressure automatic back-flushing filtering station, so that a large amount of unreacted organic waste is prevented from directly flowing out of the tubular reactor. The aqueous solution containing water-soluble organic matter in the discharged liquid and the crude oil of organic waste can be separated by liquid separation and extraction. The organic waste crude oil is available for downstream use. The aqueous solution may be treated by conventional water treatment means.
And seventhly, discharging the rest of the synthesis gas, the supercritical water and the supercritical water solute together from a certain discharge port in the high-temperature area of the tubular reactor.
And discharging the supercritical water, the synthesis gas and the supercritical water solute out of the tubular reactor at a pressure higher than 5Mpa, filtering, performing heat exchange, condensing, and separating water, liquid carbon dioxide, organic waste crude oil and non-condensable gas in the mixture.
The main reason why the supercritical water, the synthesis gas and the supercritical water solute are cooled at a pressure of more than 5Mpa is to liquefy the carbon dioxide by cooling the carbon dioxide to normal temperature. Because the viscosity of gas is much lower than that of liquid, gas filtration is much easier than liquid filtration. Under high pressure conditions, water, carbon dioxide, and crude organic waste oil are in liquid form and can be separated from non-condensable gases (e.g., hydrogen, methane, carbon monoxide, etc.) in a gas-liquid separation process. The solubility of water, carbon dioxide and organic waste solid crude oil is limited under certain temperature condition, and the organic waste solid crude oil can be separated by liquid separation.
And separating the carbon dioxide, methane, hydrogen, nitrogen, oxygen, carbon monoxide and hydrocarbon from the liquid carbon dioxide and the non-condensable gas by cooling, rectification, chemical adsorption, pressure swing adsorption and gas membrane separation.
In addition to directly collecting supercritical water, syngas, and supercritical water solubles discharged from the pipe reactor, the organic waste solids, supercritical water, syngas, and supercritical water solubles may be introduced into the gasifier together with oxygen or air to generate syngas.
The treatment mode can solve the problem of overhigh nitrogen and sulfur contents in the crude oil of the organic waste, and the obtained synthetic gas can be treated in a gaseous state by adopting the existing desulfurization and denitrification device. Compared with hydrocracking, the direct gasification has lower cost. Gasification can yield more syngas when the organic waste solids contain more fixed carbon.
Drawings
Fig. 1 is a schematic flow chart of the principle of embodiment 1 of the present invention.
Fig. 2 is a schematic flow chart of embodiment 2 of the present invention.
Fig. 3 is a schematic flow chart of embodiment 3 of the present invention.
Detailed Description
In order that those skilled in the art will better understand the technical solutions of the present invention, the present invention will be further described in detail with reference to the following embodiments.
Example 1
The soil contaminated by the crude oil production process is mixed with a suitable amount of water in a 101-agitator tank to form a pumpable slurry of oil, which is heated to 80 ℃. The slurry was injected into a 105-tube reactor through a 102 high pressure diaphragm pump at a pressure of 24MPa. The oil sludge is threaded 103 to the other end of the 105 tubular reactor. The other end of the 105-tube reactor was heated with a 104-heating jacket, which ensured a high temperature region of 425 ℃. During transportation, the crude oil gradually dissolves in water to be separated from the soil due to the temperature rise, and is hydrolyzed in a small amount to generate gas. Liquid water and a small amount of crude oil flow into a 107 storage tank through a 106 filter, and oil and water are separated.
The soil containing crude oil is conveyed to the other end of the 105 tubular reactor by a screw and then enters the 112 moving bed reactor from the upper part. The 113 boiler provides the supercritical water with 425 ℃ and 25MPa, and the supercritical water enters the 112 moving bed reactor from the lower part to extract the soil containing the crude oil. The supercritical water after extraction is discharged from the upper end of the 112 moving bed reactor and enters a 105-tube reactor. Clean soil is discharged from the lower end of the moving bed reactor 112 and enters 114 an organic waste solids collection tank.
Crude oil dissolved by gas, supercritical water and supercritical water passes through a 115 high-temperature gas filter, is cooled by a 108 heat exchanger, and then enters a 110 liquid separation tank. The pressure in the 110 separating tank is kept at 6MPa and the temperature is 10 ℃. And discharging the lower liquid in the 110 liquid separation tank into a 109 liquid storage tank for subsequent continuous separation of water, carbon dioxide, other hydrocarbons and impurities. And discharging the upper layer gas in the 110 liquid separation tank into a 111 gas storage tank, and continuing to separate hydrogen, carbon monoxide and other hydrocarbons of methane.
Example 2
The whole stillage was mixed with appropriate amount of water in a 201 stirred tank to form a pumpable thin stillage syrup which was heated to 75 ℃. The thin stillage syrup was injected into a 204 tubular reactor through a 202 high pressure diaphragm pump at 24Mpa. The 208 gas cylinder provides oxygen, the oxygen is pressurized by a 207 gas compressor to 24MPa, and the oxygen and the vinasse slurry are injected into a 204 tubular reactor together. The thin stillage syrup is fed 203 helically to the other end of the 204 tubular reactor. The lees pulp and oxygen react in a 204-tube reactor to release heat, and the temperature of a high-temperature area is ensured to be about 425 ℃. During the transportation process, as the oxidation reaction releases heat, the temperature rises, and the vinasse pulp is gradually carbonized, the biomass crude oil is generated, and the gas is generated. The aqueous solution containing soluble organic matter and part of the raw biomass oil flow into 206 a storage tank through 205 a filter to wait for oil-water separation.
The mixture solid containing biomass crude oil, biomass charcoal and the like is conveyed to the other end of the 204 tubular reactor by a screw and then enters the 213 moving bed reactor from the upper part. The 214 boiler provides supercritical water with 425 ℃ and 25MPa, and the supercritical water enters the 213 moving bed reactor from the lower part to perform supercritical water extraction on the biomass charcoal containing the biomass oil. And (4) discharging supercritical water after extraction is finished from the upper end of the 213 moving bed reactor, and feeding the supercritical water into the 204 tubular reactor. Clean biomass char is discharged from the lower end of the 213 moving bed reactor and enters 215 an organic waste solids collection tank.
After passing through a 216 high-temperature gas filter, the biomass crude oil dissolved by gas, supercritical water and supercritical water is cooled by a 212 heat exchanger and then enters a 210 liquid separation tank. The pressure in the 210 separating tank is kept at 6MPa and the temperature is 10 ℃. And discharging the lower-layer liquid in the 210 liquid separating tank into 209 a liquid storage tank for subsequent continuous separation of water, carbon dioxide and other hydrocarbons and impurities. And discharging the upper layer gas in the 210 liquid separation tank into 211 a gas storage tank for subsequent continuous separation of hydrogen, carbon monoxide, methane and other hydrocarbons.
Example 3
The biogas residue is mixed with a suitable amount of water in a 301 stirred tank to form a pumpable biogas residue slurry, the biogas residue slurry is heated to 75 ℃, and calcium hydroxide is added to make the slurry weakly alkaline. The biogas residue slurry is injected into a 304 tubular reactor through a 302 high-pressure diaphragm pump, and the pressure is 24Mpa. The 308 gas cylinder provides oxygen, the oxygen is pressurized by a 307 gas compressor to 24Mpa and is injected into the 304 tubular reactor together with the biogas residue slurry. The biogas slurry is fed 303 helically to the other end of the 304-tube reactor. The biogas residue slurry and oxygen react in the 304 tubular reactor to release heat, and the temperature of a high-temperature area is ensured to be about 425 ℃. In the conveying process, the temperature rises due to the heat release of the oxidation reaction, and the biogas residue slurry is gradually carbonized to generate the biomass crude oil and the generated gas. The aqueous solution containing soluble organics and a portion of the biocrude flow through 305 a filter into 306 a holding tank for oil-water separation.
The biomass char, which is transported by the screw 303 to the other end of the 304 tubular reactor, is discharged out of the 304 tubular reactor together with the dissolved biomass crude oil, supercritical water, and gas, and is introduced 309 into the gasifier to produce syngas. The synthesis gas can be collected after being discharged 309 from the gasification furnace through 311 synthesis gas output pipeline, and can also be directly used for power generation of a gas turbine after being filtered, desulfurized and denitrated at high temperature. 309 and finally discharging the residue of the gasification furnace reaction into a 310 ash collecting tank.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable manner, and these simple modifications and combinations should be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (10)
1. A method for continuous hydrothermal treatment of organic waste, the method comprising the steps of:
(1) The organic waste is crushed and then mixed with water to form a pumpable organic waste slurry.
(2) The organic waste slurry is injected into the tubular reactor by a high pressure pump.
(3) The end of the tubular reactor where the organic waste slurry is injected is a low temperature zone, the gas and insoluble solids produced in the organic waste slurry are discharged from the other end of the tubular reactor, and the organic waste solid and gas discharge end is a high temperature zone.
(4) A screw feeder in the tubular reactor transports the organic waste slurry from a low temperature region at one end of the tubular reactor to a high temperature region at the other end of the tubular reactor.
(5) During the process of transporting the organic waste slurry from the low temperature area to the high temperature area, the organic waste is gradually hydrolyzed, cracked, polymerized and the like to generate water soluble substances and crude oil of the organic waste, dehydrated and carbonized to be solid of the organic waste and gasified to be synthesis gas.
(6) And water-soluble organic matters and part of crude oil of the organic waste in the tubular reactor are discharged out of the tubular reactor from a liquid outlet of a low-temperature area of the tubular reactor, and the organic waste solids are conveyed to a discharge outlet of a high-temperature area to be discharged out of the tubular reactor.
(7) The rest of the synthesis gas, the supercritical water and the supercritical water dissolved matters are discharged from a certain discharge port of the high-temperature area of the tubular reactor together.
2. The method of claim 1, wherein the organic waste slurry comprises a catalyst selected from the group consisting of sodium hydroxide, potassium hydroxide, calcium hydroxide, sodium carbonate, potassium carbonate, calcium carbonate, formic acid, acetic acid, sulfuric acid, ferric chloride, zinc oxide, copper oxide, ferric oxide, ferroferric oxide, aluminum oxide, titanium oxide, silicon oxide, nickel oxide, molecular sieves, and zeolites, or combinations thereof.
3. The process according to claim 1, wherein the pressure in the tubular reactor is 22.1MPa above the critical pressure of water and the temperature in the high-temperature region is 374.3 ℃ above the critical temperature of water.
4. The method according to claim 1, wherein the heat in the high temperature zone is generated by heating means external to the tubular reactor or by exothermic reaction of the high pressure air, oxygen, hydrogen peroxide and the organic waste injected into the tubular reactor.
5. The method according to claim 4, wherein the high pressure oxygen, air, and hydrogen peroxide are injected into the tubular reactor together with the organic waste slurry, or into the moving bed or fluidized bed reactor together with the supercritical water as described in claim 7, or directly into the tubular reactor through a pipe.
6. The method of claim 1, wherein the local region of the tubular reactor is at an angle greater than 5 degrees from horizontal, such that a liquid-liquid and supercritical interface of water in the tubular reactor forms a liquid seal, and the liquid seal interface ensures that supercritical water and syngas are not discharged from the low temperature region drain.
7. The method according to claim 1, wherein the organic waste solids are discharged from the upper portion of the moving bed or fluidized bed reactor into the lower portion of the moving bed or fluidized bed reactor through a discharge port of the tubular reactor; supercritical water enters from the lower part of the moving bed or fluidized bed reactor, enters the upper part, is discharged and then enters the tubular reactor.
8. The process of claim 1, wherein the supercritical water, the synthesis gas and the supercritical water solvent are discharged from the tubular reactor at a pressure higher than 5Mpa, and then the water, the liquid carbon dioxide, the organic waste crude oil and the non-condensable gas in the mixture are separated by liquid separation after filtration, heat exchange and condensation.
9. The method of claim 8, wherein said liquid carbon dioxide and non-condensable gases are separated from carbon dioxide, methane, hydrogen, nitrogen, oxygen, carbon monoxide and hydrocarbons by temperature reduction, distillation, chemical adsorption, pressure swing adsorption and gas membrane separation.
10. The method of claim 1, wherein the organic waste solids, supercritical water, syngas, and supercritical water solubles are fed into the gasifier with oxygen or air to produce syngas.
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