CN106318417A - Method and system for the manufacture of bio-methane and eco-methane - Google Patents
Method and system for the manufacture of bio-methane and eco-methane Download PDFInfo
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- CN106318417A CN106318417A CN201610519331.5A CN201610519331A CN106318417A CN 106318417 A CN106318417 A CN 106318417A CN 201610519331 A CN201610519331 A CN 201610519331A CN 106318417 A CN106318417 A CN 106318417A
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- 238000000034 method Methods 0.000 title claims abstract description 84
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 12
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 198
- 239000007789 gas Substances 0.000 claims abstract description 195
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 177
- 239000001257 hydrogen Substances 0.000 claims abstract description 162
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 160
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 160
- 239000000203 mixture Substances 0.000 claims abstract description 85
- 238000000197 pyrolysis Methods 0.000 claims abstract description 56
- 239000002028 Biomass Substances 0.000 claims abstract description 43
- 239000002918 waste heat Substances 0.000 claims abstract description 33
- 230000008569 process Effects 0.000 claims abstract description 27
- 238000002360 preparation method Methods 0.000 claims abstract description 20
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 238000002156 mixing Methods 0.000 claims abstract description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 227
- 238000006243 chemical reaction Methods 0.000 claims description 60
- 239000000571 coke Substances 0.000 claims description 31
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 28
- 239000003245 coal Substances 0.000 claims description 28
- 239000003034 coal gas Substances 0.000 claims description 25
- 238000005755 formation reaction Methods 0.000 claims description 22
- 230000015572 biosynthetic process Effects 0.000 claims description 21
- 239000003054 catalyst Substances 0.000 claims description 20
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 15
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 14
- 229910052593 corundum Inorganic materials 0.000 claims description 14
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 14
- 239000003077 lignite Substances 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 13
- 150000002431 hydrogen Chemical class 0.000 claims description 12
- 239000000446 fuel Substances 0.000 claims description 10
- 239000012530 fluid Substances 0.000 claims description 8
- 239000002480 mineral oil Substances 0.000 claims description 8
- 235000010446 mineral oil Nutrition 0.000 claims description 8
- 238000010298 pulverizing process Methods 0.000 claims description 8
- 239000008187 granular material Substances 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 239000003921 oil Substances 0.000 claims description 6
- 239000007868 Raney catalyst Substances 0.000 claims description 5
- 229910000564 Raney nickel Inorganic materials 0.000 claims description 5
- 239000000919 ceramic Substances 0.000 claims description 5
- 150000001875 compounds Chemical class 0.000 claims description 5
- 239000002699 waste material Substances 0.000 claims description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 4
- 229910017518 Cu Zn Inorganic materials 0.000 claims description 4
- 229910017752 Cu-Zn Inorganic materials 0.000 claims description 4
- 229910017943 Cu—Zn Inorganic materials 0.000 claims description 4
- 150000001721 carbon Chemical class 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 4
- 239000000725 suspension Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- QDOXWKRWXJOMAK-UHFFFAOYSA-N chromium(III) oxide Inorganic materials O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 claims description 3
- 238000007872 degassing Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 claims description 3
- 238000005243 fluidization Methods 0.000 claims description 3
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000000843 powder Substances 0.000 claims description 3
- 239000002510 pyrogen Substances 0.000 claims description 3
- 239000000758 substrate Substances 0.000 claims description 3
- 229910052786 argon Inorganic materials 0.000 claims description 2
- 238000009835 boiling Methods 0.000 claims description 2
- 238000006555 catalytic reaction Methods 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims description 2
- 238000000227 grinding Methods 0.000 claims description 2
- 239000001307 helium Substances 0.000 claims description 2
- 229910052734 helium Inorganic materials 0.000 claims description 2
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 claims description 2
- 239000011261 inert gas Substances 0.000 claims description 2
- 239000000376 reactant Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 229910052717 sulfur Inorganic materials 0.000 claims 3
- 239000011593 sulfur Substances 0.000 claims 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 2
- CREMABGTGYGIQB-UHFFFAOYSA-N carbon carbon Chemical compound C.C CREMABGTGYGIQB-UHFFFAOYSA-N 0.000 claims 1
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- BKCAZRHVRSPNDV-UHFFFAOYSA-N lead;methane Chemical compound C.[Pb] BKCAZRHVRSPNDV-UHFFFAOYSA-N 0.000 claims 1
- 239000002245 particle Substances 0.000 claims 1
- 230000000630 rising effect Effects 0.000 claims 1
- 238000007789 sealing Methods 0.000 claims 1
- 150000003463 sulfur Chemical class 0.000 claims 1
- 238000002309 gasification Methods 0.000 abstract description 18
- 230000000035 biogenic effect Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 description 12
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 229910001868 water Inorganic materials 0.000 description 7
- 238000000926 separation method Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 230000005611 electricity Effects 0.000 description 4
- 230000032258 transport Effects 0.000 description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- 229920002488 Hemicellulose Polymers 0.000 description 2
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000001913 cellulose Substances 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- -1 hydrogen Chemical class 0.000 description 2
- 229920005610 lignin Polymers 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 241000270295 Serpentes Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- 235000013980 iron oxide Nutrition 0.000 description 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 238000001465 metallisation Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000032696 parturition Effects 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- XJKVPKYVPCWHFO-UHFFFAOYSA-N silicon;hydrate Chemical compound O.[Si] XJKVPKYVPCWHFO-UHFFFAOYSA-N 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- 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
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/40—Thermal non-catalytic treatment
-
- 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
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
-
- 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
- C10J3/48—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1014—Biomass of vegetal origin
-
- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0966—Hydrogen
-
- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/04—Gasification
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Processing Of Solid Wastes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention discloses a method and system for the manufacture of bio-methane and eco-methane; the method comprises a process of pyrolyzing biomass into biochar and mixing with pulverized and possibly suitably prepared fossil carbon, and a process of hydrogenating the carbon mixture. The system consists of a carbon hydrogenation gasification reactor, a biogenic hydrogen generating reactor, a steam and gas separator, a biomass pyrolysis reactor, a carbon mixture preparation device, a waste heat boiler, a heated gas preheater, a heat exchanger, a conveyer, and piping and pumps for liquids, vapors and gases.
Description
Technical field
Subject of the present invention is for being made by the hydrogasification of biological carbon and fossil-carbon (wherein biological hydrogen is gasifying agent)
Make biological methane and the method for ecological methane.
Background technology
Biological hydrogen is the product formed by biomass by the reaction of biological methane Yu steam.Biological methane is to use life
Thing hydrogen makes the product of biological carbon hydrogasification.Use biological hydrogen makes the product of coal or brown coal hydrogasification be ecological methane.Biological
Carbon is the product of the dry biomass pyrolysis preferably with high-load cellulose, hemicellulose and lignin.The most favourable pyrolysis
Product is combustible vapor and the gas of hereinafter referred to pyrolysis gas.Biomass are the product of not exclusively pyrolysis at 170 DEG C to 270 DEG C
Thing is half carbon comprising about 60% to 65% elemental carbon C ' that chemical property is similar to the chemical property of brown coal.Biomass are being higher than
The product being pyrolyzed completely at a temperature of 270 DEG C (preferably 300 DEG C) is comprises similar to the chemical property of coal or coke of chemical property
The biological carbon of about 65% to 80% elemental carbon C '.
Entitled according to Jerzy Szuba, Lech Michalik: " Karbochemia ",publishing
House, the hydrogen that the known use of book of 1983 is mainly obtained by the gasification based on steam and oxygen of thin coke or coal adds
The method of hydrogen-gasified.
The HYGAS method developed according to this book known Institute of Gas Technology (USA).HYGAS method be with
The high pressure method of the coal hydrogenation gasification of thin coke gasification combination, it is obtained in that high heat value gas (sub of natural gas).Should
There are three beta versions in technique, difference is that the method producing the hydrogen of hydrogasification is different.Hydrogen by oxygen-
Steam coal gasification or electric heat and gasification and obtain, or make iron oxides oxidoreduction as with the gas deriving from thin coke gasification
The result of (steam-ferrum system) and obtain.
According to this book it is known that pass through what Pittsburgh Energy Research Center (USA) developed
Hydrane method.Hydrane method is by making coal obtain high heat value gas with hydrogen direct reaction.Coal raw material (any grade)
React with the hydrogen being included in steam.Generating gasification process at 815 DEG C.In being suspended in internal reactor and flow (co-
Current), falling, (falling) and thinning bed (thinned bed) are middle there is coal gasification.Consequent thin coke is made to sink
Form sediment in the fluid bed of internal reactor, thus experience is reacted with the further of hydrogen.Internal reactor and external reactors shape
Become single assembly.Hydrogen for described technique carries out steam-oxygen gas by coke thin to a part in separate reactors
Change and obtain.
According to patent specification US 2011/0126458A1 it is known that be used for by making coal raw material add with hydrogen and steam
The method that the combination of hydrogen-gasified produces the gaseous fuel rich in methane.At about 700 DEG C to 1000 DEG C range temperature and about 132kPa
To the pressure of 560kPa, use hydrogen and superheated steam that the water paste of coal is gasified.The product of this gasification is hydrogen
Gas, methane, carbon monoxide and carbon dioxide.Separate and be recycled back to also to supply with this mixture by hydrogen in the separator
Should have in the SHR carbon gasification stove of steam, and CH4, CO and CO2Mixture be enriched in the methane (CH of up to 40%4) fuel
Gas.
According to Bohdan Stali ski, JanuszEntitled: " Wod ó r i wodorki ",
The book of Wydawnictwo Naukowo-Techniczne, Warszawa, 1987 is known to be added from outside by burning natural gas
Heat descends natural gas first to the steel pipe of the temperature of about 500 DEG C in the presence of catalyst (load nickel on a ceramic substrate)
The method manufacturing hydrogen in the reaction of alkane and steam.The gas entered in reactor using about 25% heats described pipe.
The feature of all these methane manufacture methods is consuming for producing two molecules in a large number elemental carbon C
CH4For, consume at least 5 elemental carbon atom C.Which has limited the efficiency of carbon hydrogasification technique.The feature of described method exists
In CO2Increase to the discharge of environment to maximum discharge and the solid waste of air.
Summary of the invention
Present invention solves the problem that and apply from the raw material based on plant of imtertilled crop and debirs complete
Full biomass generation biological carbon and the biological methane with high-load cellulose, hemicellulose and lignin that use, and subsequently
For making biological carbon hydrogenation chemical conversion biological methane and making the biological hydrogen of the ecological methane of fossil-carbon hydrogenation chemical conversion, and produce
The chemical energy of gained fuel changes into the high transformation efficiency more than 60% of electricity.These effects are obtained: giving birth to by following steps
Produce biological carbon during material pyrolysis, form the mixture of biological carbon and fossil-carbon, and use biological hydrogen to make described mixing
Thing gasify, described biological hydrogen utilize biological methane, steam exist catalyst and by add hot gas (add hot gas use from
Thin coke, surplus hydrogen and the heat energy of pyrolysis gas burning and use solar energy to preheat) feelings of heat supplied from the outside
Obtaining under condition, this causes the accumulation of solar energy.
Following technique is used to carry out for manufacturing the method for biological methane and ecological methane and electric energy and heat energy: to make biology
Matter is pyrolyzed into biological carbon, the technique that described biological carbon mixes with pulverizing and possible suitably prepd fossil-carbon, and makes carbon mix
Thing hydrogenation is melted into rough gas, the desulfurization of described rough gas and is separated into the technique of hydrogen and methane, uses and there is catalysis
The technique producing hydrogen in the case of agent and the heat supplied by outside in the methane reaction with steam, the feature of described method
It is, makes raw material based on plant that pulverizing is dried or waste material raw material individually or with the form experience pyrolysis of specific group
Process, described pyrolytic process or carry out under standard pressure producing half carbon and heat within the temperature range of 170 DEG C to 270 DEG C
Solve gas, or within the temperature range of 270 DEG C to 300 DEG C, carry out producing biological carbon and pyrolysis gas, or higher than 300
Carrying out within the temperature range of DEG C, the part in described pyrolysis gas leads to biomass pyrolysis device to carry out the heat of biomass
Solve, and another part of pyrolysis gas leads to preheater to preheat adding hot gas.Obtained comprise about 60% to
Half carbon of the elemental carbon of 65% preferably mixes with the brown coal pulverized, and comprises biological carbon and the powder of the elemental carbon of about 65% to 80%
Broken coal mixing, the elemental carbon C ' from biological carbon is preferably C ' with the ratio of the elemental carbon C from fossil-carbon: C=1:1.Will
Previous mixture or latter mixture supply, to the first carbon hydro-gasifier reactor, wherein use biological hydrogen to carry out complete hydrogenation gas
Metallization processes is to produce rough gas and ash, or carries out coal and biological carbon or the Partial hydrogenation gasifying process of brown coal and half carbon
To produce rough gas and thin coke.Thin coke leads to preheater to preheat and to burn adding hot gas.Former by obtained
Coal gas (in the second heat exchanger cool down) carries out desulfurization, be subsequently isolated into hydrogen, residual gas and by pure biological methane and
The methane mixture of ecological methane composition.It is transported to the heat cooled down from rough gas in preheater carry out adding hot gas
Preheat and be transported to the first heat exchanger producing in the waste heat boiler of process steam and electric power vapour.Methane is transported to gas
Body distribution pipeline or compressor or condenser or supply produce electric energy and the TRT of heat energy.By a part of methane (it is
The form of biological methane) supply is to the 3rd biological hydrogen reaction of formation device, wherein in the vapours supplied by waste heat boiler and logical
Cross add hot gas supply to described reaction heat reaction in, about 500 DEG C to 700 DEG C at a temperature of in the existence of catalyst
Under, produce biological hydrogen and CO2Mixture, it cools down in waste heat boiler and is separated into CO afterwards2Be transported to the first reaction
The biological hydrogen of the carbon mix hydrogasification technique in device.Hot gas will be added be preheated to enter in the 3rd reactor in preheater
The temperature of about 800 DEG C to 1200 DEG C needed for row biological hydrogen reaction of formation, described preheating uses and is supplied with from the second biomass
Surplus hydrogen and use that the gas burner of the pyrolysis gas of pyrolysis reactor and/or use are reclaimed from rough gas are supplied
There are the thin coke of grinding or coal or the pulverized fuel combustor of biological carbon.The hot gas stream that adds thus heated enters the 3rd reactor
In wherein there is biological hydrogen and CO with heating2The pipe of the technique generated.
Half carbon is using CO with the mixture being dried of pulverizing of brown coal or biological carbon and coal2Air is removed it from which
After from carbon mix preparation facilities supply to the first reactor.In the first reactor, the hydrogasification technique of carbon mix is first
First carrying out in the gas introduced from described interior ceiling portion the suspension bed under wandering in interior room, described gas is about
At a temperature of about 815 DEG C, the H of about 50% is comprised under the pressure of 2.5MPa to 7.5MPa2With 50% CH4.Obtain in this process
The rough gas obtained enters steam and coal gas separator through the first reactor, and described rough gas removes dust and the gas being blended at this
Body, and carry out desulfurization especially, afterwards its be separated into the clean methane mixture that is made up of biological methane and ecological methane with
And pure hydrogen, described hydrogen portion is recycled back to biological hydrogen stream.The hydrogen (for surplus hydrogen) of other parts is transported to
Burner in preheater.The carbon mix of partial reaction is provided to the mistress in the first reactor, makes described carbon mix at this
Compound and hydrogen react to generate ash and hydrogen+methane gas completely, or make its partial reaction to form thin coke and hydrogen
Gas+methane gas.Described thin coke is transported burning or stores, and described hydrogen+methane gas is supplied to described from top
The interior room of reactor.
Carbon mix is made to use nozzle form with suspended substance under the pressure of about 6.8MPa with mineral oil after merging
Supply the highest region section being referred to as evaporating region to the first high-pressure reactor.At the temperature (about 315 DEG C) of advantage herein, institute
State oil to be evaporated and its steam is arranged together with the pyrogen coal gas of the centre portion leaving the first order being referred to as carbon hydrogasification
Put to steam and coal gas separator.The most condensed, separated mineral oil is recycled and is back to oil bag
In carbon suspension body preparation facilities, and make purified rough gas, after desulfurization, be especially separated into methane mixture and treat
The pure hydrogen merged with biological hydrogen.At a temperature of about 300 DEG C, the dry granule of carbon mix falls into the centre portion of reactor,
Dry granule at this this carbon mix was given birth in the containing of reactor bottom section leaving the second level being referred to as carbon hydrogasification
The stream of the gas of thing hydrogen fluidizes, and in being referred to as the centre portion of the first order of hydrogasification, is being increased to about
Carbon and the degassing of biological carbon granule and partial hydrogenation gasification is there is at the temperature of 650 DEG C and the pressure of 6.8MPa.At reactor
In the fluid bed of bottom section, supply is used to make portion to biological hydrogen and the hydrogen of described section at a temperature of 750 DEG C to 950 DEG C
The carbon mix dividing reaction carries out complete hydrogenation gasification.
Add hot gas be the material for the 3rd reactor be inert gas, preferably CO2, nitrogen, helium or argon or
Person has the gas of high specific heat or has high boiling liquid, described in add hot gas heat carried the biology to the 3rd reactor
In the reaction of methane and steam, the amount of described heat be about 500 DEG C to 700 DEG C at a temperature of at Ni/Al2O3In the presence of catalyst
It is sufficient for biological hydrogen and CO2Form the about 155kJ/mol to 165kJ/mol CH of reaction4。
From the biological hydrogen at a temperature of about 500 DEG C and CO2Hot mixt stream heat, from the gas leaving preheater
About 600 DEG C at a temperature of steam stream heat and from external system especially from having produced when device provisioning
The heat of the TRT producing electric energy and heat energy when ecological methane or biological methane is transported to waste heat boiler.
Heating gas preheater is supplied with the high-temperature hot taking from rough gas and the heat supplied by solar collector.
In the Part I of the 3rd reactor, at the temperature ranges of about 500 DEG C to 700 DEG C and 1.5MPa to 4.5MPa
At Ni/Al under pressure2O3As generating the biological methane of reactant of biological hydrogen and steam by about in the presence of Raney nickel
800 DEG C of hot gas that add to the heat of 1200 DEG C of temperature are additionally heated in reactor tube.
Biological hydrogen for the carbon monoxide in the 3rd reactor and steam forms reaction, described biological hydrogen reaction of formation
Middle admixture of gas flow to the Part II of described 3rd reactor, described 3rd reactor from the Part I of the 3rd reactor
Part II run under the temperature range lower than described Part I, or about 200 DEG C to 300 DEG C within the temperature range of
Use Cu-Zn/Al2O3Catalyst, or in the high temperature range of 350 DEG C to 500 DEG C, use Fe/Al2O3Catalyst is subsequently
About 200 DEG C to 300 DEG C in the range of use Cu/Al2O3Catalyst or use within the temperature range of 300 DEG C to 450 DEG C
Fe2O3+Cr2O3Carry out described reaction.
Another theme of the present invention is for manufacturing biological methane and ecological methane and heat and the system of electricity.Described use
Consisting of in the system manufacturing biological methane and ecological methane and heat and electricity: carbon hydro-gasifier reactor, biological hydrogen is raw
Become reactor, coal gas-vapour separator, biomass pyrolysis reactor, carbon mix preparation facilities, waste heat boiler, add hot gas
Preheater, heat exchanger, conveyer, for pipeline and the pump of liquid, steam and gas, described system is characterised by, first
Carbon hydro-gasifier reactor has two entrances, and one for hydrogen, another is connected to and the second biomass pyrolysis reactor
The carbon mix connected or carbon pastes preparation facilities.First reactor has two outlets: for thin coke or the second of ash
Outlet and the first outlet for rough gas, described first outlet is connected to steam-coal gas separator via the second heat exchanger.
Steam-coal gas separator has the first outlet of the pipeline form of the biological hydrogen outlet being connected to the 3rd reactor, for methane
The second outlet and for dust, the 3rd outlet of steam and residual gas.First hydrogen outlet of steam-coal gas separator
Being divided into two pipelines, wherein recycle hydrogen gas pipeline is connected to the first biological hydrogen entrance of the first reactor, and surplus hydrogen pipe
Line is connected to the gas burner of preheater.For being additionally coupled to the from the second of the methane of steam-coal gas separator the outlet
Three hydrogen reaction of formation devices, the 3rd hydrogen reaction of formation device for biological hydrogen and CO2First outlet of mixture is via waste heat boiler
Stove is connected to biological hydrogen and CO2The separator of mixture, it is anti-that the outlet of described separator is connected to first by biological hydrogen pipeline
Answer device.Waste heat boiler has electric power vapor outlet and is connected to the process steam outlet of the 3rd reactor.The of 3rd reactor
Two outlets are connected to the pipeline for adding hot gas of preheater.Rough gas heat exchanger is connected to preheater via pipeline, and
And then, it is connected to waste heat boiler via preheater exit gas pipeline.
Second biomass pyrolysis reactor has the dry biomass entrance being connected to biomass conveyer to be mixed with being connected to carbon
The biological carbon outlet of compound preparation facilities, and it is connected to gas burner and the setting being arranged in biomass pyrolysis reactor
The pyrolysis gas outlet of the gas burner in heating gas preheater.
Described preheater has the 3rd heat exchanger, and described 3rd heat exchanger one end is connected to heat gas lines and another
One end is connected to be arranged on the nozzle at the 3rd reactor inlet via heat gas lines.Preheater is equipped with via pyrolysis gas
Fluid line is connected to the gas burner of the second biomass pyrolysis reactor and is connected to equipped with via thin coke conveyer
The pulverized fuel combustor of the thin coke export of the first reactor, and additionally, preheater is via preheater exit gas pipeline
It is connected to waste heat boiler.Additionally, preheater has the heat exchanger being connected to solar collector arrangement.
Preferably, the 3rd biological hydrogen reaction of formation utensil has inner tube, described inner tube to comprise to be positioned at the 3rd reactor
Load in Part I Raney nickel Ni/Al on a ceramic substrate2O3, described Part I is connected to add entering of hot gas
Mouth is to heat these pipes and to comprise Cu-Zn/Al2O3Catalyst or Fe/Al2O3And Cu/Al2O3The pipe of catalyst, described pipe
Be positioned in the Part II of the 3rd biological hydrogen reaction of formation device, and the 3rd reactor have the entrance for biological methane, for
The entrance of process steam and for biological hydrogen and CO2The outlet of mixture.
Hydrogen and CO2Mixture separator has the pure CO leading to air and/or processing for downstream and/or seal up for safekeeping2Go out
Mouthful.
One advantage of the method producing biological methane and ecological methane and electric energy and heat energy according to the present invention is to make
Produce biological methane by the biological carbon from annual renewable biomass and contact the heat to biological hydrogen life by adding hot gas
Becoming reaction, this process makes it possible to be controlled heat, and anti-available from making to leave first for making to add the heat of hot gas preheating
The rough gas answering device cools down, available from the burning of pyrolysis gas, available from surplus hydrogen and available from thin coke and solar energy, this allows
Low consumption from the elemental carbon C of fossil-carbon generates the CH of a part so that it is changed into ecological methane with biological hydrogen4,
The carbon atom C consuming a fossil-carbon more.This significantly reduces the CO in environment2Discharge the solid waste row relevant with carbon
Put.At manufacture fuel gas: when biological methane or ecological methane, this significantly reduces the consumption of biological carbon and fossil-carbon.This combustion
Material can utilize the energy efficiency more than 60% to generate electricity in TRT.
Described advantage is to use biological hydrogen to biological carbon and fossil-carbon hydrogasification simultaneously in a reactor.Adding of carbon
Hydrogen-gasified is exothermic process；Need not supply heat to described reaction, therefore the heat exchanger in hydro-gasifier reactor is
Unwanted.By using gas burner and pulverized fuel combustor to realize 800 DEG C to 1200 in heating gas preheater
DEG C suitable high temperature.In solar collector arrangement, it is done up to the temperature adding hot gas of 1200 DEG C, therefore produces and make
Accumulate in adding hot gas with solar energy described in the new method of solar energy, and then accumulate and fire at produced gaseous state
In material, i.e. biological methane and ecological methane.The level of 48% it is in by the efficiency of solar electrical energy generation.At present, the effect of photovoltaic cell
Rate is about 15%.At CO2With the pure CO obtained in the separation process of hydrogen2Stream is prone to be bound to CO2Seal up for safekeeping in technique, whether
Underground sequestration or by making CO2Be combined with silicate to form stable product.This causes the fossil used for this purpose
The zero-emission generating of carbon.
Accompanying drawing explanation
The present invention is illustrated in the embodiment combine accompanying drawing, and accompanying drawing 1 shows the schematic diagram of technique, and it illustrates
For producing the connection between subsystem and the equipment used in the method for biological methane and ecological methane.
Detailed description of the invention
Embodiment I
By biological carbon that elemental carbon content C ' is 77% and coal supply that elemental carbon content is 70% to 80% to using life
The biological carbon of thing hydrogen and fossil-carbon hydrogasification technique, be maintained at C ' by the ratio of presetting biological carbon Yu coal: C=1:1.Figure
Shown in the first biological carbon and fossil-carbon hydro-gasifier reactor 1 in, use biological hydrogen to carry out the complete of biological carbon and fossil-carbon
Full gasification.Use fuzz stick as the complete pyrolytic process for carrying out in the second biomass pyrolysis reactor 2 at about 300 DEG C
Biomass, described fuzz stick utilizes biomass conveyer 21 to supply to the second pyrolysis reactor 2.The product of biomass pyrolytic
It is that biological carbon and steam and combustible pyrolysis's gas, described steam and combustible pyrolysis's gas are anti-to second via pipeline 22a supply
Answer the gas burner 13 in device 2 and via pipeline 22b supply to the gas burner being positioned in heating gas preheater 9
14, described in add hot gas be CO2Stream.Use biological carbon conveyer 23 that from the second reactor 2, biological carbon is delivered to carbon mixing
Thing preparation facilities 25, wherein it is mixed with the coal supplied to device 25 by conveyer 24 and suitably together with pulverize.
This mixture (not having any special pretreatment) supplies the top to the first carbon hydro-gasifier reactor 1 by conveyer 26,
At this by leaving biological hydrogen and CO at about 815 DEG C2Described hydrogenation mixture is gasificated into biological first by the biological hydrogen of separator 8
Alkane and ecological methane, the biological hydrogen flowing through biological hydrogen pipeline 18a since then passes through pipe together with the hydrogen via pipeline 19a recirculation
Line 18b supplies the bottom to the first reactor 1.Biological hydrogen flowing by carbon mix in the adiabatic mistress of the first reactor 1 with
The fluid bed of thin coke causes the fluidisation of described bed and react with biological carbon and coal and comprise about 50% hydrogen and 50% with generation
The reacting gas of methane, described gas flows through the hole of the upper area of the shell being positioned at room, and flows to described interior room and carbon mixes
The whereabouts suspension bed of compound flows parallel, and with described mixture reaction, described mixture uses carbon mix conveyer 26 from mixed
Compound preparation facilities 25 is by the carbon mix entrance supply extremely interior room in interior room.React as in the interior room of the first reactor 1
, there is the partial reaction of described mixture and biological hydrogen, and the carbon of Partial Conversion in the result that gas reacts with coal and biological carbon
Mixture falls to the fluid bed in mistress, utilizes biological hydrogen this its and is completely converted and gained ash is arranged by ash
Put channels discharge and transport to ash storing spot with conveyer 28b, and unconverted thin coke (may be on sieve and by sky
Air flow recovery) it is recycled back to carbon mix preparation facilities 25.From the rough gas of the first reactor via pipeline 6 and Re Jiao
Parallel operation 6a supplies to steam and coal gas separator 5.The rough gas (doing) obtained has following average composition: CH4About 72 bodies
Long-pending %, H2About 24.7 volume %, CO are 1.5%, CO2About 1.6% (comprises H with other impurity2S) 0.2% it is about.
In steam-coal gas separator 5, rough gas carries out desulfurization and separation on the film that only hydrogen may pass through, described
Hydrogen is transported to recycle hydrogen gas pipeline 19a via hydrogen gas lines 19, merges with the biological hydrogen in pipeline 18b, and also transports
To the surplus hydrogen pipeline 19b being connected with the gas burner in preheater 9.Steam and residual gas are discharged by pipeline 17,
And the mixture of biological methane and ecological methane flows through pipeline 20 and is divided into two equal streams: supply via pipeline 20a
To the biological methane of the 3rd biological hydrogen reaction of formation device 3 with by pipeline 20b supply to gas service pipes line and supply generating
The ecological methane of device.3rd biological hydrogen reaction of formation device 3 includes the inside being filled with catalyst (i.e. nickel on ceramic monolith)
Pipe 3a.These pipes use pipeline 20a to be supplied with biological methane and the vapours using steam pipe line 11a to be supplied with about 400 DEG C.
As the result of reaction occurred in the pipe comprise Raney nickel in the 3rd reactor 3, the reaction of biological methane and steam is led
Cause biological hydrogen and CO2The formation of mixture, described biological hydrogen and CO2Mixture via in pipeline 10b and waste heat boiler 4
Heat exchanger 4a supplies and further by pipeline 10c supply to biological hydrogen and CO2Mixture separator 8.For by biology
Methane and steam form biological hydrogen and CO2Energy major part by be at a temperature of about 900 DEG C add hot gas provide, its
By nozzle 10d supply to the 3rd reactor 3 and flowing around the pipe 3a of reactor 3, the remainder of energy is by warm
400 DEG C of steam bring.In first reactor 1 coal and biological carbon hydrogasification reaction in produce and by add hot pipeline 7b supply
The heat needed for the heat energy replenished the supply to biological hydrogen reaction of formation should be significantly higher than to the heat of preheater 9.The heat of excess is via pipe
Line 7c and 7a is emitted into waste heat boiler 4 from heating gas preheater 9.Cool down during technique described in the 3rd reactor 3 adds
Hot gas is by the heat exchanger 9a of pipeline 10a supply to preheater 9, and the said hot gas that adds is heated to up to 900
DEG C and flow to the nozzle 10d of the 3rd reactor 3 again by pipeline 10.
Under the pressure suitably increased at a temperature of about 500 DEG C, there is biological hydrogen reaction of formation.Pressure is increased to 3MPa
The increase causing response speed and the reduction of the size allowing the 3rd reactor 3.Also use water pipeline 12 with from external water
The supplementary water supply waste heat boiler 4 in source.Waste heat boiler 4 produces the process steam of about 400 DEG C, and it passes through process steam pipeline 11a
Supply to the 3rd biological hydrogen reaction of formation device 3, and the electric power vapour of about 585 DEG C of temperature of generation, it is via electric power steam pipe line
11b supplies the electric power turbine TP to TRT.
Embodiment II
The biological carbon supply that elemental carbon content C ' is 77% is extremely used the biological carbon hydrogasification technique of biological hydrogen.At figure
In the first shown biological carbon hydro-gasifier reactor, carry out the conversion completely of biological carbon.Use Radix Glycyrrhizae as about 300 DEG C of temperature
Being pyrolyzed into the biomass of biological carbon technique under degree completely, every 1 ton of Radix Glycyrrhizae produces the biological carbon of about 350kg, adds pyrolysis gas.
Biomass conveyer 21 is used to make Radix Glycyrrhizae supply in the second biomass pyrolysis reactor 2；Then produced biological carbon is supplied
Should to biological carbon preparation facilities 25, this its by the most crushed, and partial thermal decomposition gas is supplied to instead via pipeline 22a
Answer the gas burner 13 in device 2, and the pyrolysis gas of another part is transported to heat in gas preheater 9 via pipeline 22b
Gas burner 14.The biological carbon suitably pulverized in biological carbon preparation facilities 25 is supplied to the via biological carbon conveyer 26
The top of one biological carbon hydro-gasifier reactor 1, the method provided according to embodiment I at this uses at a temperature of about 815 DEG C
Biological hydrogen makes it carry out complete hydrogenation and is gasificated as biological methane.From the first reactor 1, rough gas is handed over by heat via pipeline 6
Parallel operation 6a supplies to coal gas and vapour separator 5.The composition of protozoa gas is given in embodiment I.Divide at steam and coal gas
In device 5, rough gas is carried out desulfurization and separation, be then transported to the pipeline being connected with biological hydrogen pipeline 18a via pipeline 19
19a, flows further through pipeline 18b and enters the bottom of the first reactor 1, and surplus hydrogen flows through pipeline 19b and enters in preheater
Gas burner 14.Supply is divided into two streams to the biological methane stream of pipeline 20: be transported to the 3rd by pipeline 20a biological
The biological methane of hydrogen reaction of formation device 3, and by pipeline 20b transport to supply the biological first of the TRT of fuel cell form
Alkane.The biological methane of excess is provided to the biological methane tank of compression.In the 3rd reactor 3, the generation of biological hydrogen is according to enforcement
The method that example I provides is carried out.The operation of waste heat boiler 4 is described in embodiment I.
Hot gas supply is added in the preheater 9 of described gas by flow out to pipeline 10a from the 3rd reactor 3,
This its use is supplied with the gas burner 14 of pyrolysis gas and part biological methane and surplus hydrogen and is preheating to about 900 DEG C
Temperature, and subsequently, it is recycled to the nozzle 10d of the 3rd reactor 3 via pipeline 10.Pipe 3a is carried out by described reactor
Heat and biological hydrogen and CO in those pipes2The method provided according to embodiment I that generates of mixture is carried out.
Embodiment III
Elemental carbon content C ' is about 60% half carbon and elemental carbon content C be about the brown coal supply of 60% to biological carbon and
Fossil-carbon hydrogasification technique, keeps presetting preferred biological carbon and coal ratio C ': C=1:1, and it is the carbon in mineral oil
The form of mixture suspended substance.In first biological carbon shown in the figure and fossil-carbon hydro-gasifier reactor 1, use biological hydrogen
Carrying out the partial gasification of half carbon and brown coal, therefore form rough gas, described rough gas is unreacted hydrogen, biological methane and life
State methane and the mixture of other gaseous components, and also form thin coke.For manufacturing biological methane and ecological methane
System illustrates in the drawings.It is the gas manufacturing plants producing ecological methane.Use fuzz stick as at about 170 DEG C to 270 DEG C
Under the biomass of partial thermal decomposition process that carry out in the second biomass pyrolysis reactor 2, described fuzz stick uses biomass defeated
Machine 21 is sent to supply to the second reactor 2.The product of biomass portion pyrolysis is half carbon and steam and combustible pyrolysis's gas, institute
The part stating gas supplies the gas burner 13 to the second biomass pyrolysis reactor 2, and another via pipeline 22a
Part is supplied to being positioned at the gas burner 14 added in the preheater 9 that hot gas is nitrogen stream by pipeline 22b.Use biological carbon
Half carbon is delivered to the first carbon pastes preparation facilities 25, said half carbon from the second biomass pyrolysis reactor 2 by conveyer 23
Mix with the brown coal supplied to device 25 by coal conveyer 24 and suitably together with pulverize, and supply mineral oil wherein.
By by carbon and the mixture (comprising the mineral oil of 75 volume % and the carbon of the pulverizing of 25% volume) that formed of oil via supply line
26 supplies are to nozzle, and under the pressure of 6.8MPa, carbon pastes supply is referred to as evaporating area to the first reactor 1 by described nozzle
The highest region section of section.At a temperature of 315 DEG C of advantage herein, described oil evaporation and its steam are referred to as carbon hydrogenation with leaving
The pyrogen coal gas of the centre portion of the first order of gasification is emitted into steam and coal gas separator 5 via heat exchanger 6a together.Return
The mineral oil (condensing the most within the condenser) received is recycled back to carbon preparation facilities 25, and rough gas experience purifies
And desulfurization.The dry carbon of about 300 DEG C of temperature and biological carbon granule lead to central section, described dry carbon and biological carbon granule leave by
Be referred to as carbon hydrogasification the second level reactor bottom section the gas stream comprising biological hydrogen in experience fluidisation, and in
, under the pressure of the temperature and 6.8MPa that are increased to 650 DEG C, there is degassing and the partial hydrogenation gasification of carbon granule in heart section.Part
The carbon mix converted uses supply anti-first at a temperature of 750 DEG C to 950 DEG C to biological hydrogen and the hydrogen of described section
Answer device 1 bottom section fluid bed in carry out complete hydrogenation gasification.Purified rough gas is in steam and coal gas separator 5
Experience further separates, and the Hydrogen Separation being wherein not used by is in biological methane and the methane mixture of ecological methane and warp
It is recycled back to recycle hydrogen gas pipeline 19a by hydrogen gas lines 19, supplies biological hydrogen at pipeline bottom the first reactor 1
18b merges, and is recycled back to the surplus hydrogen pipeline 19b of the gas burner 14 being connected in preheater 9.Methane
Mixture flows through pipeline 20, and described pipeline is divided into the biological methane of biological methane supply to the 3rd biological hydrogen reaction of formation device 3
Pipeline 20a and by the pipeline 20b of ecological methane supply to gas distributing system.The generation of biological hydrogen occurs at the 3rd reactor 3
In, as the result of biological methane Yu steam reaction.Energy needed for the endothermic reaction is supplied extremely by by pipeline 10 and nozzle 10d
3rd reactor 3 add hot gas and the vapours supplied by steam pipe line 11a is brought, and the amount of energy to be supplied can be led to
The flow adding hot gas and the temperature of crossing flowing around the pipe 3a controlled in the 3rd reactor 3 control.Inside pipe 3a
Biological hydrogen is occurred to form reaction, described pipe at a temperature of about 500 DEG C in the presence of catalyst (nickel of load in ceramic bases)
3a heats by being in the heating gas hot-fluid at a temperature of 900 DEG C.Produced and cooled biological hydrogen is transported to first
Carbon and biological carbon hydro-gasifier reactor 1.Biological hydrogen and the elemental carbon C ' from half carbon and anti-with the elemental carbon C from brown coal
Biological methane and ecological methane should be generated and react relevant heat to carbon hydrogasification.Carry out rough gas in automatic heat-exchanger 6a cold
But heat is supplied to heating gas preheater 9 via adding hot pipeline 7b, and subsequently, from the heat warp of the hot gas of preheater 9
Supplied to waste heat boiler 4 by pipeline 7c and 7a.Additionally, waste heat boiler 4 accepts the heat from many sources, especially from heat
In exchanger the cooling of biological hydrogen heat and from biological hydrogen and the CO leaving the 3rd biological hydrogen reaction of formation device 32Mixture
Heat, heat exchanger 4a that described mixture is flow in waste heat boiler 4 by pipeline 10b and leave used heat by pipeline 10c
Boiler 4 arrives separator 8, and described in described separator 8, mixture is divided into via pipeline 18a and 18b supply anti-to first
Answer the biological hydrogen of device 1 and be transported to CO2Seal the carbon dioxide of equipment up for safekeeping.Leave the CO of separator 82Stream was (previously at waste heat boiler 4
In heat exchanger 4a in cool down) pass through CO2Pipeline 10e flow to CO2Seal technique up for safekeeping, particularly by silicate such as snake
The CO of stone2Seal technique up for safekeeping.This immobilized product, magnesium carbonate, silicon dioxide and water are durable and easily stored.
In another embodiment, heating gas preheater 9 is connected to solar energy collector system.At solar energy collecting
In all heat exchangers of device system, as the CO of heat carrier2It is heated as high as about 1200 DEG C and is recycled back to position
Heat exchanger 30 in preheater 9, heat is supplied to the 3rd reactor via heat gas lines 10 from described heat exchanger 30
3, described 3rd reactor 3 produces and is separated into biological hydrogen and CO in separator 82Biological hydrogen and CO2Mixture, described separation
Device 8 is potassium scrubber.The heat of solar energy is transferred to the 3rd reactor 3 by heat carrier with the high efficiency of up to 80%, the 3rd
In reactor 3, it is converted to the chemical energy of biological hydrogen, and changes into biological methane and ecology in the first reactor 1 subsequently
The chemical energy of methane.
The embodiment of device
As it can be seen, the first carbon and biological carbon hydro-gasifier reactor 1 have two entrances, 18b and 26, the first entrance
18b is another entrance 26 for hydrogen, and the conveyer as carbon mix is connected to the second biomass pyrolysis reactor even
The carbon mix preparation facilities 25 connect.Second pyrolysis reactor 2 is equipped with pyrolysis gas pipeline 22a and 22b, wherein pipeline 22a
It is connected to the gas burner 13 that is positioned in described reactor and pipeline 22b is connected to be positioned in heating gas preheater 9
Gas burner 14.Second pyrolysis reactor 2 is equipped with two conveyers, and wherein conveyer 21 is biomass conveyer and defeated
Sending machine 23 is the biological carbon conveyer being connected with carbon mix preparation facilities 25.Described device has the outlet purifying gas
16a and entrance 16, and also equipped with coal conveyer 24 and carbon mix conveyer 26.First reactor 1 has two outlets 6
With 28, wherein the second outlet (thin coke export) 28 is connected to supply the thin of the pulverized fuel combustor 15 that is positioned in preheater 9
Coke Transport machine 28a and be connected to conveyer 28b to lead to storage, and handed over by heat for the first outlet 6 of rough gas
Parallel operation 6a is connected to steam and coal gas separator 5.Steam and coal gas separator 5 have first hydrogen outlet the 19, second methane and go out
Mouth 20 and the 3rd waste outlet 17.First hydrogen outlet 19 of separator 5 is divided into two pipeline 19a and 19b, wherein pipeline 19a
It is connected to the first entrance 18b of the first reactor 1, and the burner 14 that pipeline 19b is connected in preheater 9, and separator 5
The second methane outlet 20 be additionally coupled to the 3rd reactor 3, the first outlet 10b of described 3rd reactor 3 is via waste heat boiler 4
Heat exchanger 4a and be connected to separator 8 via pipeline 10c, described separator 8 first biological hydrogen export via pipeline
18a and 18b is connected to the first reactor 1, and the 2nd CO2Outlet is connected to CO by pipeline 10e2Mothballed plant is (the most not
Illustrate).Waste heat boiler 4 has and is connected to the 3rd biological hydrogen and CO via steam pipe line 11a2The process steam of reaction of formation device 3
Outlet and be connected to the electric power vapor outlet (not shown in FIG.) of steam turbine of TRT via pipeline 11b.Used heat
Boiler 4 also has and the connection of water pipeline 12.Second outlet of the 3rd reactor 3 is connected to and the heat exchanger in preheater 9
Heat gas lines 10a that 9a connects, described exchanger adds hot gas via what pipeline 10 was connected to be positioned in the 3rd reactor 3
Nozzle 10d.Additionally, connect via pipeline 7b, preheater 9 and pipeline 7c and 7a from adding the heat exchanger 6a obtaining heat hot gas
It is connected to waste heat boiler 4.Additionally, preheater 9 is equipped with heat exchanger 30 and the 3rd reaction being connected to solar collecting device
Utensil has one group of pipe 3a with catalyst.
The reference used in figure
1 for carbon and/or the first reactor of the hydrogasification of biological carbon
2 second biomass pyrolysis reactors
3 for generating the 3rd reactor of biological hydrogen
Pipe assembly R (III) of 3a reactor
4 waste heat boilers
First heat exchanger of 4a waste heat boiler
5 steams and coal gas separator
6 rough gas pipelines
6a the second rough gas heat exchanger
7a supplies heat to the pipeline of boiler
7b rough gas adds hot pipeline
7c preheater adds hot pipeline
7d is for the pipeline of external heat
8 hydrogen gas segregators
9–CO2Stream preheater
3rd heat exchanger of 9a preheater
10 heating gas flow lines
10a stream of recycled gases pipeline
10b hydrogen gas lines
The pipeline that 10c hydrogen leaves
10d adds hot runner nozzle
10e leads to discharge or the CO sealed up for safekeeping2Pipeline
11a process steam pipeline
11b electric power steam pipe line
12 water pipelines
Gas burner in 13 devices
Gas burner in 14 preheaters
Pulverized fuel combustor in 15 preheaters
16 for removing the CO of carbon mix2Nozzle
16a removes the outlet of gas
The pipeline that 17 steams and coal gas leave
18a biological hydrogen pipeline
18b hydrogen collecting apparatus pipeline
19 hydrogen gas lines separated
The hydrogen gas lines of 19a recirculation
19b surplus hydrogen pipeline
20 methane mixture pipelines
20a biological methane pipeline
20b ecology methane pipeline
21 biomass conveyers
22 biomass pyrolysis devices
22a pyrolysis steam and gas-pipe line
The pyrolysis gas pipeline of 22b supply preheater
23 biological carbon conveyers
24 carbon (brown coal or coal) conveyer
25 carbon mix preparation facilitiess
26 carbon mix conveyers
27 powder carbons/biological carbon conveyer
28 thin coke conveyers
The thin coke conveyer that 28a grinds
28b leads to the thin coke conveyer of storage
29 waste material conveyers
30 the 4th heat exchangers being used for solar heat
Claims (13)
1., for producing biological methane and a method for ecological methane, described method uses following technique to carry out: make raw
Material pyrolysis becomes biological carbon the technique mixed with pulverizing and possible suitably prepd fossil-carbon, and makes carbon mix add
The technique of hydrogen-gasified, described method is characterised by, makes raw material based on plant that pulverizing is dried or former material based on waste material
Material individually or experiences pyrolytic process, described pyrolytic process or the temperature at about 170 DEG C to 270 DEG C with the form of specific group
In the range of carry out producing half carbon and pyrolysis gas under standard pressure, or about 270 DEG C to 300 DEG C within the temperature range of enter
Row is to produce biological carbon and pyrolysis gas, or carries out within the temperature range of higher than 300 DEG C, in described pyrolysis gas
Point leading to the second biomass pyrolysis reactor to carry out biomass pyrolytic, the another part in described pyrolysis gas leads to preheater
So that the stream adding hot gas is preheated, and obtained comprise about 60% to 65% elemental carbon described half carbon preferably with powder
Broken brown coal mixing, and the described biological carbon comprising the elemental carbon of about 65% to 80% mixes with the coal of pulverizing, based on biological carbon
The ratio of elemental carbon C ' and elemental carbon C based on fossil-carbon be preferably C ': C=1:1, by previous mixture or latter mixture
Supply, to the first hydro-gasifier reactor, wherein uses biological hydrogen to carry out complete hydrogenation gasifying process to produce rough gas and ash
Point, or carry out coal and biological carbon or the partial hydrogenation gasifying process of brown coal and half carbon with generation rough gas and thin coke,
And described thin coke leads to preheater to preheat adding hot gas stream, make to be obtained is cold in the second heat exchanger simultaneously
But rough gas experience sulfur removal technology, is subsequently isolated into hydrogen, residual gas and is made up of pure biological methane and ecological methane
Methane mixture, and the heat cooled down from described rough gas is led in preheater to preheat and to lead to adding hot gas
Produce steam waste heat boiler in the first heat exchanger, and a part for described methane lead to gas service pipes line and another
Part supply is to the 3rd biological hydrogen reaction of formation device, wherein in the reaction of biological methane with the vapours from described waste heat boiler
In, utilize by adding hot gas supply to the heat of described reaction, about 500 DEG C to 700 DEG C at a temperature of and at catalyst
In the presence of, form biological hydrogen and CO2Mixture, described mixture is separated into CO after cooling down in described waste heat boiler2With logical
The biological hydrogen of the carbon mix hydrogasification technique in described first reactor, and by described add hot gas in preheater pre-
Heat extremely carries out the temperature of about 800 DEG C to 1200 DEG C needed for biological hydrogen formation reaction in the 3rd reactor, and described preheating uses
It is supplied with the gas burner of the pyrolysis gas from described second biomass pyrolysis reactor and/or uses from described rough gas
The surplus hydrogen of middle recovery and use are supplied with the thin coke of grinding or carbon or the pulverized fuel combustor of biological carbon, and will
That thus heats adds the supply of hot gas stream to described 3rd reactor.
Method the most according to claim 1, it is characterised in that by half carbon and brown coal or the pulverizing of biological carbon and coal do
Dry mixture is supplied to described first reactor from carbon mix preparation facilities, in this carbon mix hydrogasification process first
Carrying out in the gas supplied from described interior ceiling portion the suspension bed under wandering in interior room, described gas is at about 2.5MPa
At a temperature of about 815 DEG C, the H of about 50% is comprised to the pressure of 7.0MPa2With 50% CH4, obtain in this process
Rough gas is transported to steam and coal gas separator, and it is de-that described rough gas removes dust and the gas being blended, especially experience at this
Sulfur, it is separated into the pure methane mixture and pure hydrogen being made up of biological methane and ecological methane afterwards, and Partial Conversion
Carbon mix be transported to the mistress of described first reactor, utilize at this hydrogen to be subjected to completely and convert to generate ash
With hydrogen+methane gas, or it is subjected to convert to generate thin coke and hydrogen+methane gas completely with biological hydrogen and hydrogen
Or it is partially converted into thin coke and described hydrogen+methane gas, and described hydrogen+methane gas is provided to described reactor
Interior room.
Method the most according to claim 1, it is characterised in that in described first high-pressure reactor, described carbon mix
Nozzle is used to supply to described reaction with the form of suspended substance after merging with the ratio of 1:2.5 to 1:3.5 with mineral oil
The highest region section being referred to as evaporating region of device, wherein under the pressure of about 6.8MPa and under the prevailing temperature of about 315 DEG C, institute
State oil to be evaporated and its steam is emitted into steam-coal gas separator together with pyrogen coal gas, make at this to be recovered and exist subsequently
During in condenser, the mineral oil of condensation is recycled back to the suspended substance preparation facilities of oil bag carbon, and make purified, especially de-
Rough gas after sulfur is separated into methane mixture and the pure hydrogen with biological hydrogen combination, and by falling at a temperature of about 300 DEG C
The carbon being dried and biological carbon particle delivery to the centre portion of described first reactor, wherein said granule leave described instead
Answer the bottom section of the second level being referred to as carbon hydrogasification of device the gas containing biological hydrogen stream in experience fluidisation, and at quilt
In the centre portion of the first order being referred to as carbon hydrogasification, carry out at the temperature of rising of about 650 DEG C and the pressure of 6.8MPa
Carbon and the degassing of biological carbon and partial hydrogenation gasify, then, in the fluid bed of the bottom section of described reactor, at 750 DEG C
Supply is used to make the carbon mix of Partial Conversion experience to biological hydrogen and the hydrogen of described bottom section at a temperature of 950 DEG C
Full hydrogasification.
4. according to the method according to any one of claim 1 and claim 2 and claim 3, it is characterised in that described in add
Hot gas be the material to described 3rd reactor be inert gas, preferably CO2, nitrogen, helium or argon, or have
The gas of high specific heat, or there is high boiling liquid, described in add hot gas and heat carried to described 3rd reactor and be used for
Biological methane and steam reaction, the amount of described heat be about 500 DEG C to 700 DEG C at a temperature of at Ni/Al2O3In the presence of catalyst
It is sufficient for biological hydrogen and CO2Form the about 165kJ/mol CH of reaction4。
Method the most according to claim 1, it is characterised in that from the biological hydrogen at a temperature of about 500 DEG C and CO2Heat mix
Compound, from the gas at a temperature of leaving about 600 DEG C of described preheater stream and from external system, especially
It is to be transported to described waste heat boiler from the heat of the TRT producing electric energy and heat energy.
Method the most according to claim 4, it is characterised in that take from the high-temperature hot of rough gas and supplied by solar collector
The heat answered is transported to described heating gas preheater.
Method the most according to claim 1, it is characterised in that in the Part I of described 3rd reactor, in reaction
In device pipe, at Ni/Al under the temperature range of about 500 DEG C to 900 DEG C and the pressure of 1.5MPa to 4.5MPa2O3Raney nickel
In the presence of generate biological hydrogen and CO2Reactant: biological methane and steam are by the heating of the heat of about 800 DEG C to 1200 DEG C of temperature
Gas stream is additionally heated.
8. according to the method according to any one of claim 1 and claim 7, it is characterised in that for described 3rd reaction
In device, the biological hydrogen of carbon monoxide and steam forms reaction, and in described biological hydrogen reaction of formation, admixture of gas is from the described 3rd
The Part I of reactor flow to the Part II of described 3rd reactor, and described Part II is lower than described Part I
Under temperature range run, or about 200 DEG C to 300 DEG C within the temperature range of use Cu-Zn/Al2O3Catalyst, or 350
DEG C to using Fe/Al in the high temperature range of 500 DEG C2O3Catalyst subsequently about 200 DEG C to 300 DEG C in the range of use Cu/
Al2O3Catalyst, or within the temperature range of 300 DEG C to 450 DEG C, use Fe2O3+Cr2O3Catalyst carries out described reaction.
9., for manufacturing biological methane and a system for ecological methane, consist of: carbon hydro-gasifier reactor, biological hydrogen
Reaction of formation device, steam and coal gas separator, biomass pyrolysis reactor, carbon mix preparation facilities, waste heat boiler, add steam
Body preheater, heat exchanger, conveyer, for pipeline and the pump of liquid, steam and gas, described system is characterised by, the
One carbon hydro-gasifier reactor (1) has the first entrance (18b) and the second entrance (26), and wherein the first entrance (18b) is used for hydrogen
Gas and the second entrance (26) are connected to the carbon mix preparation facilities (25) being connected with the second biomass pyrolysis reactor (2), institute
State the first reactor (1) have the first outlet (6) and second outlet (28), wherein second outlet (28) for thin coke and first
Outlet (6) is connected to steam and coal gas separator for rough gas, described first outlet (6) by the second heat exchanger (6a)
(5), described steam and coal gas separator (5) have the first hydrogen outlet (19), the second methane exports (20) and the 3rd waste material goes out
Mouth (17), described first hydrogen outlet (19) of wherein said separator (5) is divided into two pipelines (19a) and (19b), wherein
Pipeline (19a) is connected to described first entrance (18b) of described first reactor (1), and pipeline (19b) is connected to described preheating
The burner (14) of device (9), and described separator (5) second methane outlet (20) be additionally coupled to described 3rd hydrogen generate
Reactor (3), the first outlet (10b) of described 3rd hydrogen reaction of formation device (3) is connected to institute via described waste heat boiler (4)
Stating separator (8), the outlet of described separator (8) is connected to described first reactor (1) via pipeline (18a), described in addition
Waste heat boiler (4) has process steam outlet (11a) being connected to described 3rd reactor (3), and described 3rd reactor (3)
The second outlet be connected to the heat gas lines (10a) that is connected with described preheater (9), this outer heat-exchanger (6a) is via pipe
Line (7b), preheater (9) and pipeline (7c) are connected to described waste heat boiler (4).
System the most according to claim 9, it is characterised in that described second biomass pyrolysis reactor (2) has dry raw
Matter inlet and the biological carbon outlet being connected to described device (25), and be connected to be positioned at described heating gas preheater (9)
In gas burner (14) pyrolysis gas outlet (22a).
11. according to the system according to any one of claim 9 and claim 10, it is characterised in that described preheater (9) has
The 3rd heat exchanger (9a), described 3rd heat exchanger (9a) one end is had to be connected to described heat gas lines (10a) and another
Hold and be connected to be arranged on the nozzle (10d) of described 3rd reactor (3) porch via pipeline (10), and described preheater (9)
Equipped with being connected to the burner (14) of described second biomass pyrolysis reactor (2) via pipeline (22b) and via conveying
Machine (28a) is connected to the pulverized fuel combustor (15) of thin coke export (28), additionally, described preheater (9) is connected to described
Waste heat boiler (4).
12. systems according to claim 9, it is characterised in that described 3rd reactor (3) has inner tube (3a), institute
State inner tube (3a) and comprise the Raney nickel on a ceramic substrate of the load in the Part I being positioned at described 3rd reactor (3)
Ni/Al2O3, described Part I is connected to heating gas inlet (10d), and described pipe (3a) also comprises Cu-Zn/Al2O3Catalysis
Agent or Fe/Al2O3And Cu/Al2O3Catalyst or Fe2O3+Cr2O3Catalyst, described pipe is positioned at the second of described 3rd reactor
In part, and described 3rd reactor (3) has the entrance (20a) for biological methane, entrance (11a) for process steam
With for biological hydrogen and CO2The outlet (10b) of mixture.
13. systems according to claim 9, it is characterised in that described hydrogen and CO2Mixture separator (8) has and leads to
Air and/or the pure CO processing for downstream and/or sealing up for safekeeping2Outlet (10e).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PL412999A PL231090B1 (en) | 2015-07-02 | 2015-07-02 | Method and the system for the production of biomethane and ecomethane |
| PLP.412999 | 2015-07-02 |
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| CN106318417A true CN106318417A (en) | 2017-01-11 |
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| Country | Link |
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| CN (1) | CN106318417B (en) |
| PL (1) | PL231090B1 (en) |
| WO (1) | WO2017002096A1 (en) |
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| WO2012142488A2 (en) | 2011-04-15 | 2012-10-18 | Biogenic Reagents LLC | Methods and apparatus for enhancing the energy content of carbonaceous materials from pyrolysis |
| HRP20201795T1 (en) | 2012-05-07 | 2021-01-08 | Carbon Technology Holdings, LLC | Continuous process for producing biogenic activated carbon |
| WO2015061701A1 (en) | 2013-10-24 | 2015-04-30 | Biogenic Reagent Ventures, Llc | Methods and apparatus for producing activated carbon from biomass through carbonized ash intermediates |
| CA2977092C (en) | 2014-02-24 | 2022-12-13 | Biogenic Reagents Ventures, Llc | Highly mesoporous activated carbon |
| WO2016065357A1 (en) | 2014-10-24 | 2016-04-28 | Biogenic Reagent Ventures, Llc | Halogenated activated carbon compositions and methods of making and using same |
| PL424040A1 (en) * | 2017-12-22 | 2019-07-01 | Instytut Agrofizyki Im. Bohdana Dobrzańskiego Polskiej Akademii Nauk | Eco-friendly system for production of biomethane |
| IL279398B1 (en) | 2018-06-14 | 2025-05-01 | Carbon Tech Holdings Llc | Biogenic porous carbon silicon dioxide compositions and methods of making and using same |
| CN108946661B (en) * | 2018-07-04 | 2020-07-24 | 新奥科技发展有限公司 | Method and system for preparing hydrogen through biomass gasification |
| CN111154518A (en) * | 2019-04-12 | 2020-05-15 | 新能能源有限公司 | Coal hydro-gasification safety monitoring system and monitoring method thereof |
| CN110713844A (en) * | 2019-10-17 | 2020-01-21 | 中国科学院山西煤炭化学研究所 | Method for co-producing methane and light liquid tar by catalytic hydro-gasification two-step method |
| EP4328341A3 (en) | 2020-09-25 | 2024-07-17 | Carbon Technology Holdings, LLC | Bio-reduction of metal ores integrated with biomass pyrolysis |
| BR112023016141A2 (en) | 2021-02-18 | 2023-11-21 | Carbon Tech Holdings Llc | METALLURGICAL PRODUCTS WITH NEGATIVE CARBON |
| CN113403099A (en) * | 2021-04-12 | 2021-09-17 | 西北大学 | Medium-low temperature coal pyrolysis semicoke passivation method |
| EP4329955A4 (en) | 2021-04-27 | 2025-03-12 | Carbon Technology Holdings, LLC | Biocarbon compositions with optimized fixed carbon and processes for producing the same |
| EP4446443A3 (en) | 2021-07-09 | 2025-01-01 | Carbon Technology Holdings, LLC | Processes for producing biocarbon pellets with high fixed-carbon content and optimized reactivity, and biocarbon pellets obtained therefrom |
| WO2023014679A1 (en) * | 2021-08-02 | 2023-02-09 | Carbon Technology Holdings, LLC | Processes and systems for recapturing carbon from biomass pyrolysis liquids |
| CN113636524B (en) * | 2021-09-10 | 2025-02-11 | 山东恒昌聚材化工科技股份有限公司 | A gas conversion and purification device and method for producing high-purity hydrogen from biogas |
| CA3237226A1 (en) | 2021-11-12 | 2023-05-19 | Carbon Technology Holdings, LLC | Biocarbon compositions with optimized compositional parameters, and processes for producing the same |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060265953A1 (en) * | 2005-05-26 | 2006-11-30 | Arizona Public Service Company | Method and apparatus for producing methane from carbonaceous material |
| US20130023707A1 (en) * | 2009-11-18 | 2013-01-24 | Keefer Bowie | Method and system for biomass hydrogasification |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CA1300885C (en) * | 1986-08-26 | 1992-05-19 | Donald S. Scott | Hydrogasification of biomass to produce high yields of methane |
| NL1010288C2 (en) * | 1998-10-12 | 2000-04-13 | Stichting Energie | Method for the conversion of hydrogen into substitute natural gas. |
| US8915981B2 (en) * | 2009-04-07 | 2014-12-23 | Gas Technology Institute | Method for producing methane from biomass |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20060265953A1 (en) * | 2005-05-26 | 2006-11-30 | Arizona Public Service Company | Method and apparatus for producing methane from carbonaceous material |
| US20130023707A1 (en) * | 2009-11-18 | 2013-01-24 | Keefer Bowie | Method and system for biomass hydrogasification |
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| WO2017002096A1 (en) | 2017-01-05 |
| PL412999A1 (en) | 2017-01-16 |
| CN106318417B (en) | 2020-10-27 |
| PL231090B1 (en) | 2019-01-31 |
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