CN106833759B - Device and method for removing biomass gasification tar based on chemical chain reforming - Google Patents
Device and method for removing biomass gasification tar based on chemical chain reforming Download PDFInfo
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- 239000000126 substance Substances 0.000 title claims abstract description 25
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- GEYXPJBPASPPLI-UHFFFAOYSA-N manganese(III) oxide Inorganic materials O=[Mn]O[Mn]=O GEYXPJBPASPPLI-UHFFFAOYSA-N 0.000 claims description 3
- 230000003197 catalytic effect Effects 0.000 abstract description 2
- 150000003384 small molecules Chemical class 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 61
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 16
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- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- 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
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- 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
Abstract
The invention discloses a device and a method for removing biomass gasification tar based on chemical chain reforming, wherein the device comprises a first cyclone separator, a preheater, a reforming reactor and an air combustion reactor, wherein the first cyclone separator is used for separating and dedusting biomass gasification crude gas, the preheater is used for preheating the biomass gasification crude gas, the reforming reactor is used for reforming the preheated biomass gasification crude gas and an oxygen carrier, the air combustion reactor is used for carrying out combustion reaction on the oxygen carrier and air after reforming reaction, a second cyclone separator is connected between the air combustion reactor and the reforming reactor and is used for separating and dedusting the oxidized oxygen carrier, and the reforming reactor is also connected with a third cyclone separator which is used for separating and dedusting the reacted gas. The invention utilizes lattice oxygen of an oxygen carrier and catalytic action to oxidize the macromolecular part of tar into CO and H2And other small molecule substances; the oxygen carrier is circularly regenerated between the reforming reactor and the combustion reactor, and the oxygen carrier is simply regenerated.
Description
Technical Field
The invention relates to the technical field of energy and chemical industry, in particular to a device and a method for removing biomass gasification tar based on chemical chain reforming.
Background
Biomass is a renewable energy source with abundant resources. The characteristic of high volatile matter content (about 70%) of the biomass determines that the gasification utilization mode has economic and technical advantages. The biomass gasification technology can be linked with units for subsequent synthesis of liquid fuel, power generation, heat supply, production of chemical products and the like, thereby realizing the biomass resourceClean, efficient and diversified utilization. However, in the current biomass gasification technology, no matter air, water vapor or oxygen and a fixed bed or fluidized bed reactor are adopted, the fuel gas contains more tar byproducts due to high volatile components of the biomass, and the tar is gaseous at high temperature and can be condensed into liquid at the temperature of less than about 200 ℃. The existence of tar has serious influence on biomass gasification and utilization thereof, such as reduction of gasification efficiency, blockage of pipelines, poisoning of subsequent synthetic catalysts, damage of fuel gas utilization equipment and the like, and simultaneously, the difficulty of fuel gas purification is increased, and environmental pollution is caused. Therefore, the tar content in the fuel gas is one of the decisive factors restricting the large-scale application of the biomass gasification technology, and how to eliminate the tar in the gasification process is the most urgent problem to be solved by the current biomass gasification technology. Although the tar generation amount during biomass gasification can be reduced to a certain extent by adopting measures such as increasing the operating temperature, the tar content in the fuel gas is still relatively high, and the downstream utilization requirement can be met by further removing the tar. The technology for removing tar in the fuel gas comprises a physical method and a chemical method. The physical method is to remove tar in the fuel gas by water washing or an absorbent, and the method is simple and is easy to cause secondary pollution. The chemical method decomposes tar into small molecular gas through catalytic cracking, has no secondary pollution, converts and utilizes tar simultaneously, and is a tar removal method which is researched more at present. Traditional catalytic cracking is divided into two modes: one is that dolomite, alkaline earth metal compound and bionass are gasified catalytically together in the gasification furnace so as to reduce the production of tar; one is the nickel-based catalyst which decomposes tar in gasified fuel gas outside the furnace. Coke and dolomite have the disadvantages of large dosage and low catalytic efficiency. The nickel-based catalyst has high activity and good tar cracking effect, but the surface of the nickel-based catalyst is easy to coke and deactivate; the nickel-based catalyst is generally composed of nickel, an auxiliary agent and a carrier, the catalyst needs to be reduced before use, and the simple substance nickel is an active site of the catalyst. Ni-MgO/HZSM-5 disclosed in patent (CN 104549450A) and NiO-MgO-CeO disclosed in patent (CN 102145292A)2-WO3-olivine, NiO-La as disclosed in patent (CN 101693204B)2O3-CeO2-MgO-γAl2O3And patent (CN 100404135C)NiO-gamma Al2O3The catalyst for catalytic cracking of biomass gasification tar such as cordierite is used by first using H2And (4) carrying out reduction. After the carbon deposition of the nickel-based catalyst is inactivated, the regeneration process of carbon removal and reduction is carried out, the process is complex, the cost is high, and the cracking tar by using the nickel-based catalyst is severely restricted by the cost in the industrial application.
Accordingly, the prior art is yet to be improved and developed.
Disclosure of Invention
In view of the defects of the prior art, the invention aims to provide a device and a method for removing biomass gasification tar based on chemical chain reforming, and aims to solve the problems of easy carbon deposition, pre-reduction and difficult regeneration in the prior tar removal technology.
The technical scheme of the invention is as follows:
the utility model provides a device based on chemical chain reforming desorption living beings gasification tar, wherein, including the first cyclone that is used for separating the dust removal to the living beings gasification crude gas that connects gradually, be used for carrying out the preheater that preheats to the living beings gasification crude gas, be used for carrying out reforming reaction's reforming reactor and the air combustion reactor that is used for carrying out combustion reaction with the oxygen carrier after the reforming reaction with the oxygen carrier after preheating, be connected with between air combustion reactor and the reforming reactor and be used for carrying out the second cyclone that separates the dust removal to the oxygen carrier after the oxidation, the reforming reactor still is connected with the third cyclone that is used for carrying out the separation dust removal to the gas after the reaction.
A method for removing biomass gasification tar by using the device comprises the following steps:
step A, after the biomass gasification crude gas is separated and dedusted by a first cyclone separator and preheated by a preheater, the biomass gasification crude gas enters a reforming reactor to carry out reforming reaction with an oxygen carrier, and the reacted gas is separated and dedusted by a third cyclone separator to obtain clean gas;
and B, enabling the oxygen carrier after the reforming reaction to enter an air combustion reactor to perform combustion reaction with air, and enabling the oxygen carrier after being oxidized to enter the reforming reactor for recycling after being separated and dedusted by a second cyclone separator.
The method comprises the step of enabling oxygen-deficient air generated by combustion reaction in the air combustion reactor to enter a preheater to preheat crude fuel gas after being separated and dedusted by a second cyclone separator.
In the step A, the mass ratio of the tar content in the crude fuel gas to the lattice oxygen of the oxygen carrier in the reforming reactor is 1: 0.5-5.
The method of (a), wherein in the step (B), the air burn surplus factor in the air-fired reactor is 0.5 to 1.5.
The method comprises the step A, wherein the operation temperature of the reforming reactor is 550-950 ℃, and the operation pressure is 0.1 MPa.
The method, wherein the operating temperature of the air combustion reactor is 850-.
The method comprises the following steps that the active component of the oxygen carrier is one or more of Fe oxide, Cu oxide, Ni oxide, Ce oxide, Mn oxide and Ca oxide, and the inert component of the oxygen carrier is Al2O3One or more of MgO and ZrO.
The method comprises the following steps of preparing the active component, preparing the inert component, and mixing the active component and the inert component, wherein the content of the active component is 30-80wt%, and the content of the inert component is 20-70 wt%.
The method of (a), wherein the particle size of the oxygen carrier is in the range of 0.1 to 5 mm.
Has the advantages that: the invention utilizes lattice oxygen of an oxygen carrier to oxidize the macromolecular part of tar into CO and H at high temperature2The small molecular substances are removed, simultaneously the energy of tar can be partially reserved and utilized, and the tar content of the fuel gas after being removed by the device is lower than 1g/Nm3The tar removal rate exceeds 90 percent; in addition, the circulation of the oxygen carrier integrates oxygen transfer, heat transfer and catalysis, and can fully utilize the oxidation reaction heat of the oxygen carrier and the sensible heat of crude fuel gas; in addition, the oxygen carrier is regenerated by circulating between the reforming reactor and the air combustion reactorThe possible carbon deposition is eliminated, the oxygen carrier is simple to regenerate and eliminate, and the continuous operation of the system is favorably maintained.
Drawings
FIG. 1 is a schematic diagram of an apparatus for removing biomass gasification tar based on chemical-looping reforming according to the present invention.
Detailed Description
The invention provides a device and a method for removing biomass gasification tar based on chemical chain reforming, and the invention is further described in detail below in order to make the purpose, technical scheme and effect of the invention clearer and clearer. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Referring to fig. 1, the schematic diagram of the apparatus for removing biomass gasification tar based on chemical-looping reforming of the present invention includes, as shown in the figure, a first cyclone separator for separating and dedusting biomass gasification raw gas, a preheater for preheating biomass gasification raw gas, a reforming reactor for reforming the preheated biomass gasification raw gas with an oxygen carrier, and an air combustion reactor for combustion reaction of the oxygen carrier after reforming reaction with air, which are connected in sequence, a second cyclone separator for separating and dedusting the oxidized oxygen carrier is connected between the air combustion reactor and the reforming reactor, and a third cyclone separator for separating and dedusting the reformed gas.
Based on the device, the invention provides a method for removing biomass gasification tar by using the device, which comprises the following steps:
step A, after separation and dust removal of biomass gasification crude gas through a first cyclone separator and preheating of a preheater, the biomass gasification crude gas enters a reforming reactor to carry out reforming reaction with an oxygen carrier, and the gas after the reforming reaction is separated and dust removed through a third cyclone separator to obtain clean gas;
and B, enabling the oxygen carrier after the reforming reaction to enter an air combustion reactor to perform combustion reaction with air, and enabling the oxygen carrier after being oxidized to enter the reforming reactor for recycling after being separated and dedusted by a second cyclone separator.
The method for removing biomass gasification tar according to the present invention will be described in detail below with reference to FIG. 1.
In the step A, crude fuel gas containing tar from a biomass gasification system is separated and dedusted by a first cyclone separator, then preheated in a preheater with high-temperature tail gas (oxygen-poor tail gas) from an air combustion reactor, and enters a reforming reactor filled with metal oxide (oxygen carrier), and macromolecular tar substances in the crude fuel gas and lattice oxygen of the high-temperature oxygen carrier are subjected to partial oxidation reaction and converted into CO and H2Reducing oxygen carrier and other small molecular substances, and separating and dedusting the reacted fuel gas by a third cyclone separator to obtain clean fuel gas. The invention utilizes lattice oxygen of an oxygen carrier to oxidize tar in biomass crude fuel gas into CO and H2And the small molecular substances are removed, and simultaneously, the energy of the tar can be partially reserved and utilized.
In step A, the mass ratio of the tar content in the crude fuel gas to the lattice oxygen of the oxygen carrier in the reforming reactor is 1:0.5-5, preferably 1:1-3, such as 1:1, 1:2 or 1:3
In the step A, the operation temperature of the reforming reactor is 550-950 ℃, and the operation pressure is 0.1 MPa. The heat required by the temperature of the reforming reactor is provided by the sensible heat of the crude fuel gas and the high-temperature oxygen carrier and the sensible heat of the high-temperature tail gas of the air combustion reactor.
In step B, the oxygen carrier (possibly with partial carbon deposit on the surface) reduced after the reforming reaction enters an air combustion reactor to perform combustion reaction with air, the oxygen carrier is completely or mostly oxidized to obtain lattice oxygen again, and the carbon deposit on the surface is completely oxidized into CO2And the oxygen carrier is heated by the heat generated by combustion at the same time, and the oxidized high-temperature oxygen carrier enters the reforming reactor for recycling.
In the step B, the air combustion surplus coefficient in the air combustion reactor is 0.5-1.5, and the air combustion surplus coefficient refers to the ratio of the actual air quantity to the theoretical air quantity of the reduced oxygen carrier which is completely oxidized.
The operating temperature of the air combustion reactor is 850-1050 ℃, and the operating pressure is 0.1 MPa. The heat required by the temperature of the air combustion reactor is provided by the oxidation reaction heat of the reduced oxygen carrier and the oxygen in the air.
The steps A and B form a cyclic process.
The invention utilizes lattice oxygen of an oxygen carrier to oxidize tar in biomass crude fuel gas into CO and H2And the small molecular substances are removed, and simultaneously, the energy of the tar can be partially reserved and utilized. The method does not need to reduce the oxygen carrier in advance, and can continuously regenerate the oxygen carrier lattice oxygen and eliminate carbon deposition through the circulation of the oxygen carrier between the reforming reactor and the air combustion reactor.
Specifically, high-temperature tail gas (oxygen-deficient air) generated by combustion reaction in the air combustion reactor is separated and dedusted by the second cyclone separator and then enters the preheater to preheat crude fuel gas so as to recover heat. Part of the oxygen-lean air after heat recovery can enter the air combustion reactor according to the requirement to adjust the air combustion surplus coefficient.
Specifically, the active component of the oxygen carrier of the present invention may be one or more of Fe oxide, Cu oxide, Ni oxide, Ce oxide, Mn oxide, Ca oxide, etc., and the inert component of the oxygen carrier may be Al oxide2O3One or more of MgO, ZrO, etc. The invention adopts non-noble metal oxide as the oxygen carrier, thereby reducing the operation cost. Preferably, the content of the active component is 30-80wt%, and the content of the inert component is 20-70 wt%. The oxygen carrier has a particle size in the range of 0.1 to 5mm, preferably in the range of 0.15 to 2mm, for example 0.18 mm.
Compared with the prior art, the invention has the following advantages:
(1) oxidizing tar macromolecule part into CO and H by using lattice oxygen of oxygen carrier at high temperature2The micromolecular substances are removed, and simultaneously, the energy of tar can be partially reserved and utilized;
(2) the circulation of the oxygen carrier integrates oxygen transfer, heat carrying and catalysis, and makes full use of the oxidation reaction heat of the oxygen carrier and the sensible heat of crude fuel gas;
(3) the oxygen carrier is circularly regenerated and eliminates possible carbon deposition between the reforming reactor and the air combustion reactor, and the regeneration and the carbon deposition elimination of the oxygen carrier are simple, so that the continuous operation of the system is maintained;
(4) and non-noble metal oxide is used as an oxygen carrier, so that the operation cost is reduced.
The present invention will be described in detail below with reference to examples.
Example 1
The method is explained by taking the example of removing the biomass downdraft fixed bed air gasification crude gas tar.
From biomass downdraft fixed bed gasification crude fuel gas 10.0 Nm3H, tar content 2.35g/Nm3The temperature is 450 ℃, the mixture enters a reforming reactor and a high-temperature oxygen carrier (CuO-NiO/Al) from a second cyclone separator after being separated and dedusted by a first cyclone separator and preheated by a preheater2O36 kg/H), the oxygen carrier is reduced, the tar macromolecules in the crude fuel gas are partially oxidized and catalytically reformed into CO and H2The micromolecular substances are removed by conversion, and the tar content of the fuel gas obtained after the separation and the dust removal of the third cyclone separator is 0.07g/Nm3The removal rate of tar in the crude fuel gas is 97 percent;
the reduced oxygen carrier (with carbon deposition on the surface) enters an air combustion reactor, the air excess coefficient of the oxygen carrier combustion reaction is controlled to be 0.95, the reduced oxygen carrier is completely oxidized by air to obtain lattice oxygen again, and the carbon deposition on the surface is oxidized into CO2And eliminating, wherein the oxidized oxygen carrier is separated and dedusted by the second cyclone separator and then enters the reforming reactor for recycling.
The temperature of the reforming reactor is 850 ℃, the pressure is 0.1Mpa, the temperature of the air combustion reactor is 900 ℃, and the pressure is 0.1 Mpa; the oxygen carrier comprises CuO and NiO as active components and Al as an inert component2O3The mass ratio of the three components is 2:2:1, and the particle size range of the oxygen carrier is 0.15-0.84 mm.
The results of the process are given in table 1 below:
TABLE 1 results of the experiments
Example 2
The method is used for removing the crude gas tar by the downdraft fixed bed oxygen enrichment (50 v% oxygen) gasification of biomass.
From biomass fixed bed oxygen rich (50 v% oxygen) gasification crude gas 10.0 Nm3H, tar content 1.02g/Nm3The temperature is 480 ℃, the mixture enters a reforming reactor and high-temperature oxygen carriers (Mn) from a second cyclone separator after being separated and dedusted by a first cyclone separator and preheated by a preheater2O3-NiO/Al2O35 kg/H), the oxygen carrier is reduced, the tar macromolecules in the crude fuel gas are partially oxidized and catalytically reformed into CO and H2The micromolecular substances are removed by conversion, and the tar content of the obtained fuel gas is 0.05g/Nm after passing through a third cyclone separator3The removal rate of tar in the crude gas is 95 percent;
the reduced oxygen carrier (with carbon deposition on the surface) enters an air combustion reactor, the air excess coefficient of the oxygen carrier combustion reaction is controlled to be 0.8, the reduced oxygen carrier is completely oxidized by air to obtain lattice oxygen again, and the carbon deposition on the surface is oxidized into CO2And eliminating, wherein the oxidized oxygen carrier is separated and dedusted by the second cyclone separator and then enters the reforming reactor for recycling.
The temperature of the reforming reactor is 900 ℃, the pressure is 0.1Mpa, the temperature of the combustion reactor is 1000 ℃, and the pressure is 0.1 Mpa; the oxygen carrier active component is Mn2O3NiO, inert component Al2O3The mass ratio of the three components is 4:5:1, and the particle size range of the oxygen carrier is 0.35-1.40 mm.
The results of the process are given in table 2 below:
TABLE 2 results of the experiments
Example 3
The method for removing the crude gas tar in the air gasification of the biomass fluidized bed is taken as an example for explanation.
From biomass fluidized bed gasification crude gas 5.0 Nm3H, tar content 11.72g/Nm3At 520 deg.C, separating and dedusting with the first cyclone separator, preheating with the preheater, feeding into the reforming reactor, and mixing with high-temperature oxygen carrier (Fe) from the second cyclone separator2O3-NiO/Al2O35.4 kg/H), the oxygen carrier is reduced, the tar macromolecules in the crude fuel gas are partially oxidized and catalytically reformed into CO and H2The micromolecular substances are removed by conversion, and the tar content of the fuel gas obtained after the separation and the dust removal of the third cyclone separator is 0.92g/Nm3The removal rate of tar in the crude fuel gas is 92 percent;
the reduced oxygen carrier (with carbon deposition on the surface) enters an air combustion reactor, the air excess coefficient of the oxygen carrier combustion reaction is controlled to be 0.85, the reduced oxygen carrier is completely oxidized by air to obtain lattice oxygen again, and the carbon deposition on the surface is oxidized into CO2And eliminating, wherein the oxidized oxygen carrier is separated and dedusted by the second cyclone separator and then enters the reforming reactor for recycling.
The temperature of the reforming reactor is 880 ℃, the pressure is 0.1Mpa, the temperature of the combustion reactor is 950 ℃, and the pressure is 0.1 Mpa; the oxygen carrier active component is Fe2O3NiO, inert component Al2O3The mass ratio of the three components is 4.5:4.5:1, and the particle size range of the oxygen carrier is 0.25-1.19 mm.
The results of the process are given in table 3 below:
TABLE 3 results of the experiments
In summary, the invention provides a device and a method for removing biomass gasification tar based on chemical chain reforming, and the method does not need to reduce an oxygen carrier in advance, and uses the oxygen carrier to carry out combustion in a reforming reactorThe circulation between the burning reactors can continuously regenerate the oxygen carrier lattice oxygen and eliminate carbon deposition. In addition, the high-temperature crude fuel gas at the fuel gas outlet of the gasification furnace can directly enter the reforming reactor, and the sensible heat carried by the high-temperature crude fuel gas and the oxygen carrier is utilized to provide a high-temperature environment required by partial oxidation reaction, so that the energy utilization efficiency is improved. In addition, the lattice oxygen of the oxygen carrier is utilized to oxidize the tar in the biomass crude fuel gas into CO and H2And the small molecular substances are removed, so that the energy of tar can be fully utilized. The tar content of the fuel gas removed by the method is lower than 1g/Nm3The tar removal rate exceeds 90 percent. The method of the invention is a new method for efficiently removing biomass gasification tar.
It is to be understood that the invention is not limited to the examples described above, but that modifications and variations may be effected thereto by those of ordinary skill in the art in light of the foregoing description, and that all such modifications and variations are intended to be within the scope of the invention as defined by the appended claims.
Claims (3)
1. A device for removing biomass gasification tar based on chemical chain reforming is characterized by comprising a first cyclone separator, a preheater, a reforming reactor and an air combustion reactor, wherein the first cyclone separator is used for separating and dedusting biomass gasification crude gas, the preheater is used for preheating the biomass gasification crude gas, the reforming reactor is used for reforming the preheated biomass gasification crude gas with an oxygen carrier, the air combustion reactor is used for carrying out combustion reaction on the oxygen carrier and air after the reforming reaction, a second cyclone separator is connected between the air combustion reactor and the reforming reactor and is used for separating and dedusting the oxidized oxygen carrier, and the reforming reactor is also connected with a third cyclone separator which is used for separating and dedusting the reacted gas;
the temperature of the reforming reactor is 900 ℃ and the pressure is 0.1 Mpa;
the temperature of the combustion reactor is 1000 ℃ and the pressure is 0.1 Mpa;
the oxygen carrier active component is Mn2O3NiO, inert component Al2O3The mass ratio of the three is 4:5:1, and the particle size range of the oxygen carrier is 0.35～1.40mm；
The mass ratio of tar content in the biomass gasification crude fuel gas to lattice oxygen of an oxygen carrier in the reforming reactor is 1:2, and the air excess coefficient of the air combustion reactor is 0.8.
2. A method for removing biomass gasification tar by using the apparatus of claim 1, comprising the steps of:
step A, after the biomass gasification crude gas is separated and dedusted by a first cyclone separator and preheated by a preheater, the biomass gasification crude gas enters a reforming reactor to carry out reforming reaction with an oxygen carrier, and the reacted gas is separated and dedusted by a third cyclone separator to obtain clean gas;
b, enabling the oxygen carrier after the reforming reaction to enter an air combustion reactor to perform combustion reaction with air, and enabling the oxygen carrier after being oxidized to enter the reforming reactor for recycling after being separated and dedusted by a second cyclone separator;
the temperature of the reforming reactor is 900 ℃ and the pressure is 0.1 Mpa;
the temperature of the combustion reactor is 1000 ℃ and the pressure is 0.1 Mpa;
the oxygen carrier active component is Mn2O3NiO, inert component Al2O3The mass ratio of the three components is 4:5:1, and the particle size range of the oxygen carrier is 0.35-1.40 mm;
the mass ratio of tar content in the biomass gasification crude fuel gas to lattice oxygen of an oxygen carrier in the reforming reactor is 1:2, and the air excess coefficient of the air combustion reactor is 0.8.
3. The method of claim 2, wherein the oxygen-depleted air generated by the combustion reaction in the air combustion reactor is separated and dedusted by the second cyclone separator and enters the preheater to preheat the raw fuel gas.
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| WO2014162075A1 (en) * | 2013-04-05 | 2014-10-09 | IFP Energies Nouvelles | Method and device for chemical loop combustion of liquid hydrocarbon feedstocks |
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| CN104877713A (en) * | 2015-06-01 | 2015-09-02 | 农业部规划设计研究院 | Secondary pyrolysis and waste heat recycling system for biomass pyrolysis gas |
| CN106336879A (en) * | 2016-08-11 | 2017-01-18 | 安徽理工大学 | Biomass pyrolysis-reforming hydrogen production method |
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| US4289502A (en) * | 1979-05-30 | 1981-09-15 | Texaco Development Corporation | Apparatus for the production of cleaned and cooled synthesis gas |
| WO2014162075A1 (en) * | 2013-04-05 | 2014-10-09 | IFP Energies Nouvelles | Method and device for chemical loop combustion of liquid hydrocarbon feedstocks |
| CN104164273A (en) * | 2014-08-25 | 2014-11-26 | 中国科学院青岛生物能源与过程研究所 | Method for preparing calcium-based oxygen carrier |
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