CN113979409B - Organic solid waste treatment device and treatment method - Google Patents
Organic solid waste treatment device and treatment method Download PDFInfo
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- CN113979409B CN113979409B CN202111305752.5A CN202111305752A CN113979409B CN 113979409 B CN113979409 B CN 113979409B CN 202111305752 A CN202111305752 A CN 202111305752A CN 113979409 B CN113979409 B CN 113979409B
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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
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/061—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of metal oxides with water
- C01B3/063—Cyclic methods
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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
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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
- C10J3/58—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
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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
- C10J3/72—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
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
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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
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Abstract
The invention provides a treatment device for organic solid waste, and belongs to the technical field of organic solid waste treatment. When the treatment device provided by the invention is used for treating organic solid waste, the organic solid waste enters the pyrolysis-gasification reactor through the organic solid waste feeding hole to be decomposed, tar gas generated by decomposition enters the chemical chain reactor through the valve to react with an oxygen carrier to obtain synthesis gas, and the synthesis gas is collected through the gas outlet.
Description
Technical Field
The invention belongs to the technical field of organic solid waste treatment, and particularly relates to a treatment device and a treatment method for organic solid waste.
Background
With the development of economy, china generates a large amount of organic solid wastes (municipal domestic waste, agricultural and forestry wastes, sludge and the like) every year, and reasonable utilization of the organic solid wastes is not only beneficial to reducing environmental pollution, but also can convert the organic solid wastes into energy, materials, chemical products and the like. The organic solid waste thermochemical conversion (pyrolysis, gasification and combustion) is a common organic solid waste recycling method, but the pyrolysis and gasification processes have the defects of high tar content, low fuel conversion rate and the like, and the development of a novel organic solid waste utilization technology has important significance.
In recent years, based on the principle of chemical looping combustion technology, researchers develop chemical looping conversion technology of solid fuel, which can convert solid fuel (such as forestry and agricultural residues, municipal sludge, household garbage and the like) into synthesis gas and hydrogen, and improve the utilization efficiency of the fuel, and have a good application prospect, for example, chinese patent CN112624039A describes an organic solid waste treatment device based on chemical looping hydrogen production, which comprises a pyrolysis reactor (3) and a sleeve-type chemical looping reactor (19), wherein the sleeve-type chemical looping reactor (19) comprises an inner cavity and an outer cavity annularly wrapping the inner cavity, the pyrolysis reactor (3) can generate pyrolysis gas, and pyrolysis gas is input into the inner cavity and the outer cavity through a pyrolysis gas inlet device (6), the inner cavity and the outer cavity are provided with water vapor through a water vapor inlet device (7), synthesis gas generated by the inner cavity and the outer cavity is output through a synthesis gas output device (28), hydrogen generated by the inner cavity and the outer cavity is output through a hydrogen output device (29), the inner reaction chamber (17) is loaded with oxygen carriers, and the reversible oxygen carriers are loaded into the outer reaction chamber (18) and the reversible oxygen carriers. Although the device can convert solid fuels (such as agricultural and forestry wastes, municipal sludge, household garbage and the like) into the synthesis gas and the hydrogen, the structure of the device is complex, and the requirement on a control system is high. Therefore, how to simplify the organic solid waste treatment device becomes a difficult problem to be solved urgently.
Disclosure of Invention
The invention aims to provide a treatment device and a treatment method for organic solid wastes. The treatment device provided by the invention is simple, and can convert organic solid waste into synthesis gas and hydrogen.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides an organic solid waste treatment device, which comprises a pyrolysis-gasification reactor and a chemical chain reactor which are connected in series;
a valve is arranged between the pyrolysis-gasification reactor and the chemical chain reactor;
the pyrolysis-gasification reactor and the chemical chain reactor are provided with a steam inlet and a gas outlet;
the pyrolysis-gasification reactor is provided with an organic solid waste feeding hole;
the chemical chain reactor is provided with an oxygen carrier feed inlet.
Preferably, the organic solid waste treatment device further comprises an organic solid waste hopper, and the organic solid waste hopper is connected with the organic solid waste feeding hole through a screw feeder.
Preferably, the organic solid waste treatment device further comprises an ash hopper, and the ash hopper is connected with the pyrolysis-gasification reactor through a screw feeder.
Preferably, the water vapour inlet is provided with a perforated plate.
The invention also provides a method for treating the organic solid waste, the treatment device adopts the technical scheme to treat the organic solid waste, and the treatment comprises the following steps:
(1) Opening a valve, and allowing the organic solid waste to enter a pyrolysis-gas reactor through an organic solid waste feeding hole for decomposition to obtain tar gas and residual carbon;
(2) Feeding an oxygen carrier into the chemical-looping reactor through an oxygen carrier feeding hole;
(3) Discharging the tar gas obtained in the step (1) into a chemical chain reactor through a valve, mixing the tar gas with an oxygen carrier, and carrying out reduction reaction to obtain synthesis gas and a reduced oxygen carrier;
(4) Discharging the synthesis gas obtained in the step (3) through a gas outlet of a chemical-looping reactor;
(5) Closing a valve, discharging water vapor into a pyrolysis-gasification reactor through a water vapor inlet, and performing oxidation reaction on the water vapor and the residual carbon obtained in the step (1) to obtain synthesis gas; the synthesis gas is discharged through a gas outlet of the pyrolysis-gas reactor;
(6) Discharging water vapor into a chemical chain reactor through a water vapor inlet, and carrying out oxidation reaction on the water vapor and the reduced oxygen carrier obtained in the step (3) to obtain an oxygen carrier and hydrogen; the hydrogen is discharged through a gas outlet of the chemical-looping reactor;
the steps (1) and (2) are not in sequence;
the steps (5) and (6) are not in sequence.
Preferably, the temperature of decomposition in the step (1) is 500 to 800 ℃.
Preferably, the mass ratio of the organic solid waste in the step (1) to the oxygen carrier in the step (2) is 1: (1-6).
Preferably, the oxygen carrier in step (2) comprises an iron-based oxygen carrier.
Preferably, the particle size of the oxygen carrier in step (2) is not higher than 500 μm.
Preferably, the temperature of the reduction reaction in the step (3) is 700 to 1000 ℃.
The invention provides a treatment device for organic solid waste, which comprises a pyrolysis-gasification reactor and a chemical chain reactor which are connected in series; a valve is arranged between the pyrolysis-gasification reactor and the chemical-looping reactor; the pyrolysis-gasification reactor and the chemical chain reactor are provided with a steam inlet and a gas outlet; the pyrolysis-gasification reactor is provided with an organic solid waste feeding hole; the chemical chain reactor is provided with an oxygen carrier feed inlet. When the treatment device provided by the invention is used for treating organic solid waste, the organic solid waste enters the pyrolysis-gasification reactor through the organic solid waste feed inlet to be decomposed, tar gas generated by decomposition enters the chemical chain reactor through the valve to react with an oxygen carrier to obtain synthesis gas, the synthesis gas is collected through the gas outlet, after the reaction is finished, the valve is closed, water vapor is respectively introduced into the two reactors through the water vapor inlet to obtain the synthesis gas in the pyrolysis-gasification reactor, and high-purity hydrogen is obtained in the chemical chain reactor and is respectively collected through the gas outlet, so that the treatment device can be simplified, and meanwhile, the organic solid waste can be converted into the synthesis gas and the hydrogen. Experimental results show that the treatment device provided by the invention is used for treating organic solid waste, and the yield of the synthesis gas is 0.87-1.68 Nm 3 The purity of the synthetic gas is 70.13-90.42%, the carbon conversion rate is 70.34-99.77%, the hydrogen yield is 3.6-13.8 mmol/g oxygen carrier, and the hydrogen purity is 92.31-99.65%.
Drawings
FIG. 1 is a schematic structural diagram of an apparatus for treating organic solid waste provided by the present invention;
in the figure, 1 is an ash bucket, 2 is a pyrolysis-gasification reactor, 3 is a porous plate, 4 is a steam inlet, 5 is an organic solid waste hopper, 6 is a valve-1, 7 is a valve-2, 8 is a discharge hole, 9 is a chemical chain reactor, 10 is a valve-3, 11 is a cyclone separator, 12 is an oxygen carrier hopper, and 13 is a gas outlet.
Detailed Description
The invention provides a treatment device for organic solid waste, which comprises a pyrolysis-gasification reactor and a chemical chain reactor which are connected in series;
a valve is arranged between the pyrolysis-gasification reactor and the chemical-looping reactor;
the pyrolysis-gasification reactor and the chemical chain reactor are provided with a water vapor inlet and a gas outlet;
the pyrolysis-gasification reactor is provided with an organic solid waste feeding hole;
the chemical chain reactor is provided with an oxygen carrier feeding hole.
The device for treating the organic solid waste is suitable for organic solid waste obtained from any source.
As shown in fig. 1, in the present invention, the treatment apparatus includes a pyrolysis-gasification reactor 2 and a chemical-looping reactor 9 connected in series. The sizes of the pyrolysis-gasification reactor and the chemical-looping reactor are not particularly limited and can be adjusted according to needs.
As shown in fig. 1, in one embodiment of the present invention, the chemical looping reactor 9 is disposed above the pyrolysis-gasification reactor 2. In the present invention, the chemical-looping reactor is disposed above the pyrolysis-gasification reactor to facilitate the discharge of the synthesis gas into the chemical-looping reactor.
As shown in fig. 1, in the present invention, a valve-2 is provided between the pyrolysis-gasification reactor 2 and the chemical-looping reactor 9. In the present invention, the valve is opened for the discharge of the tar gas from the pyrolysis-gasification reactor into the chemical-looping reactor.
As shown in fig. 1, in the present invention, the pyrolysis-gasification reactor 2 is provided with a steam inlet 4. In the present invention, the water vapor inlet is for the entry of water vapor.
As shown in fig. 1, in one embodiment of the present invention, the water vapor inlet 4 is provided at the bottom of the pyrolysis-gasification reactor 2.
In one embodiment of the invention, as shown in fig. 1, the water vapour inlet 4 is provided with a perforated plate 3. In the present invention, the perforated plate enables uniform entry of water vapor.
As shown in fig. 1, in the present invention, the pyrolysis-gasification reactor 2 is provided with a gas outlet 13; the gas outlet 13 is provided with a valve-1. In the present invention, the gas outlet is used for discharging the synthesis gas obtained by reacting the water vapor with the residual carbon in the pyrolysis-gasification reactor.
As shown in fig. 1, in the present invention, the pyrolysis-gasification reactor 2 is provided with an organic solid waste feed port.
As shown in fig. 1, in one embodiment of the present invention, the organic solid waste feed inlet is provided at the middle upper portion of the sidewall of the pyrolysis-gasification reactor 2. In the invention, the organic solid waste feeding hole is arranged at the middle upper part of the side wall of the pyrolysis-gasification reactor, which is beneficial to feeding of organic solid waste.
As shown in fig. 1, in one embodiment of the present invention, the apparatus for processing organic solid waste further comprises an organic solid waste hopper 5; the organic solid waste hopper 5 is connected with the organic solid waste feeding hole through a screw feeder.
As shown in fig. 1, in one embodiment of the present invention, the organic solid waste treatment apparatus further includes an ash hopper 1; the ash hopper 1 is connected with the pyrolysis-gasification reactor 2 through a screw feeder.
As shown in fig. 1, in one embodiment of the present invention, the ash hopper 1 is disposed at the bottom of the pyrolysis-gasification reactor 2.
As shown in fig. 1, in the present invention, the chemical-looping reactor 9 is provided with a steam inlet 4. In the present invention, the water vapor inlet is for the entry of water vapor.
As shown in fig. 1, in one embodiment of the invention, the water vapor inlet 4 is disposed at the bottom of the chemical looping reactor 9.
In one embodiment of the invention, as shown in fig. 1, the water vapour inlet 4 is provided with a perforated plate 3. In the present invention, the perforated plate is to allow water vapor to uniformly enter.
In the present invention, as shown in fig. 1, the chemical-looping reactor 9 is provided with an oxygen carrier feed port. In the present invention, the oxygen carrier feed inlet is used for feeding of the oxygen carrier.
As shown in fig. 1, in one embodiment of the present invention, the apparatus for treating organic solid waste further comprises an oxygen carrier hopper 12; the oxygen carrier hopper 12 is connected to the oxygen carrier feed port by a screw feeder.
As shown in fig. 1, in the present invention, the chemical looping reactor 9 is provided with a gas outlet. In the present invention, the gas outlet is used for the discharge of synthesis gas or hydrogen.
As shown in fig. 1, in one embodiment of the invention, the gas outlet of the chemical looping reactor 9 is provided with a cyclone 11; and a valve-3 is arranged at an air outlet of the cyclone separator 11. In the present invention, the cyclone is used to effect separation of the syngas/hydrogen from the doping and oxygen carriers in the syngas/hydrogen. In the present invention, the valve-3 is used to control the opening and closing of the gas outlet of the chemical looping reactor.
In one embodiment of the invention, as shown in figure 1, the ash discharge of the cyclone 11 is connected to a screw feeder. In the present invention, the ash discharge of the cyclone 11 is connected to a screw feeder, through which the separated oxygen carriers can be re-fed to the chemical looping reactor.
In one embodiment of the invention, as shown in fig. 1, the chemical looping reactor 9 is further provided with a discharge outlet 8. In the present invention, the discharge port is used for discharging most of the oxygen carriers.
When the treatment device provided by the invention is used for treating organic solid waste, the organic solid waste enters the pyrolysis-gasification reactor through the organic solid waste feeding hole to be decomposed, tar gas generated by decomposition enters the chemical chain reactor through the valve to react with an oxygen carrier to obtain synthesis gas, and the synthesis gas is collected through the gas outlet.
The feeding and discharging of the oxygen carrier in the organic solid waste treatment device provided by the invention are convenient, and the problem that the oxygen carrier is not easy to remove in the conventional treatment device is solved; compared with the existing device, the device can generate more synthesis gas, and solves the problem that the existing device only adopts tar gas to prepare synthesis gas and hydrogen, and residual carbon is not utilized; further, the processing device of the present invention is an intermittent device.
The oxygen carrier in the organic solid waste treatment device provided by the invention does not need to flow between reactors, so that the requirements on the wear resistance and strength of the oxygen carrier in the traditional technology are lowered, the energy consumption required by the circulation of the oxygen carrier is reduced, the direct contact between the organic solid waste and the oxygen carrier is effectively avoided, the influence of ash on the oxygen carrier is reduced, the inactivation of the oxygen carrier is relieved, and the high-efficiency coupling can be carried out on the pyrolysis of the organic solid waste, the gasification of residual carbon and the hydrogen production of a chemical chain, so that the co-preparation of synthesis gas and high-concentration hydrogen is realized; the hydrogen does not need a complex gas separation and purification system, so the cost is low and the operation is simple; continuous preparation of hydrogen and synthesis gas can be realized by switching the pyrolysis gas and steam inlet valves; the concentration of the synthesis gas is regulated and controlled by the generated high-purity hydrogen, so that the further utilization of the synthesis gas is facilitated, and the method has wide market prospect and environmental benefit.
The invention also provides a method for treating the organic solid waste, the treatment device adopts the technical scheme to treat the organic solid waste, and the treatment comprises the following steps:
(1) Opening a valve, and allowing the organic solid waste to enter a pyrolysis-gas reactor through an organic solid waste feeding hole for decomposition to obtain tar gas and residual carbon;
(2) Feeding an oxygen carrier into the chemical-looping reactor through an oxygen carrier feeding hole;
(3) Discharging the tar gas obtained in the step (1) into a chemical chain reactor through a valve, mixing the tar gas with an oxygen carrier, and carrying out reduction reaction to obtain synthesis gas and a reduced oxygen carrier;
(4) Discharging the synthesis gas obtained in the step (3) through a gas outlet of a chemical-looping reactor;
(5) Closing a valve, discharging water vapor into a pyrolysis-gasification reactor through a water vapor inlet, and carrying out oxidation reaction on the water vapor and the residual carbon obtained in the step (1) to obtain synthesis gas; the synthesis gas is discharged through a gas outlet of the pyrolysis-gas reactor;
(6) Discharging water vapor into a chemical chain reactor through a water vapor inlet, and carrying out oxidation reaction on the water vapor and the reduced oxygen carrier obtained in the step (3) to obtain an oxygen carrier and hydrogen; the hydrogen is discharged through a gas outlet of the chemical-looping reactor;
the steps (1) and (2) are not in sequence;
the steps (5) and (6) are not in sequence.
The invention opens the valve, and the organic solid waste enters the pyrolysis-gas reactor through the organic solid waste feeding hole to be decomposed, so as to obtain tar gas and residual carbon. In the present invention, the organic solid waste will produce tar gas (containing mainly H) by pyrolysis 2 、CO、CH 4 、CO 2 And C n H m O y ) And residual carbon.
In the present invention, the organic solid waste is preferably at least one of sawdust, paper, plastic and fabric; the particle size of the organic solid waste is preferably not higher than 1mm; when the particle size of the organic solid waste does not meet the requirements, the organic solid waste is preferably crushed firstly. The operation of the crushing in the present invention is not particularly limited, and may be performed by a method known to those skilled in the art.
In the present invention, the valve is preferably a valve between the pyrolysis-gasification reactor and the chemical-looping reactor.
In the present invention, the temperature of the decomposition is preferably 500 to 800 ℃, more preferably 600 to 700 ℃. In the present invention, the time for the decomposition is not particularly limited, and may be determined based on common knowledge.
The invention leads oxygen carriers to enter a chemical chain reactor through an oxygen carrier feed inlet.
In the present invention, the oxygen carrier preferably includes an iron-based oxygen carrier, and more preferably iron ore or Fe 3 O 4 And Ca 2 Fe 2 O 5 More preferably Ca 2 Fe 2 O 5 (ii) a The oxygen carrier has excellent particle diameterPreferably no more than 500 microns and more preferably from 100 to 300 microns. The source of the oxygen carrier is not particularly limited in the present invention, and it may be prepared by a commercially available product or a known preparation method known to those skilled in the art. In the invention, the oxygen carrier has the capability of decomposing water to produce hydrogen, not only provides lattice oxygen, but also has a catalytic action, and greatly improves the conversion rate of fuel.
After obtaining the tar gas, the invention opens the valve, discharges the tar gas into the chemical chain reactor through the valve, mixes the tar gas with the oxygen carrier, and carries out reduction reaction to obtain synthesis gas and a reduction state oxygen carrier.
In the present invention, the mass ratio of the organic solid waste to the oxygen carrier is preferably 1: (1 to 6), and more preferably 1 (2.9 to 5). In the invention, the content and purity of the synthesis gas can be further improved by controlling the mass ratio of the organic solid waste to the oxygen carrier.
In the present invention, the valve is preferably a valve between the pyrolysis-gasification reactor and the chemical-looping reactor.
In the present invention, the temperature of the reduction reaction is preferably 700 to 1000 ℃, and more preferably 800 to 900 ℃. In the present invention, the time for the reduction reaction is not particularly limited, and may be determined based on common knowledge.
After the synthesis gas is obtained, the invention discharges the synthesis gas through a gas outlet of the chemical-looping reactor.
After the residual carbon is obtained, the valve is closed, the steam is discharged into the pyrolysis-gasification reactor through the steam inlet, and the steam and the obtained residual carbon are subjected to oxidation reaction to obtain the synthesis gas.
In the present invention, the mass ratio of water vapor to organic solid waste in the pyrolysis-gasification reactor is preferably 1:1 to 6:1, more preferably 3:1 to 4:1.
in the present invention, the temperature of the oxidation reaction is preferably 500 to 800 ℃, more preferably 600 to 700 ℃. In the present invention, the time of the oxidation reaction is not particularly limited, and may be determined based on common knowledge.
In the present invention, the synthesis gas is discharged through a gas outlet of the pyrolysis-gasification reactor.
After the reduced oxygen carrier is obtained, the valve is closed, water vapor is discharged into the chemical chain reactor through the water vapor inlet, and the oxidation reaction is carried out on the water vapor and the obtained reduced oxygen carrier, so that the oxygen carrier and hydrogen are obtained.
In the present invention, the mass ratio of water vapor to oxygen carrier in the chemical looping reactor is preferably 1:5 to 2:1, more preferably 1:3 to 1.2:1.
in the present invention, the temperature of the oxidation reaction is preferably 700 to 1000 ℃, more preferably 800 to 900 ℃. In the present invention, the time of the oxidation reaction is not particularly limited, and may be determined based on common knowledge.
In the present invention, the hydrogen gas is discharged through a gas outlet of the chemical-looping reactor.
The method for treating the organic solid waste provided by the invention is divided into two stages, wherein the first stage comprises pyrolysis of the organic solid waste and reformation of tar gas; the second stage is that the water vapor reacts with the residual carbon and the reduced oxygen carrier respectively to generate synthesis gas and hydrogen.
The following reactions take place in the first stage:
pyrolysis-gasification reactor:
organic solid waste + heat → residual carbon (C) + tar gas (including CO, CO) 2 、CH 4 、C n H m 、C x H y O z )
Chemical chain reactor:
tar gas + oxygen carrier (Me) x O y ) → syngas + Me x O y -m (reduced oxygen carrier)
The following reactions take place in the second stage:
pyrolysis-gasification reactor:
steam + residual carbon (C) → syngas (CO + H) 2 )
Chemical chain reactor:
Me x O y -m + water vapor → H 2 +Me x O y
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It should be apparent that the described embodiments are only some embodiments of the present invention, and not all embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
Example 1
The treatment device for organic solid waste provided by the embodiment comprises a pyrolysis-gasification reactor and a chemical-looping reactor which are connected in series;
a valve is arranged between the pyrolysis-gasification reactor and the chemical chain reactor;
the pyrolysis-gasification reactor and the chemical chain reactor are provided with a steam inlet and a gas outlet;
the pyrolysis-gasification reactor is provided with an organic solid waste feeding hole;
the chemical chain reactor is provided with an oxygen carrier feed inlet.
Example 2
The schematic structural diagram of the organic solid waste treatment device provided in this embodiment is shown in fig. 1, in which 1 is an ash hopper, 2 is a pyrolysis-gasification reactor, 3 is a porous plate, 4 is a steam inlet, 5 is a hopper, 6 is a valve-1, 7 is a valve-2, 8 is a discharge port, 9 is a chemical chain reactor, 10 is a valve-3, 11 is a cyclone separator, 12 is an oxygen carrier hopper, and 13 is a gas outlet;
the organic solid waste treatment device comprises a pyrolysis-gasification reactor 2 and a chemical chain reactor 9 which are connected in series;
the chemical-looping reactor 9 is arranged above the pyrolysis-gasification reactor 2;
a valve-2 is arranged between the pyrolysis-gasification reactor 2 and the chemical chain reactor 9;
the pyrolysis-gasification reactor 2 is provided with a steam inlet 4; the steam inlet 4 is arranged at the bottom of the pyrolysis-gasification reactor 2;
the water vapor inlet 4 is provided with a porous plate 3;
the pyrolysis-gasification reactor 2 is provided with a gas outlet 13;
the gas outlet 13 is provided with a valve-1;
the pyrolysis-gasification reactor 2 is provided with an organic solid waste feeding hole;
the organic solid waste feeding hole is formed in the middle upper part of the side wall of the pyrolysis-gasification reactor 2;
the organic solid waste treatment device also comprises an organic solid waste hopper 5; the organic solid waste hopper 5 is connected with the organic solid waste feeding hole through a spiral feeder;
the organic solid waste treatment device further comprises an ash bucket 1, and the ash bucket 1 is connected with the pyrolysis-gasification reactor 2 through a spiral feeder;
the chemical chain reactor 9 is provided with a steam inlet 4; the steam inlet 4 is arranged at the bottom of the chemical-looping reactor 9; the water vapor inlet 4 is provided with a porous plate 3;
the chemical chain reactor 9 is provided with an oxygen carrier feeding hole;
the organic solid waste treatment device also comprises an oxygen carrier hopper 12; the oxygen carrier hopper 12 is connected with an oxygen carrier feeding hole through a screw feeder;
the chemical looping reactor 9 is provided with a gas outlet;
a gas outlet of the chemical chain reactor 9 is provided with a cyclone separator 11; a valve-3 is arranged at an air outlet of the cyclone separator 11;
the ash discharge port of the cyclone separator 11 is connected with a screw feeder;
the chemical chain reactor 9 is also provided with a discharge port 8.
Example 3
Organic solid waste (sawdust, paper, plastic and fabric mix) was treated using the treatment apparatus of example 2, with the following steps:
(1) Opening a valve-2, feeding 35g of organic solid waste into the pyrolysis-gas reactor 2 through an organic solid waste feeding hole, and decomposing for 30min at 500 ℃ to obtain tar gas and residual carbon;
(2) 100g of Fe 3 O 4 Entering into chemical chain reaction through oxygen carrier feed inletIn the device 9;
(3) Discharging the tar gas obtained in the step (1) into a chemical chain reactor 9 through a valve 7, and reacting with Fe 3 O 4 Mixing, and carrying out reduction reaction at 800 ℃ to obtain synthesis gas and a reduced oxygen carrier;
(4) Discharging the synthesis gas obtained in the step (3) through a gas outlet of a chemical-looping reactor 9;
(5) Closing a valve-2, discharging water vapor into the pyrolysis-gasification reactor 2 through a water vapor inlet, and performing oxidation reaction on the water vapor and the residual carbon obtained in the step (1) at the temperature of 500 ℃ to obtain synthesis gas; the synthesis gas is discharged through a gas outlet of the pyrolysis-gasification reactor 2; the time for discharging the water vapor is 30min; the flow rate of the water vapor is 4g/min;
(6) Discharging water vapor into a chemical chain reactor 9 through a water vapor inlet, and carrying out oxidation reaction on the water vapor and the reduced oxygen carrier obtained in the step (3) at the temperature of 800 ℃ to obtain Fe 3 O 4 And hydrogen; the hydrogen is discharged through a gas outlet of the chemical-looping reactor 9; the time for discharging the water vapor is 30min; the steam flow rate was 4g/min.
The synthesis gas and hydrogen obtained in example 3 were tested and the results are shown in table 1.
Table 1 synthesis gas and hydrogen data in example 3
Example 4
On the basis of the embodiment 3, the decomposition temperature of the step (1) and the oxidation reaction temperature of the step (5) are modified to 600 ℃, the reduction reaction temperature of the step (3) and the oxidation reaction temperature of the step (6) are modified to 900 ℃, and other steps are not changed.
The synthesis gas and hydrogen obtained in example 4 were tested and the results are shown in table 2.
Table 2 synthesis gas and hydrogen data in example 4
Example 5
On the basis of the embodiment 3, the decomposition temperature of the step (1) and the oxidation reaction temperature of the step (5) are modified to 700 ℃, the reduction reaction temperature of the step (3) and the oxidation reaction temperature of the step (6) are modified to 900 ℃, and other steps are not changed.
The synthesis gas and hydrogen obtained in example 5 were tested and the results are shown in table 3.
Table 3 synthesis gas and hydrogen data in example 5
Example 6
On the basis of the embodiment 3, the decomposition temperature of the step (1) and the oxidation reaction temperature of the step (5) are modified to 700 ℃, the reduction reaction temperature of the step (3) and the oxidation reaction temperature of the step (6) are modified to 1000 ℃, and other steps are not changed.
The synthesis gas and hydrogen obtained in example 6 were tested and the results are shown in table 4.
Table 4 synthesis gas and hydrogen data in example 6
Example 7
The quality of the organic solid waste is modified to 20g on the basis of the example 4, and other steps are not changed.
The synthesis gas and hydrogen obtained in example 7 were tested and the results are shown in table 5.
Table 5 synthesis gas and hydrogen data in example 7
Example 8
The quality of the organic solid waste is modified to 30g on the basis of the example 4, and other steps are not changed.
The synthesis gas and hydrogen obtained in example 8 were tested and the results are shown in table 6.
Table 6 synthesis gas and hydrogen data in example 8
Example 9
The quality of the organic solid waste is modified to 45g on the basis of the example 4, and other steps are not changed.
The synthesis gas and hydrogen obtained in example 9 were tested and the results are shown in table 7.
Table 7 synthesis gas and hydrogen data in example 9
As can be seen from the above examples, the pyrolysis-gasification reactor temperature of 600 to 700 ℃, and the chemical-looping reactor temperature of 900 to 1000 ℃ can further improve the yield and purity of syngas, carbon conversion rate, and hydrogen yield and purity.
From the above examples, it can be seen that the mass ratio of the oxygen carrier to the organic solid waste is 1: at 0.35, the synthesis gas and hydrogen yields are highest.
From the above examples, it can be seen that the treatment device provided by the invention is simple and can convert organic solid wastes into synthesis gas and hydrogen.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (6)
1. A treatment method of organic solid waste adopts a treatment device to treat the organic solid waste, and the treatment method comprises the following steps:
(1) Opening a valve, and allowing the organic solid waste to enter a pyrolysis-gas reactor through an organic solid waste feeding hole for decomposition to obtain tar gas and residual carbon;
(2) Feeding an oxygen carrier into a chemical-looping reactor through an oxygen carrier feeding hole;
(3) Discharging the tar gas obtained in the step (1) into a chemical chain reactor through a valve, mixing the tar gas with an oxygen carrier, and carrying out a reduction reaction to obtain synthesis gas and a reduced oxygen carrier;
(4) Discharging the synthesis gas obtained in the step (3) through a gas outlet of a chemical-looping reactor;
(5) Closing a valve, discharging water vapor into a pyrolysis-gasification reactor through a water vapor inlet, and performing oxidation reaction on the water vapor and the residual carbon obtained in the step (1) to obtain synthesis gas; the synthesis gas is discharged through a gas outlet of the pyrolysis-gasification reactor;
(6) Discharging water vapor into a chemical chain reactor through a water vapor inlet, and carrying out oxidation reaction on the water vapor and the reduced oxygen carrier obtained in the step (3) to obtain an oxygen carrier and hydrogen; the hydrogen is discharged through a gas outlet of the chemical-looping reactor;
the steps (1) and (2) are not in sequence;
the steps (5) and (6) are not in sequence;
the treatment device comprises a pyrolysis-gasification reactor and a chemical-looping reactor which are connected in series; a valve is arranged between the pyrolysis-gasification reactor and the chemical chain reactor; the pyrolysis-gasification reactor and the chemical chain reactor are provided with a steam inlet and a gas outlet; the pyrolysis-gasification reactor is provided with an organic solid waste feeding hole; the chemical chain reactor is provided with an oxygen carrier feeding hole; the organic solid waste treatment device also comprises an organic solid waste hopper, and the organic solid waste hopper is connected with the organic solid waste feeding hole through a spiral feeder; the organic solid waste treatment device also comprises an ash hopper, wherein the ash hopper is connected with the pyrolysis-gasification reactor through a spiral feeder; the steam inlet is provided with a porous plate.
2. The pretreatment method according to claim 1, wherein the decomposition temperature in the step (1) is 500 to 800 ℃.
3. The pretreatment method according to claim 1, wherein the mass ratio of the organic solid waste in the step (1) to the oxygen carrier in the step (2) is 1: (1-6).
4. The pretreatment method according to claim 1, wherein the oxygen carrier in the step (2) comprises an iron-based oxygen carrier.
5. The pretreatment method according to claim 1 or 4, wherein the particle size of the oxygen carrier in the step (2) is not more than 500 μm.
6. The pretreatment method according to claim 1, wherein the temperature of the reduction reaction in the step (3) is 700 to 1000 ℃.
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| CN117480111A (en) * | 2022-02-18 | 2024-01-30 | 南极实验室私人有限公司 | Pyrolysis reactor for recovering carbon from certain plastics and system and method for recovering carbon from certain plastics |
| CN114735644A (en) * | 2022-03-24 | 2022-07-12 | 上海电气集团股份有限公司 | Hydrogen production system of solid organic matter |
| CN115228874B (en) * | 2022-05-25 | 2023-12-29 | 海南省智慧环境投资控股有限公司 | Dynamic circulation organic solid waste treatment process |
| CN115321478A (en) * | 2022-07-29 | 2022-11-11 | 山西科化技术服务有限公司 | Biomass pyrolysis chemical-looping hydrogen production device and process |
| CN115895736A (en) * | 2022-11-15 | 2023-04-04 | 华南农业大学 | Method for preparing low-carbon olefin and co-producing high-purity hydrogen by coupling waste plastic with alkali lignin |
| CN115948172B (en) * | 2022-12-29 | 2024-04-09 | 中国科学院广州能源研究所 | Device and method for preparing clean synthetic gas by organic solid waste pyrolysis-chemical chain reforming |
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