CN113773876A - Method and system for preparing hydrogen by melting and gasifying organic wastes by using redox method - Google Patents
Method and system for preparing hydrogen by melting and gasifying organic wastes by using redox method Download PDFInfo
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- CN113773876A CN113773876A CN202111109937.9A CN202111109937A CN113773876A CN 113773876 A CN113773876 A CN 113773876A CN 202111109937 A CN202111109937 A CN 202111109937A CN 113773876 A CN113773876 A CN 113773876A
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- pressure swing
- swing adsorption
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 101
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 101
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 88
- 238000000034 method Methods 0.000 title claims abstract description 62
- 238000002844 melting Methods 0.000 title claims abstract description 57
- 230000008018 melting Effects 0.000 title claims abstract description 57
- 239000010815 organic waste Substances 0.000 title claims abstract description 24
- 238000001179 sorption measurement Methods 0.000 claims abstract description 115
- 239000007789 gas Substances 0.000 claims abstract description 91
- 238000000197 pyrolysis Methods 0.000 claims abstract description 49
- 239000002910 solid waste Substances 0.000 claims abstract description 49
- 238000002309 gasification Methods 0.000 claims abstract description 47
- 239000003054 catalyst Substances 0.000 claims abstract description 39
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 36
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 32
- 238000000746 purification Methods 0.000 claims abstract description 31
- 239000000292 calcium oxide Substances 0.000 claims abstract description 16
- 235000012255 calcium oxide Nutrition 0.000 claims abstract description 16
- 238000012545 processing Methods 0.000 claims abstract description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 22
- 238000003795 desorption Methods 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 16
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 238000009826 distribution Methods 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 238000010791 quenching Methods 0.000 claims description 9
- 230000000171 quenching effect Effects 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 8
- 239000002893 slag Substances 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 7
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- 239000002241 glass-ceramic Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 4
- 238000007872 degassing Methods 0.000 claims description 3
- 239000000155 melt Substances 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 abstract description 15
- 238000006243 chemical reaction Methods 0.000 abstract description 7
- 230000033116 oxidation-reduction process Effects 0.000 abstract description 5
- 238000006479 redox reaction Methods 0.000 abstract description 5
- 231100000614 poison Toxicity 0.000 abstract description 3
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- 230000009471 action Effects 0.000 description 5
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- 230000000694 effects Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000006378 damage Effects 0.000 description 3
- 230000004992 fission Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 231100000331 toxic Toxicity 0.000 description 3
- 230000002588 toxic effect Effects 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
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- 241001417527 Pempheridae Species 0.000 description 1
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- 150000007824 aliphatic compounds Chemical class 0.000 description 1
- 229910001514 alkali metal chloride Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
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- 238000003763 carbonization Methods 0.000 description 1
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- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000010169 landfilling Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000010309 melting process Methods 0.000 description 1
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- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
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- 238000006722 reduction reaction Methods 0.000 description 1
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- 238000004056 waste incineration Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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- 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
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- 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
- C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C—CHEMISTRY; METALLURGY
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- 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
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- C10J3/725—Redox processes
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- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
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- 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
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- 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
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- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- 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
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- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
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- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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- C10J2300/0913—Carbonaceous raw material
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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- 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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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- C10J2300/0976—Water as steam
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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- 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
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- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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- C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- General Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
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- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a method and a system for preparing hydrogen by melting and gasifying organic wastes by using a redox method, wherein the system comprises a low-temperature pyrolysis furnace, a hydrogen-generating furnace and a hydrogen-generating furnace, wherein the low-temperature pyrolysis furnace is used for generating a carbon redox catalyst and first gas; the melting gasification furnace is used for melting the carbon redox catalyst, the quicklime and the second organic solid waste to generate second gas; the purification device is used for obtaining and purifying the gas to obtain hydrogen; the secondary pressure swing adsorption device is connected with the purification device to purify the hydrogen; and the control unit is connected with the low-temperature pyrolysis furnace, the melting gasification furnace, the purification device and the secondary pressure swing adsorption device. The application provides a system adopts controller unit cooperative control, utilizes the low temperature pyrolysis stove to generate carbon oxidation reduction catalyst to first organic solid waste pyrolysis, utilizes the melting gasifier to carry out the redox reaction, and the reaction produces gas and obtains purification hydrogen through purifying and secondary pressure swing adsorption, realizes equipment cooperative operation in the processing procedure, generates pure hydrogen, has reduced poisonous and harmful gas and has discharged.
Description
Technical Field
The invention relates to the technical field of organic waste treatment, in particular to a method and a system for preparing hydrogen by melting and gasifying organic waste by using a redox method.
Background
The organic waste (mainly organic solid waste) refers to household garbage, market garbage, scattered garbage, hospital garbage, construction garbage, street sweeper and the like generated by residents in daily life. The existing solutions mainly include incineration, sanitary landfill, composting and the like. As the population of cities increases, the amount of municipal waste produced increases, which leads to an increase in the transportation cost of organic solid waste and a decrease in the land available for sanitary landfill, and thus the operability of solutions such as sanitary landfill and composting is becoming lower.
The existing waste incineration technology is mainly a process for rapidly oxidizing organic solid waste, and a large amount of light and heat and various toxic and harmful gases are generated in the process, so that the ecological environment is further deteriorated.
Disclosure of Invention
In order to solve the technical problems mentioned in the background art or at least partially solve the technical problems, the application provides a method and a system for producing hydrogen by melting and gasifying organic wastes through a redox method, which can effectively treat solid wastes and simultaneously reduce the emission of toxic and harmful gases and generate hydrogen, thereby avoiding the damage to the environment.
In a first aspect, the present application provides a system for producing hydrogen by melt-gasification of organic wastes using a redox process, comprising:
a low temperature pyrolysis furnace for processing the first organic solid waste to produce a carbon redox catalyst and a first gas;
the conveying device is connected with the material output end of the low-temperature pyrolysis furnace to obtain the carbon redox catalyst;
the material input end of the melting gasification furnace is arranged at the top of the melting gasification furnace and is connected with the material output end of the conveying device to obtain and melt the carbon redox catalyst, the quick lime and the second organic solid waste so as to generate second gas; a spiral fan and a steam input end are fixed on the side wall of the melting gasification furnace, and the output end of the spiral fan obliquely extends to the inner side of the side wall of the melting gasification furnace to form spiral ascending airflow;
the purification device is respectively connected with the gas output end of the melting gasifier and the gas output end of the low-temperature pyrolysis furnace, and is used for respectively obtaining and purifying the second gas and the first gas to obtain hydrogen;
the secondary pressure swing adsorption device is connected with the output end of the purification device to purify the hydrogen;
and the control unit is respectively electrically connected with the low-temperature pyrolysis furnace, the conveying device, the melting gasification furnace, the purifying device and the secondary pressure swing adsorption device.
The first output end of the air distribution machine is connected with the input end of the low-temperature pyrolysis furnace, and the second output end of the air distribution machine is connected with the gate valve unit belonging to the melting gasification furnace and used for injecting nitrogen into the low-temperature pyrolysis furnace and the gate valve unit respectively;
and a third output end of the air distribution machine is connected with a second input end of the melting gasification furnace and used for injecting oxygen.
Further, the conveying device comprises a conveying belt and a lifting machine;
the conveyer belt is connected with the material output end of the low-temperature pyrolysis furnace, the tail end of the conveyer belt is connected with the input end of the hoister, and the output end of the hoister is connected with the material input end of the melting gasification furnace.
Further, a water quenching unit is arranged on the inner side of the bottom of the melting gasification furnace;
and at least two spiral fans forming spiral ascending air flows are arranged on the side wall of the melting gasification furnace at equal intervals.
Further, the secondary pressure swing adsorption apparatus includes:
the input end of the first-stage pressure swing adsorption unit is connected with the output end of the purification device through a first separator;
the input of the second-stage pressure swing adsorption unit is connected with the first output end of the first-stage pressure swing adsorption unit through the oil removal tower and the first heater in sequence; the first output end of the second-stage pressure swing adsorption unit is connected with the gas buffer tank through the vacuum desorption unit.
Furthermore, the secondary pressure swing adsorption device also comprises a three-stage pressure swing adsorption unit, wherein the input end of the three-stage pressure swing adsorption unit is connected with the second output end of the two-stage pressure swing adsorption unit through a cooler; the output end of the three-stage pressure swing adsorption unit is connected with the second heater, the dryer and the second separator in sequence;
the secondary pressure swing adsorption device also comprises a forward air release buffer tank, a desorption air buffer tank and a steam unit;
the second output end of the first-stage pressure swing adsorption unit, the second output end of the second-stage pressure swing adsorption unit and the second output end of the third-stage pressure swing adsorption unit are respectively connected with the input end of the forward degassing buffer tank;
the third output end of the first-stage pressure swing adsorption unit, the third output end of the second-stage pressure swing adsorption unit and the third output end of the third-stage pressure swing adsorption unit are respectively connected with the input end of a desorption gas buffer tank, and the output end of the desorption gas buffer tank is connected with a second heater;
the steam unit is respectively connected with the first heater and the second heater.
In a second aspect, the present application also provides a method for producing hydrogen by melt gasification of organic waste by using a redox method, which is applied to the system of the first aspect, and comprises the following steps:
pyrolyzing the first organic solid waste in a low-temperature pyrolysis furnace to generate a carbon redox catalyst and first gas;
melting carbon redox catalyst, quicklime and second organic solid waste in a melting gasifier to generate second gas;
the purifying device purifies the first gas and the second gas to obtain hydrogen;
the secondary pressure swing adsorption device is used for secondary pressure swing adsorption of hydrogen to generate purified hydrogen.
Further, before pyrolyzing the first organic solid waste at low temperature, the method further comprises:
the air separation machine separates nitrogen and oxygen in the air;
injecting nitrogen into a multistage gate valve belonging to the low-temperature pyrolysis furnace and the melting gasification furnace;
injecting oxygen into the mixed tuyere to which the melter-gasifier belongs.
Further, the melting gasifier melts the carbon redox catalyst, the quicklime and the second organic solid waste to generate a second gas, and specifically comprises:
drying and oxidizing the carbon redox catalyst, the quicklime and the second organic solid waste to generate second gas and liquid slag;
water quenching the liquid slag to produce the glass ceramic body.
Further, the secondary pressure swing adsorption device is used for secondary pressure swing adsorption of hydrogen to generate purified hydrogen, and the method specifically comprises the following steps:
desulfurizing and purifying the hydrogen to obtain desulfurized hydrogen;
performing primary pressure swing adsorption and secondary purification on the desulfurized hydrogen to obtain primary pressure swing hydrogen;
and (4) performing secondary pressure swing adsorption and pressure swing hydrogen to obtain purified hydrogen.
Compared with the prior art, the technical scheme provided by the embodiment of the application has the following advantages: the application provides a method and system for utilizing redox method to make hydrogen to organic waste melt gasification, this system utilizes the controller unit at first to carry out the pyrolysis through the low temperature pyrolysis stove to first organic solid waste, generate the carbon oxidation reduction catalyst, later utilize conveyer with carbon oxidation reduction catalyst and lime, the second organic solid waste is carried to the melter gasifier and is carried out the redox reaction, and pass through purification and secondary pressure swing adsorption with the produced gas of pyrolysis process and redox process, obtain pure hydrogen, thereby in carrying out the thermal decomposition processing procedure to organic solid waste, utilize the control unit to realize the interoperation between the equipment, poisonous and harmful gas emission has been reduced effectively when generating pure hydrogen, the destruction to the environment has been avoided.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the invention and together with the description, serve to explain the principles of the invention.
Fig. 1 is a schematic structural diagram of a system for producing hydrogen by melt gasification of organic wastes through a redox method according to an embodiment of the present invention.
FIG. 2 is a schematic structural diagram of a secondary pressure swing adsorption apparatus in a system for producing hydrogen by melt gasification of organic wastes through a redox process according to an embodiment of the present invention.
Fig. 3 is a schematic connection diagram of a melter-gasifier and a purification apparatus in a system for producing hydrogen by melt-gasifying organic wastes through a redox method according to an embodiment of the present invention.
FIG. 4 is a schematic flow diagram of a method for producing hydrogen by melt gasification of organic wastes through a redox process according to an embodiment of the present invention.
FIG. 5 is a schematic flow chart of another method for producing hydrogen by melt gasification of organic wastes through a redox method according to an embodiment of the present invention.
FIG. 6 is a schematic flow chart of a melting process in a method for producing hydrogen by melting and gasifying organic wastes by using a redox method, which is provided by an embodiment of the invention.
FIG. 7 is a schematic flow chart of secondary pressure swing adsorption in a method for producing hydrogen by melt gasification of organic wastes through a redox method according to an embodiment of the present invention.
In the figure: 1. a low temperature pyrolysis furnace; 2. a conveying device; 3. a melter-gasifier; 4. a helical fan; 5. a steam input; 6. a purification device; 7. a secondary pressure swing adsorption unit; 8. a control unit; 9. an air distribution machine; 10. a gate valve unit; 11. a water quenching unit; 12. a first-stage pressure swing adsorption unit; 13. a first separator; 14. a secondary pressure swing adsorption unit; 15. an oil removal tower; 16. a first heater; 17. a vacuum analysis unit; 18. a three-stage pressure swing adsorption unit; 19. a second heater; 20. a dryer; 21. a second separator; 22. a forward venting buffer tank; 23. a desorption gas buffer tank; 24. a steam unit; 25. a gas buffer tank; 26. a gas purification unit; 27. a CO conversion unit; 28. an acid gas removal unit.
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
Detailed Description
To make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings, and it is apparent that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
At present, the main modes of incineration, sanitary landfill, composting and the like are mainly adopted for the garbage such as organic solid waste and the like. But with the increase in the transportation costs of organic solid wastes, the time and mechanical costs of composting, and the decrease in land available for landfilling, the feasibility of sanitary landfills and composting approaches has become less and less feasible.
The nature of the process of burning organic solid wastes belongs to a redox reaction, and a large amount of light and heat are generated in the process and multiple toxic and harmful gases are generated along with the light and the heat, so that the ecological environment pollution is aggravated, a large amount of renewable resources are lost, and the sustainable development of the environment and the economy is not facilitated.
In order to reduce the pollution to the environment caused by burning the organic solid waste and ensure the sustainable development of the environment, the application provides a method and a system for preparing hydrogen by melting and gasifying the organic solid waste by using a redox method. In order to facilitate understanding of the embodiments of the present invention, a system for producing hydrogen by melt-gasification of organic solid wastes using a redox method will be described in detail.
Example one
As shown in fig. 1, 2 and 3, the system for producing hydrogen by melt-gasification of organic solid waste by using a redox method includes:
a low-temperature pyrolysis furnace 1 for processing the first organic solid waste to generate a carbon redox catalyst and a first gas; the first organic solid waste, such as used tires, dried organic sludge, etc., is subjected to low-temperature anaerobic pyrolysis in a low-temperature pyrolysis furnace 1 at a temperature of about 500 to 700 ℃, and then carbonized to produce a carbon redox catalyst.
The conveying device 2 is connected with the material output end of the low-temperature pyrolysis furnace 1 to obtain the carbon redox catalyst; the conveying device 2 includes, but is not limited to, a conveyor belt and a lifter.
A material input end of the melter-gasifier 3 is arranged at the top of the melter-gasifier 3, and is connected with a material output end of the conveyer 2 to obtain and melt a carbon redox catalyst, quicklime and second organic solid waste to generate second gas; in a preferred embodiment, the melter-gasifier 3 is a fixed-bed vertical reactor. The carbon redox catalyst, the quicklime and the second organic solid waste are poured into the melting gasification furnace 3 and then are in a mixed state, and the processes of drying, oxidative decomposition and reduction melting are sequentially carried out. It is to be added here that the above-mentioned carbon redox catalyst is mixed with the second organic solid waste in a mass ratio of 1:5, accompanied by limestone as a co-solvent.
A spiral fan 4 and a steam input end 5 are fixed on the side wall of the melting gasification furnace 3, and the output end of the spiral fan 4 extends obliquely to the inner side of the side wall of the melting gasification furnace 3 to form spiral ascending airflow; specifically, the helical fan 4 is arranged at the bottom of the melter-gasifier 3 and injects air obliquely, and forms a tornado-state helical wind (the pressure is more than 10Mpa) under the action of the furnace top expansion body, so as to drive the steam input from the steam input end 5 to form hot air flow to react with the mixture.
It is added here that the oxidation reaction comprises the following stages depending on the reaction temperature:
100 ℃ -200 ℃: drying; the physical water is removed.
250 ℃ C: deoxidizing; eliminating water component; start of elimination of H2S gasification stage (oxidation reaction):
340℃：CH4and the aliphatic compounds started to fission at 380 ℃, and the organic matter was carbonized.
400 ℃ -600 ℃: C-O and C-N compound fission; asphaltenes transform tar.
The temperature is higher than 600 ℃: asphaltenes fission into thermally stable chain gaseous hydrocarbons; and (3) synthesizing aromatic hydrocarbon.
800-1300 ℃: gasifying; the halogen is completely in the vapor state (e.g., alkali metal chloride or HCI).
The reduction melting stage further comprises:
1400-2000 deg.C: the aromatics and organic compounds begin to decompose completely and the minerals melt. Finally, the second gas and the liquid slag are generated.
The purification device 6 is respectively connected with the gas output end of the melting gasifier 3 and the gas output end of the low-temperature pyrolysis furnace 1, and is used for respectively obtaining and purifying the second gas and the first gas to obtain hydrogen;
specifically, the purification apparatus 6 includes a gas purification unit 26, a CO conversion unit 27, and an acid gas removal unit 28, which are connected in series. Wherein the first gas and the second gas contain hydrogen, other gases and impurities. The gas purification unit 26 mainly functions to primarily purify impurities in the first gas and the second gas. The impurities are discharged and returned to the furnace through the bottom of the purifying device 6.
The CO conversion unit is used for combusting CO mixed in the gas to generate CO2Then gas and CO2Preliminary desulfurization and CO removal by the acid gas removal unit 282。
And the secondary pressure swing adsorption device 7 is connected with the output end of the purification device 6 to purify the hydrogen. The pressure swing adsorption has the function of purifying hydrogen by utilizing different adsorption capacities of adsorbents in the adsorption device on various components in impure hydrogen.
And the control unit 8 is respectively electrically connected with the low-temperature pyrolysis furnace 1, the conveying device 2, the melting gasification furnace 3, the purifying device 6 and the secondary pressure swing adsorption device 7.
Specifically, the control unit 8 includes, but is not limited to, a single chip microcomputer for controlling the temperature, time and atmosphere of the carbonization of the first organic solid waste through the electrical connection with the low-temperature pyrolysis furnace 1.
The control unit 8 is electrically connected to the melter-gasifier 3, and sets different ratio moduli according to the components of the second organic solid waste sample, thereby controlling the entry rate of the carbon redox catalyst. Meanwhile, in an ideal state, the wind pressure generated by the helical fan 4 in the melting gasification furnace 3 is more than or equal to 10Mpa, and the wind quantity is more than or equal to 415m3H is used as the reference value. The control unit 8 and the pressure sensor at the top of the melter-gasifier 3 acquire the air pressure and the air volume, and maintain the stability of the air pressure and the air volume by controlling the rotating speed of the spiral fan 4.
The application provides a method and system for utilizing redox method to make hydrogen to organic waste melt gasification, this system utilizes the controller unit at first to carry out the pyrolysis through the low temperature pyrolysis stove to first organic solid waste, generate the carbon oxidation reduction catalyst, later utilize conveyer with carbon oxidation reduction catalyst and lime, the second organic solid waste is carried to the melter gasifier and is carried out the redox reaction, and pass through purification and secondary pressure swing adsorption with the produced gas of pyrolysis process and redox process, obtain pure hydrogen, thereby in carrying out the thermal decomposition processing procedure to organic solid waste, utilize the control unit to realize the interoperation between the equipment, poisonous and harmful gas emission has been reduced effectively when generating pure hydrogen, the destruction to the environment has been avoided.
Example two
On the basis of the first embodiment, the system for producing hydrogen by melting and gasifying organic wastes through a redox method further comprises an air distribution machine 9, wherein a first output end of the air distribution machine 9 is connected with an input end of the low-temperature pyrolysis furnace 1 so as to prevent gas leakage in the low-temperature pyrolysis furnace 1. A second output end of the air distribution machine 9 is connected with a gate valve unit 10 belonging to the melting gasification furnace 3 and is used for respectively injecting nitrogen into the low-temperature pyrolysis furnace 1 and the gate valve unit 10;
in a preferred embodiment, the gate valve unit 10 employs a charging damper, which includes at least a two-stage gate valve structure, a material support structure, a fire prevention and closure mechanism; and nitrogen is filled between the multi-stage gate valve systems to ensure that the gas in the furnace cannot leak, and further ensure that the carbon redox catalyst, the quicklime and the second organic solid waste fall from top to bottom.
The third output end of the air distribution machine 9 is connected with the second input end of the melting gasification furnace 3 and is used for injecting oxygen. Specifically, the bottom of the melter-gasifier 3 is provided with an air mixing port, oxygen separated by the air separation machine 9 is injected into the melter-gasifier 3 through the air mixing port, and a tornado state is formed under the action of the helical fan 4, so as to meet the oxygen content required by the oxidation reaction in the melter-gasifier 3.
Further, the conveying device 2 comprises a conveying belt and a lifter;
the conveyer belt is connected with the material output end of the low-temperature pyrolysis furnace 1, the tail end of the conveyer belt is connected with the input end of the hoister, and the output end of the hoister is connected with the material input end of the melting gasification furnace 3.
Further, a water quenching unit 11 is arranged on the inner side of the bottom of the melter-gasifier 3; the water quenching unit 11 is used for performing a water quenching process on the liquid slag generated in the reduction melting stage to form a glass ceramic body.
In a preferred embodiment, the control unit 8 is electrically connected to the air distribution machine 9, the charging throttle, and the elevator, respectively, for controlling the respective operating states. Specifically, the control unit 8 controls the air separation machine 9 to adjust the speed of separating and conveying nitrogen and oxygen; the control unit 8 adjusts the descending rate of the carbon redox catalyst, the quicklime and the second organic solid waste by controlling a charging throttle valve; the control unit 8 controls the lifting motor to adjust the transmission rate of the carbon redox catalyst, the quicklime and the second organic solid waste by the lifting motor.
At least two helical fans 4 forming helical updraft are arranged on the side wall of the melter-gasifier 3 at equal intervals. The effect of the tornado is improved by arranging at least two helical fans 4.
Further, the control unit 8 performs cooperative operations among the different devices by performing distributed control of the low-temperature pyrolysis furnace 1, the conveyor 2, the melter-gasifier 3, the purification device 6, the secondary pressure swing adsorption device 7, the air classifier 9, the charging damper, and the elevator.
EXAMPLE III
In the system for producing hydrogen by melt-gasification of organic waste by using a redox process according to the first embodiment of the present invention, the secondary pressure swing adsorption device 7 includes:
the input end of the first-stage pressure swing adsorption unit 12 is connected with the output end of the purification device 6 through a first separator 13; the first separator 13 is used for desulfurization purification and filtration of water in the impure hydrogen, and then the mixed gas is purified by the first pressure swing adsorption unit 12, wherein the hydrogen after the first pressure swing adsorption needs to be subjected to gas composition measurement to identify the purification effect.
The input of the secondary pressure swing adsorption unit 14 is connected with the first output end of the primary pressure swing adsorption unit 12 through an oil removal tower 15 and a first heater 16 in sequence; a first output end of the two-stage pressure swing adsorption unit 14 is connected with the gas buffer tank 25 through the vacuum desorption unit 17. The oil removing tower 15 is used for removing impurities remained in the first-stage pressure swing adsorption hydrogen through the solvent. And the first heater 16 is used for heating the hydrogen after the first pressure swing adsorption so as to improve the impurity removal effect of the solvent.
The secondary pressure swing adsorption unit 14 performs secondary purification on the primary desulfurized hydrogen, and then performs hydrogen component measurement again by using the vacuum desorption unit 17 to obtain purified hydrogen, and the purified hydrogen is injected into the gas buffer tank 25.
In a preferred embodiment, the secondary pressure swing adsorption device 7 further comprises a three-stage pressure swing adsorption unit 18, wherein an input end of the three-stage pressure swing adsorption unit 18 is connected with a second output end of the two-stage pressure swing adsorption unit 14 through a cooler; the output end of the three-stage pressure swing adsorption unit 18 is connected with the dryer 20 and the second separator 21 in sequence;
the hydrogen after the second-stage pressure swing adsorption is cooled by a cooler and is subjected to the third-stage pressure swing adsorption by the third-stage pressure swing adsorption unit 18.
The secondary pressure swing adsorption device 7 also comprises a forward air release buffer tank 22, a desorption gas buffer tank 23 and a steam unit 24;
the second output end of the first-stage pressure swing adsorption unit 12, the second output end of the second-stage pressure swing adsorption unit 14 and the second output end of the third-stage pressure swing adsorption unit 18 are respectively connected with the input end of the forward degassing buffer tank 22; the purpose of the forward vent buffer tank 22 is to prevent the reactions in the first pressure swing adsorption unit 12, the second pressure swing adsorption unit 14, and the third pressure swing adsorption unit 18 from being too fast.
The third output end of the first-stage pressure swing adsorption unit 12, the third output end of the second-stage pressure swing adsorption unit 14 and the third output end of the third-stage pressure swing adsorption unit 18 are respectively connected with the input end of a desorption gas buffer tank 23, and the output end of the desorption gas buffer tank 23 is connected with a second heater 19;
the steam unit 24 is connected to the first heater 16 and the second heater 19, respectively. It should be added here that the desorption gas buffer tank 23 is connected to the first pressure swing adsorption unit 12, the second pressure swing adsorption unit 14, and the third pressure swing adsorption unit 18 to receive the gas generated therefrom and to prepare the catalyst required for purifying hydrogen using the second heater 19. The hydrogen after the three-stage pressure swing adsorption is mixed with a catalyst, and after dehydrogenation and drying, the waste water is separated by a second separator 21 to obtain dry pure hydrogen.
Example four
A method for producing hydrogen by melt gasification of organic wastes using a redox method, as shown in fig. 4, comprising:
s01: pyrolyzing the first organic solid waste in a low-temperature pyrolysis furnace to generate a carbon redox catalyst and first gas; the low-temperature pyrolysis furnace is used for carbonizing the first organic solid waste through low-temperature anaerobic pyrolysis at the temperature of 500-700 ℃ to generate the carbon redox catalyst.
S02: melting carbon redox catalyst, quicklime and second organic solid waste in a melting gasifier to generate second gas; the redox reaction occurring in the melter gasifier has already been described in the first embodiment and will not be described here.
It is to be added here that the carbon redox catalyst is transported from the low-temperature pyrolysis furnace to the top of the melter-gasifier by means of a transport device. While the conveyor adds limestone and the second organic solid waste during the conveying process.
S03: the purifying device purifies the first gas and the second gas to obtain hydrogen; the first gas and the second gas include hydrogen, acid gas, impurities, and the like. The purification process mainly comprises the steps of gas purification, CO conversion, high-pressure acid gas removal and the like. Wherein the impurities are absorbed by deslagging and returning to the furnace. The acid gas is recycled to the sludge by high pressure acid gas removal.
S04: the secondary pressure swing adsorption device is used for secondary pressure swing adsorption of hydrogen to generate purified hydrogen. The third specific purification process example is already described, and is not repeated here.
The method for preparing hydrogen by melting and gasifying organic wastes by using the redox method is applied to the system and adopts the same technical means to achieve the same technical effect, and the details are not repeated.
EXAMPLE five
In addition to example five, as further shown in fig. 5 and 6, before the low-temperature pyrolysis of the first organic solid waste, the method further includes:
s05: the air separation machine separates nitrogen and oxygen in the air;
s06: injecting nitrogen into a multistage gate valve belonging to the low-temperature pyrolysis furnace and the melting gasification furnace;
s07: injecting oxygen into the mixed tuyere to which the melter-gasifier belongs.
It should be added here that step S02 specifically includes:
s021: drying and oxidizing the carbon redox catalyst, the quicklime and the second organic solid waste to generate second gas and liquid slag;
s022: water quenching the liquid slag to produce the glass ceramic body.
EXAMPLE six
On the basis of the fourth embodiment, as further shown in fig. 7, step S04 specifically includes:
s041: desulfurizing and purifying the hydrogen to obtain desulfurized hydrogen; the first-stage pressure swing adsorption unit is used for simultaneously separating the wastewater in the process of desulfurizing the impure hydrogen through the first separator.
S042: after the first-stage pressure swing adsorption and the secondary purification of the desulfurized hydrogen, the first-stage pressure swing adsorption hydrogen is obtained; it is necessary to supplement that after the first pressure swing adsorption of hydrogen is obtained, the hydrogen composition must be measured to determine the purity of the purified hydrogen.
S043: and (3) performing secondary pressure swing adsorption and primary pressure swing adsorption on hydrogen to obtain purified hydrogen. And (4) measuring the hydrogen component again by using a vacuum analysis unit to obtain purified hydrogen, and injecting the purified hydrogen into the gas buffer tank. It is necessary to supplement that before the two-stage pressure swing adsorption, and after the pressure swing adsorption hydrogen is heated by the first heater connected with the steam unit, the effect of removing impurities in the first-stage pressure swing adsorption hydrogen by the solvent in the oil removing tower is improved.
In an optional embodiment, after step S043, the method further includes:
s044: and purifying the hydrogen by three-stage pressure swing adsorption to obtain pure hydrogen. The purified hydrogen needs to be cooled by a cooler.
S045: and receiving the catalyst generated in the desorption gas buffer tank, dehydrogenating, drying and carrying out secondary separation.
It is supplemented here that the stripping gas buffer tank is connected to the first pressure swing adsorption unit, the second pressure swing adsorption unit and the third pressure swing adsorption unit to receive the moisture-containing hydrogen generated therefrom and to be heated by the second heater to prepare the raw material gas required for purifying hydrogen. And separating the dehydrogenated and dried hydrogen from the wastewater by a second separator to obtain the dried pure hydrogen.
It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
The foregoing are merely exemplary embodiments of the present invention, which enable those skilled in the art to understand or practice the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A system for producing hydrogen by melting and gasifying organic wastes by using a redox method is characterized by comprising the following steps:
a low temperature pyrolysis furnace for processing the first organic solid waste to produce a carbon redox catalyst and a first gas;
the conveying device is connected with the material output end of the low-temperature pyrolysis furnace to obtain the carbon redox catalyst;
the material input end of the melting gasification furnace is arranged at the top of the melting gasification furnace and is connected with the material output end of the conveying device so as to obtain and melt the carbon redox catalyst, the quick lime and the second organic solid waste, and second gas is generated; a spiral fan and a steam input end are fixed on the side wall of the melting gasification furnace, and the output end of the spiral fan extends to the inner side of the side wall of the melting gasification furnace in an inclined manner to form spiral ascending airflow;
the purification device is respectively connected with the gas output end of the melting gasifier and the gas output end of the low-temperature pyrolysis furnace, and is used for respectively obtaining and purifying the second gas and the first gas to obtain hydrogen;
the secondary pressure swing adsorption device is connected with the output end of the purification device to purify the hydrogen;
and the control unit is respectively electrically connected with the low-temperature pyrolysis furnace, the conveying device, the melting gasification furnace, the purifying device and the secondary pressure swing adsorption device.
2. The system of claim 1, wherein: the first output end of the air distribution machine is connected with the input end of the low-temperature pyrolysis furnace, and the second output end of the air distribution machine is connected with the gate valve unit belonging to the melting gasification furnace and used for injecting nitrogen into the low-temperature pyrolysis furnace and the gate valve unit respectively;
and a third output end of the air distribution machine is connected with a second input end of the melting gasification furnace and used for injecting oxygen.
3. The system of claim 1, wherein: the conveying device comprises a conveying belt and a lifting machine;
the conveyer belt with the material output of low temperature pyrolysis oven is connected, the conveyer belt end with the input of lifting machine is connected, the output of lifting machine with the material input of melter gasifier is connected.
4. The system of claim 1, wherein: a water quenching unit is arranged on the inner side of the bottom of the melting gasification furnace;
and at least two spiral fans forming spiral ascending air flow are arranged on the side wall of the melting gasification furnace at equal intervals.
5. The system of claim 1, wherein the secondary pressure swing adsorption device comprises:
the input end of the first-stage pressure swing adsorption unit is connected with the output end of the purification device through a first separator;
the input of the second-stage pressure swing adsorption unit is connected with the first output end of the first-stage pressure swing adsorption unit through an oil removal tower and a first heater in sequence; and the first output end of the second-stage pressure swing adsorption unit is connected with the gas buffer tank through the vacuum desorption unit.
6. The system of claim 5, wherein: the secondary pressure swing adsorption device also comprises a three-stage pressure swing adsorption unit, and the input end of the three-stage pressure swing adsorption unit is connected with the second output end of the two-stage pressure swing adsorption unit through a cooler; the output end of the three-stage pressure swing adsorption unit is connected with the second heater, the dryer and the second separator in sequence;
the secondary pressure swing adsorption device also comprises a forward air release buffer tank, a desorption air buffer tank and a steam unit;
the second output end of the first-stage pressure swing adsorption unit, the second output end of the second-stage pressure swing adsorption unit and the second output end of the third-stage pressure swing adsorption unit are respectively connected with the input end of the forward degassing buffer tank;
the third output end of the first-stage pressure swing adsorption unit, the third output end of the second-stage pressure swing adsorption unit and the third output end of the third-stage pressure swing adsorption unit are respectively connected with the input end of the desorption gas buffer tank, and the output end of the desorption gas buffer tank is connected with the second heater;
the steam unit is connected with the first heater and the second heater respectively.
7. A method for producing hydrogen by melting and gasifying organic wastes by using a redox method, which is applied to the system of any one of claims 1 to 6, and is characterized by comprising the following steps:
pyrolyzing the first organic solid waste in a low-temperature pyrolysis furnace to generate a carbon redox catalyst and first gas;
the melting gasification furnace melts the carbon redox catalyst, the quicklime and the second organic solid waste to generate second gas;
purifying the first gas and the second gas by a purifying device to obtain hydrogen;
and the secondary pressure swing adsorption device is used for carrying out secondary pressure swing adsorption on the hydrogen to generate purified hydrogen.
8. The method of claim 7, further comprising, prior to the low temperature pyrolysis of the first organic solid waste:
the air separation machine separates nitrogen and oxygen in the air;
injecting nitrogen into the low-temperature pyrolysis furnace and the multistage gate valve belonging to the melting gasification furnace;
injecting oxygen into the tuyere mixture to which the melter-gasifier belongs.
9. The method of claim 7, wherein the melter-gasifier melts the carbon redox catalyst, the quicklime, and the second organic solid waste to generate a second gas, and specifically comprises:
drying and carrying out redox reduction on the carbon redox catalyst, the quicklime and the second organic solid waste to generate a second gas and liquid slag;
water quenching the liquid slag to produce a glass ceramic body.
10. The method of claim 7, wherein the secondary pressure swing adsorption unit pressure swing adsorbs the hydrogen gas a second time to produce purified hydrogen gas, comprising:
desulfurizing and purifying the hydrogen to obtain desulfurized hydrogen;
performing primary pressure swing adsorption and secondary purification on the desulfurized hydrogen to obtain primary pressure swing adsorption hydrogen;
and performing secondary pressure swing adsorption on the primary pressure swing adsorption hydrogen to obtain the purified hydrogen.
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