CN105623685A - Method and equipment for continuous co-production of gas and charcoal through biomass material in-situ catalytic cracking - Google Patents
Method and equipment for continuous co-production of gas and charcoal through biomass material in-situ catalytic cracking Download PDFInfo
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- CN105623685A CN105623685A CN201510903500.0A CN201510903500A CN105623685A CN 105623685 A CN105623685 A CN 105623685A CN 201510903500 A CN201510903500 A CN 201510903500A CN 105623685 A CN105623685 A CN 105623685A
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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
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
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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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
- C10B47/20—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge according to the moving bed type
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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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/18—Modifying the properties of the distillation gases in the oven
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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
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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Abstract
The invention discloses a method and equipment for continuous co-production of gas and charcoal through biomass material in-situ catalytic cracking. The method is characterized in that a cracking and reforming catalyst and biomass materials are mixed and then fed into a moving bed reactor; biomass is subjected to anaerobic pyrolysis to produce biomass gas under the condition that an external reactor provides a heat source; tar produced during the biomass gasification process is subjected to in-situ catalytic cracking to produce small molecular gas under the action of a catalyst; in addition, part of CO is further cracked and reformed into H2; the catalyst subjected to catalytic action and biomass charcoal are discharged from the moving bed reactor; the catalyst and the biomass charcoal are obtained after magnetic separation; the catalyst is reused, and the biomass charcoal serves as the carrier of the catalyst, an adsorbent or a soil conditioner to be used. The method and equipment solve the disadvantages that during the current biomass gasification process, the content of effective gas composition in gas is low, the existence of jar affects continuous and stable operation of the process, the biomass charcoal quality is low, and the utilization efficiency of biomass energy is low.
Description
Technical field
The invention belongs to Biomass Energy Technology field, be specifically related to the method and apparatus of a kind of continuous biomass raw material In-stiu catalysis gas, charcoal coproduction.
Background technology
Biomass material refers to and converts solar energy into, by photosynthesis, a kind of energy that chemical energy is stored in plant, utilizing in process because of to CO in air of biomass energy2Clean discharge be zero, obtain the extensive concern of people.
At present, biomass energy utilizes on a large scale and mostly adopts the mode of air gasification to be used, due to the diluting effect (N of nitrogen in air2Concentration of volume percent about 60% in exit gas) cause that the gas heating value that gasification of biomass produces is low, the not high (H of the volume by volume concentration of available gas2: about 10%; About CO:18%), limit its utilization, add in the biomass ash after gasification of biomass carbon left mass percentage content about 20%, and the tar produced in biomass gasification process, adhere to each other blocking transport pipeline with flying dust, while affecting its continuous and steady operation, biomass utilization efficiency is low.
A kind of continuous external heating type biomass In-stiu catalysis gas provided by the present invention, charcoal coproduction method and apparatus produce in this context just. Although at present about the existing research of the technology of biogas, charcoal coproduction, as the technology such as CN101967386A, CN1721503A all refer to utilize biomass to produce biomass carbon product, but these technology there is problems in that the batch production method that mostly adopts; The tar produced in biomass gasification process is not acted upon; In the gas produced, available gas composition needs to be improved further. CN2723837Y utilizes the biomass pyrolytic carbonization heat supply that the sensible heat that the combustion gas gasifying out is with is postorder, because of the fuel gas temperature low (380-420 DEG C) gasified out, the yield of biomass pyrolytic carbon and difficult quality guarantee; Although CN103614151A solves continuity problem, but but the tar supervened in gasification is to well solving.
Summary of the invention
The invention aims to solve gas effective ingredient in current biomass gasification process low, the continuous and steady operation of the existence influence process of tar, the shortcoming such as biomass carbon quality is not high and biomass utilization efficiency is low, develop a kind of continuous external heating type biomass In-stiu catalysis gas, the method and apparatus of charcoal coproduction, the cracking reforming catalyst and biomass material with catalytic cracking activity are homogeneously added in moving-burden bed reactor and gasify by the method, and biomass gasification process and external firing heat supplying process are integrated, the catalytic pyrolysis of the tar being gasified for biomass Non-oxygen pyrolytic by the burning of external fuel and supervening in gasification provides heat energy, owing to biomass are the pyrolytic gasifications under isolation external environment oxygen free condition, the tar supervened in gasification is under the effect of cracking reforming catalyst, tar can be little molecule available gas composition by In-stiu catalysis, CO also catalyzed can reform and occur transformationreation to generate H simultaneously2, thus can make the H in the gas effective ingredient of generation2Content is improved significantly.
In order to realize foregoing invention purpose, the technical solution used in the present invention is as follows:
A kind of continuous external heating type biomass In-stiu catalysis gas is provided, the equipment of charcoal coproduction, it includes the moving-burden bed reactor 2 for biomass In-stiu catalysis and external firing reactor 6, moving-burden bed reactor is located in external firing reactor, moving-burden bed reactor one end be arranged over feed bin 1, the pyrolysis gas of biomass that is arranged over of the other end exports 4, it is connected with biomass carbon and cracking reforming catalyst outlet 5, the inside of moving-burden bed reactor is provided with rotation flight 3, rotate flight and under external force the mixture of the biomass material sent into through feed bin with cracking reforming catalyst is continuously fed in moving-burden bed reactor carry out the Non-oxygen pyrolytic of biomass and supervene the catalytic pyrolysis of tar, the conversion reforming process of CO.
By such scheme, external firing reactor is provided with fuel inlet 7 and the air compartment 9 of supply fuel combustion auxiliary agent, and the top of external firing reactor is additionally provided with combustion reactor exhanst gas outlet 8.
By such scheme, fuel used by external burner is biomass, coal and natural gas, comburant is air, the addition of the blow rate required with fuel by controlling external firing reactor air, while making complete combustion of fuel, keep the temperature in external firing reactor at 650-800 DEG C.
By such scheme, when the air capacity passed into is affiliated complete combustion of fuel 1-1.2 times of required air quantity.
A kind of continuous external heating type biomass In-stiu catalysis gas is provided, the method of charcoal coproduction, it is characterized in that: be sent in moving-burden bed reactor after biomass material is mixed with cracking reforming catalyst, fuel is sent into simultaneously the outside combustion outside moving-burden bed reactor anti-burn to answer in device fully burn, it is the required heat of micro-molecular gas supply for the biomass pyrolytic in moving-burden bed reactor and the tar In-stiu catalysis supervened, the mixture sending into the biomass material in moving-burden bed reactor and cracking reforming catalyst continues into the catalytic pyrolysis of the Non-oxygen pyrolytic carrying out biomass in moving-burden bed reactor and the tar supervened under the effect of moving-burden bed reactor internal rotating flight, the conversion reforming process of CO, the pyrolysis gas that biomass pyrolytic produces flows out for subsequent handling from the pyrolysis gas outlet of moving-burden bed reactor, cracking reforming catalyst after biomass carbon and catalytic reaction is moved to biomass carbon in the effect rotating flight and discharges with cracking reforming catalyst outlet.
By such scheme, the charcoal discharged from biomass carbon and cracking reforming catalyst outlet obtains biomass carbon and cracking reforming catalyst with cracking reforming catalyst after magnetic separation, cracking reforming catalyst recycles, and biomass carbon uses as the cracking carrier of reforming catalyst or adsorbent or the modifying agent as soil.
By such scheme, the particle diameter of biomass is at below 10mm, and water content mass percent is below 10%.
By such scheme, the oxide Fe of the ferrum that described cracking reforming catalyst is produced by the calcining of biomass carbon carrier and supported on carriers2O3Form with the oxide NiO of nickel, wherein the oxide Fe of the oxide NiO of nickel and ferrum2O3Mass percent respectively 20-30%, 20-30%, surplus is high-area carbon.
By such scheme, the biomass carbon of the described method acquisition that the biomass carbon carrier in cracking reforming catalyst is continuous external heating type biomass In-stiu catalysis gas of the present invention, charcoal coproduction.
By such scheme, described cracking reforming catalyst is with biomass carbon for carrier, by infusion process load ferric nitrate and nickel nitrate, forms again through vacuum calcining, and the calcining heat of vacuum calcining is 350-400 DEG C, wherein: ferric nitrate is with Fe2O3Metering, nickel nitrate measures with NiO, and the mass percent of each component is: ferric nitrate 20-30%, nickel nitrate 20-30%, and surplus is high-area carbon.
It is 6.25-12.5wt% by such scheme, described biomass material and the mass percent cracking reforming catalyst in cracking reforming catalyst.
By such scheme, the biomass In-stiu catalysis gasification response time in moving-burden bed reactor is 6-8min, and the temperature in external firing reactor is at 650-800 DEG C.
Beneficial effects of the present invention:
1. the method is to join in moving-burden bed reactor after being mixed with biomass material by cracking reforming catalyst, when the burning of reactor external fuel provides thermal source, biomass Non-oxygen pyrolytic is produced biogas, the tar supervened in biomass gasification process is also produced micro-molecular gas by In-stiu catalysis under the effect of catalyst, in addition, in the process, part CO is also generated H by catalytic reforming generation transformationreation2Discharge from moving-burden bed reactor afterbody together with the biomass carbon that catalyst after generation catalytic action produces with biomass pyrolytic, cracking reforming catalyst and biomass carbon is obtained through magnetic separation, cracking reforming catalyst recycles, and biomass carbon uses as the cracking carrier of reforming catalyst or adsorbent or the modifying agent as soil. The method compared with the conventional method, has the following advantages;
(1) a kind of continuous biomass raw material In-stiu catalysis gas, the method for charcoal coproduction proposed by the invention overcome and adopt the mode of interval to produce the deficiency existing for biomass carbon currently with biomass, and the problem that the tar produced when being solved for producing continuously by the In-stiu catalysis of tar affects continuous and steady operation, it is aided with the conversion catalytic reforming of CO again, improves available gas component H in pyrolysis gas product2While, make the application of gas produced wider; Additionally, this operating process is simple, continuously, stable, it is to avoid the tar produced in pyrolytic process adheres to each other with flying dust and to affect continuous and steady operation, improves the utilization ratio of biomass.
(2) a kind of continuous biomass raw material In-stiu catalysis gas proposed by the invention, the method of charcoal coproduction utilizes abundant biomass resource, biomass gasification process and external firing heat supplying process are integrated, catalytic pyrolysis and the CO of the tar gasified by the burning form biomass pyrolysis anaerobic of external fuel and supervene in gasification are reformed and provide heat energy, owing to biomass are the Non-oxygen pyrolytic gasifications under isolation external environmental condition, and with the cracking reforming process carried out in gasification, avoid a tar producing to the conversion of secondary tar aromatic compound, thus while reducing generation secondary coke tar cracking difficulty, while improve the cleavage rate of tar, maintain the activity of catalyst, make H in the gas effective ingredient produced2Content is improved significantly, and also greatly improves the specific surface area and porosity of biomass carbon, and the biomass carbon that the method obtains can be widely applied to adsorbent, the improvement field such as soil and catalyst carrier.
(3) the cracking reforming catalyst used in the inventive method is except having obvious catalytic cracking activity to tar, also there is CO and convert reformation effect, additionally, the oxide of ferrum and nickel and there is magnetic, it is easy to and biomass carbon Magnetic Isolation, it is achieved the recycling of catalyst.
2. continuous biomass raw material In-stiu catalysis gas provided by the invention, charcoal cogeneration facility are reasonable in design, it is simple to operation. In addition, in moving-burden bed reactor, biomass material and tar cracking catalyst are moved to while outlet is discharged to continuous pyrolysis from import by the flight that rotates of configuration, it is possible to making biomass be heated evenly in moving-burden bed reactor, pyrolysis is abundant, the biomass carbon produced is uniform, and specific surface area is high.
Accompanying drawing illustrates:
Fig. 1 continuous Novel external heat type biomass In-stiu catalysis gas, charcoal cogeneration facility schematic diagram. As it is shown in figure 1,1 feed bin, 2 moving-burden bed reactors, 3 rotate flights, 4 pyrolysis gas of biomass outlet, 5 biomass carbons with cracking reforming catalyst outlet, 6 external firing reactors, 7 fuel inlets, 8, exhanst gas outlet, 9 air compartments.
Fig. 2 has when being the gasification of biomass Non-oxygen pyrolytic, without In-stiu catalysis reforming catalyst time the gas on-line monitoring result that produces.
The absorption of the biomass carbon that Fig. 3 form biomass pyrolysis produces departs from attached curve.
Fig. 4 is the XRD phenogram of cracking reforming catalyst.
Detailed description of the invention:
It is described below in conjunction with the drawings and Examples concrete structure to the present invention and work process.
Embodiment 1
As shown in Figure 1, continuous external heating type biomass In-stiu catalysis gas, the equipment of charcoal coproduction, including for the moving-burden bed reactor 2 of biomass In-stiu catalysis and external firing reactor 6, moving-burden bed reactor is located in external firing reactor, moving-burden bed reactor one end be arranged over feed bin 1, the pyrolysis gas of biomass that is arranged over of the other end exports 4, it is connected with biomass carbon and catalyst for cracking outlet 5, the inside of moving-burden bed reactor is provided with rotation flight 3, rotate flight to be continuously fed to the mixture of the biomass material sent into through feed bin Yu catalyst for cracking under external force in the middle part of moving-burden bed reactor, carry out the pyrolysis of biomass carbon and cracking reforming process. external firing reactor is provided with fuel inlet 7 and the air compartment 9 of supply fuel combustion auxiliary agent, and the top of external firing reactor is additionally provided with combustion reactor exhanst gas outlet 8.
Entered in mobile reactor 2 by feed bin 1 after dry tree skill biomass material within long 10mm is mixed by the mass ratio of 7:1 with cracking reforming catalyst, the biomass being used for burning completely are sent into external firing reactor from the entrance 7 of external firing reactor 6, burn completely under the effect of the air of air compartment 9 offer, control air-fuel ratio simultaneously, combustion reaction temperature is controlled in 650-800 DEG C of temperature range, the flue gas produced after burning is discharged from 8, owing to moving-burden bed reactor is in external firing reactor 6, biomass fuels etc. burn in combustion reactor 6, the heat that burning produces passes through heat radiation, to flowing through and the heat of generation is supplied the biomass pyrolytic in moving-burden bed reactor 2 by conduction of heat and the tar In-stiu catalysis supervened is the heat needed for micro-molecular gas, part CO is also generated H by catalytic reforming simultaneously2, send into the biomass material in moving-burden bed reactor and cracking reforming catalyst continues under the effect of moving-burden bed reactor internal rotating scraper plate 3 and carries out the pyrolysis of biomass and the cracking process of tar in the middle part of moving-burden bed reactor, while biomass carbon that in moving-burden bed reactor, pyrolysis produces and catalyst move to biomass carbon and catalyst for cracking outlet 5 discharge under the effect rotating flight 3 from import, also the biomass in reactor are made to be heated evenly, the gas that in moving-burden bed reactor, biomass pyrolytic produces exports 4 outflows for rear operation from pyrolysis gas of biomass, H in the pyrolysis gas of biomass that moving-burden bed reactor is discharged2��CO��CH4Concentration of volume percent respectively 34%, 19% and 4%, gas production reaches 1.537Nm3/ kg biomass. By add catalyst and be not added with catalyst and produce gas analysis result compared with, (as shown in Figure 2), find by contrasting: add catalyst and be not added with in catalyst outlet gas hydrogen content and be significantly improved, bringing up to 34% from be not added with catalyst 14%. Obtaining biomass carbon and catalyst from the biomass carbon of biomass carbon with catalyst for cracking outlet 5 discharge after magnetic separation with catalyst, catalyst recycles. Specific surface area and the adsorpting characteristic curve of biomass carbon are as it is shown on figure 3, its specific surface area reaches 592.85m2/ g. Separate the biomass carbon produced to recycle as cracking Reforming catalyst agent carrier or adsorbent or the modifying agent as soil.
Above-mentioned cracking reforming catalyst is the biomass carbon separating generation after biomass cracking is carrier, by the nitrate of infusion process carried metal ferrum Yu nickel, forms again through 350 DEG C of vacuum calcinings, wherein: ferric nitrate is with Fe2O3Metering, nickel nitrate measures with NiO, and the mass percent of each component is: ferric nitrate 30%, nickel nitrate 20%, and surplus is high-area carbon. The XRD characterization result of this cracking reforming catalyst is shown in that Fig. 4, Fig. 4 can be seen that Fe occur when the angle of diffraction is 35 ��, 42 ��, 49 �� and 55 �� places2O3Obvious diffraction maximum, the obvious diffraction maximum of NiO occurs when the angle of diffraction is 38 ��, 43 �� and 63 �� places, charcoal is agraphitic carbon, occurs without obvious characteristic diffraction peak.
The present invention by adding the oxide Fe being carrier and supported on carriers ferrum with biomass carbon in biomass material2O3With the oxide NiO of the nickel cracking reforming catalyst formed, can based on cracking reforming catalyst to the cracking and catalyzing activity of tar and the reforming activity to CO, avoid a tar that biomass cracking produces to the conversion of secondary tar aromatic compound, thus reducing the cracking difficulty generating secondary tar, and the CO that can improve coke tar cracking generation passes through to convert reforming H2Efficiency, thereby guarantee that the content of available gas component such as hydrogen in the biomass cracking gases that biomass cracking produces.
Embodiment 2
Entered in mobile reactor 2 by feed bin 1 after rice husk biomass material is mixed by the mass ratio of 7.5:0.5 with cracking reforming catalyst, the biomass being used for burning completely are sent into external firing reactor from the entrance 7 of external firing reactor 6, burn completely under the effect of the air of air compartment 9 offer, control air-fuel ratio simultaneously, combustion reaction temperature is controlled in 650-800 DEG C of temperature range, the flue gas produced after burning is discharged from 8, owing to moving-burden bed reactor is in external firing reactor 6, biomass fuels etc. burn in combustion reactor 6, the heat that burning produces passes through heat radiation, to flowing through and the heat of generation is supplied the biomass pyrolytic in moving-burden bed reactor 2 by conduction of heat and the tar In-stiu catalysis supervened is the heat needed for micro-molecular gas, part CO is also generated H by catalytic reforming simultaneously2, send into the biomass material in moving-burden bed reactor and cracking reforming catalyst continues under the effect of moving-burden bed reactor internal rotating scraper plate 3 and carries out the pyrolysis of biomass and the cracking process of tar in the middle part of moving-burden bed reactor, while biomass carbon that in moving-burden bed reactor, pyrolysis produces and catalyst move to biomass carbon and catalyst for cracking outlet 5 discharge under the effect rotating flight 3 from import, also the biomass in reactor are made to be heated evenly, the gas that in moving-burden bed reactor, biomass pyrolytic produces exports 4 outflows for rear operation from pyrolysis gas of biomass, H in the pyrolysis gas of biomass that moving-burden bed reactor is discharged2��CO��CH4Concentration of volume percent respectively 30%, 16% and 2.5%, gas production reaches 1.125Nm3/ kg biomass. The specific surface area specific surface area of biomass carbon reaches 152.73m2/ g. Separate the biomass carbon produced to recycle as cracking Reforming catalyst agent carrier or adsorbent or the modifying agent as soil.
Above-mentioned cracking reforming catalyst is the biomass carbon separating generation after biomass cracking is carrier, by the nitrate of infusion process carried metal ferrum Yu nickel, forms again through 380 DEG C of vacuum calcinings, wherein: ferric nitrate is with Fe2O3Metering, nickel nitrate measures with NiO, and the mass percent of each component is: ferric nitrate 22%, nickel nitrate 28%, and surplus is high-area carbon. The XRD characterization result of this cracking reforming catalyst is shown in that Fig. 4, Fig. 4 can be seen that the angle of diffraction Fe occurs when being 35 ��, 42 ��, 49 �� and 55 �� places2O3Obvious diffraction maximum, the obvious diffraction maximum of NiO occurs when the angle of diffraction is 38 ��, 43 �� and 63 �� places, charcoal is agraphitic carbon, without characteristic diffraction peak appearance.
Claims (10)
1. a continuous external heating type biomass In-stiu catalysis gas, the equipment of charcoal coproduction, it is characterized in that: it includes the moving-burden bed reactor for biomass In-stiu catalysis and external firing reactor, moving-burden bed reactor is located in external firing reactor, moving-burden bed reactor one end be arranged over feed bin, the pyrolysis gas of biomass that is arranged over of the other end exports, it is connected with biomass carbon and cracking reforming catalyst outlet, the inside of moving-burden bed reactor is provided with rotation flight, rotate flight and under external force the mixture of the biomass material sent into through feed bin with cracking reforming catalyst is continuously fed in moving-burden bed reactor carry out the Non-oxygen pyrolytic of biomass and supervene the catalytic pyrolysis of tar, the conversion reforming process of CO.
2. the equipment of continuous external heating type biomass In-stiu catalysis gas according to claim 1, charcoal coproduction, it is characterized in that: external firing reactor is provided with fuel inlet and the air compartment of supply fuel combustion auxiliary agent, and the top of external firing reactor is additionally provided with combustion reactor exhanst gas outlet.
3. the equipment of continuous external heating type biomass In-stiu catalysis gas according to claim 1, charcoal coproduction, it is characterized in that: the fuel used by external burner is biomass, coal and natural gas, comburant is air, the addition of the blow rate required and fuel by controlling external firing reactor air, while making complete combustion of fuel, keep the temperature in external firing reactor at 650-800 DEG C.
4. a continuous external heating type biomass In-stiu catalysis gas, the method of charcoal coproduction, it is characterized in that: be sent in moving-burden bed reactor after biomass material is mixed with cracking reforming catalyst, fuel is sent into simultaneously the outside combustion outside moving-burden bed reactor anti-burn to answer in device fully burn, it is the required heat of micro-molecular gas supply for the biomass pyrolytic in moving-burden bed reactor and the tar In-stiu catalysis supervened, the mixture sending into the biomass material in moving-burden bed reactor and cracking reforming catalyst continues into the catalytic pyrolysis of the Non-oxygen pyrolytic carrying out biomass in moving-burden bed reactor and the tar supervened under the effect of moving-burden bed reactor internal rotating flight, the conversion reforming process of CO, the pyrolysis gas that biomass pyrolytic produces flows out for subsequent handling from the pyrolysis gas outlet of moving-burden bed reactor, cracking reforming catalyst after biomass carbon and catalytic reaction is moved to biomass carbon in the effect rotating flight and discharges with cracking reforming catalyst outlet.
5. the method for continuous external heating type biomass In-stiu catalysis gas according to claim 4, charcoal coproduction, it is characterised in that: the oxide Fe of the ferrum that described cracking reforming catalyst is produced by the calcining of biomass carbon carrier and supported on carriers2O3Form with the oxide NiO of nickel, wherein the oxide Fe of the oxide NiO of nickel and ferrum2O3Mass percent respectively 20-30%, 20-30%, surplus is high-area carbon.
6. the method for continuous external heating type biomass In-stiu catalysis gas according to claim 5, charcoal coproduction, it is characterized in that: described cracking reforming catalyst is for biomass carbon for carrier, by infusion process load ferric nitrate and nickel nitrate, form again through vacuum calcining, the calcining heat of vacuum calcining is 350-400 DEG C, wherein: ferric nitrate is with Fe2O3Metering, nickel nitrate measures with NiO, and the mass percent of each component is: ferric nitrate 20-30%, nickel nitrate 20-30%, and surplus is high-area carbon.
7. the method for continuous external heating type biomass In-stiu catalysis gas according to claim 4, charcoal coproduction, it is characterised in that: described biomass material and the mass percent cracking reforming catalyst in cracking reforming catalyst are 6.25-12.5wt%.
8. the method for continuous external heating type biomass In-stiu catalysis gas according to claim 4, charcoal coproduction, it is characterized in that: the biomass In-stiu catalysis gasification response time in moving-burden bed reactor is 6-8min, and the temperature of external firing reactor is 650-800 DEG C.
9. the method for continuous external heating type biomass In-stiu catalysis gas according to claim 4, charcoal coproduction, it is characterized in that: the charcoal discharged from biomass carbon and cracking reforming catalyst outlet obtains biomass carbon and cracking reforming catalyst with cracking reforming catalyst after magnetic separation, cracking reforming catalyst recycles, and biomass carbon uses as the cracking carrier of reforming catalyst or adsorbent or the modifying agent as soil.
10. the method for continuous external heating type biomass In-stiu catalysis gas according to claim 4, charcoal coproduction, it is characterised in that: the particle diameter of biomass is at below 10mm, and water content mass percent is below 10%.
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| CN106378348A (en) * | 2016-10-31 | 2017-02-08 | 新奥生态环境治理有限公司 | Garbage treatment and resource utilization method |
| CN106582663A (en) * | 2016-10-19 | 2017-04-26 | 中国科学院过程工程研究所 | Method for in situ catalytic removal of tar in biomass pyrolysis process |
| CN108758638A (en) * | 2018-03-27 | 2018-11-06 | 清华大学 | A kind of air classification regulation and control pyrolysis and combustion all-in-one oven |
| CN111218291A (en) * | 2020-03-09 | 2020-06-02 | 中国农业科学院农业环境与可持续发展研究所 | Pyrolysis, carbonization and catalysis integrated method |
| CN112126450A (en) * | 2020-09-29 | 2020-12-25 | 华中科技大学 | Light-gathering pyrolysis catalytic reforming system and method based on spectrum splitting |
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