CN110066670B - Catalyst regenerated biomass continuous catalytic pyrolysis method and integrated device - Google Patents
Catalyst regenerated biomass continuous catalytic pyrolysis method and integrated device Download PDFInfo
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- CN110066670B CN110066670B CN201910392362.2A CN201910392362A CN110066670B CN 110066670 B CN110066670 B CN 110066670B CN 201910392362 A CN201910392362 A CN 201910392362A CN 110066670 B CN110066670 B CN 110066670B
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- 239000003054 catalyst Substances 0.000 title claims abstract description 151
- 239000002028 Biomass Substances 0.000 title claims abstract description 62
- 238000007233 catalytic pyrolysis Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000000197 pyrolysis Methods 0.000 claims abstract description 118
- 238000001833 catalytic reforming Methods 0.000 claims abstract description 87
- 239000010453 quartz Substances 0.000 claims abstract description 78
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 78
- 230000008929 regeneration Effects 0.000 claims abstract description 61
- 238000011069 regeneration method Methods 0.000 claims abstract description 61
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 12
- 238000009833 condensation Methods 0.000 claims abstract description 6
- 230000005494 condensation Effects 0.000 claims abstract description 6
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 85
- 238000005485 electric heating Methods 0.000 claims description 39
- 230000001172 regenerating effect Effects 0.000 claims description 17
- 239000010410 layer Substances 0.000 claims description 16
- 238000007599 discharging Methods 0.000 claims description 13
- 239000011261 inert gas Substances 0.000 claims description 12
- 239000012159 carrier gas Substances 0.000 claims description 11
- 238000003756 stirring Methods 0.000 claims description 10
- 238000012544 monitoring process Methods 0.000 claims description 9
- 238000005192 partition Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 7
- 230000005540 biological transmission Effects 0.000 claims description 6
- 229920000742 Cotton Polymers 0.000 claims description 5
- 239000011229 interlayer Substances 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 238000009413 insulation Methods 0.000 claims description 3
- 230000005855 radiation Effects 0.000 claims description 3
- 230000008021 deposition Effects 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 6
- 230000000694 effects Effects 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 230000001276 controlling effect Effects 0.000 description 6
- 230000009849 deactivation Effects 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000004888 barrier function Effects 0.000 description 2
- 239000012075 bio-oil Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910000288 alkali metal carbonate Inorganic materials 0.000 description 1
- 150000008041 alkali metal carbonates Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
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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
-
- 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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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- Wood Science & Technology (AREA)
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Abstract
The invention discloses a biomass continuous catalytic pyrolysis method for catalyst regeneration and an integrated device, wherein the method comprises the steps of heating a catalyst regeneration zone in an anaerobic environment, receiving corresponding radiant heat by a pyrolysis zone, a tar removal zone and a catalytic reforming zone of a vertical quartz tube, and generating pyrolysis gas and biochar after pyrolysis of biomass in the pyrolysis zone, wherein the biochar forms the tar removal zone, and the pyrolysis gas is subjected to tar removal, pyrolysis catalysis and condensation collection; after the catalyst in the catalytic reforming zone is deactivated, the catalyst is collected in a deactivated catalyst collection zone, then fed into a catalyst regeneration zone through a screw feeder to effect regeneration of the deactivated catalyst, and then returned to the catalytic reforming zone. The integrated device links the two processes of catalytic pyrolysis and catalyst regeneration which are commonly separated in the same device, realizes the graded utilization of heat, has high energy utilization efficiency, saves energy and protects environment, can be widely applied to the field of biomass pyrolysis, and has wider application prospect.
Description
Technical Field
The invention relates to an integrated method for improving biomass catalytic pyrolysis efficiency, in particular to a biomass continuous catalytic pyrolysis method for regenerating a catalyst and an integrated device.
Background
With the increasing level of living of people, the consumption of energy and the generation of waste are increasing. On the one hand, fossil energy is exhausted daily, and on the other hand, waste is deposited and hilled due to incomplete utilization of energy. These two problems make efficient and rational use of energy source urgent. Compared with non-renewable resources such as fossil energy, renewable biomass resources have wide prospects. Biomass resources are abundant today, but the technology of conversion utilization is still immature, so that the search for better means of biomass conversion utilization is the direction that many researchers are striving to.
There are many studies on pyrolysis of biomass at home and abroad, and a certain theoretical basis is formed. In the field of bio-oil refining, the methods which are relatively common at present are a catalytic pyrolysis method and a catalytic hydrodeoxygenation method. The catalytic pyrolysis method mainly comprises the steps of carrying out pyrolysis experiments under the environment pressure, and then carrying out catalytic reforming on the generated pyrolysis gas in a catalyst to crack light oil components similar to gasoline. Compared with the catalytic hydrodeoxygenation method, the method omits the pressurizing process, and simplifies, facilitates and economizes the experimental operation flow.
During biomass catalytic pyrolysis, tar is a substance which can be inevitably generated, and the characteristic of high volatile content of biomass determines that more tar is generated in the biomass pyrolysis process than coal, and the characteristic severely restricts the development of biomass pyrolysis technology. Tar removal is a critical issue in the development of biomass pyrolysis.
ZSM-5 is often used in catalytic pyrolysis reactions of biomass, which can improve the quality of bio-oil to some extent. However, ZSM-5 has smaller pore diameter and larger reaction diffusion resistance for macromolecules, and reactants are easy to coke and deactivate on the surface of the ZSM-5, so that the reduction of the deactivation of the catalyst is an important aspect for the efficient utilization of the catalyst. ZSM-5 has high thermal stability, one of the highest thermal stability known for zeolites, and can withstand the high temperatures encountered in regenerating the catalyst. And normally, the carbon deposit in ZSM-5 can be burnt out at 900 ℃, the activity of the catalyst is recovered, and the regeneration recovery is realized.
The solid product obtained after biomass pyrolysis is the biochar, and the biochar has the potential of becoming a cheap catalyst for removing tar because the biochar has a loose and porous structure and contains more alkali metal carbonate in ash, and has the basic conditions of catalytic conversion and catalytic pyrolysis of tar. The use of biochar for tar removal can reduce the deactivation and the use amount of commercial catalysts and reduce the reaction cost. But biochar only plays a role in tar removal above 700 ℃. While the optimum pyrolysis temperature of biomass is generally considered to be around 500 ℃.
Usually, biomass pyrolysis and catalyst regeneration are carried out separately, and the problem of high energy consumption exists. In consideration of the gradient distribution of optimal reaction temperature of biomass pyrolysis, tar removal and catalyst regeneration, a method and a device for utilizing the temperature gradient to efficiently and reasonably utilize energy and reaction materials are developed.
Disclosure of Invention
In order to overcome the defects and shortcomings of the prior art, the invention aims to provide a continuous catalytic pyrolysis method and a device for improving the quality of biomass pyrolysis oil, wherein the continuous catalytic pyrolysis method is capable of efficiently utilizing energy and recycling a catalyst.
In order to achieve the above object, the present invention provides the following technical solutions.
The invention provides a biomass continuous catalytic pyrolysis integrated device for catalyst regeneration, which comprises a gas device, a vertical quartz tube, a catalyst regeneration zone, a catalytic reforming zone, an inactive catalyst collecting zone, a spiral feeder and a condensing zone; the gas device is connected to the side wall of the vertical quartz tube, inert gas is introduced into the vertical quartz tube, biomass is placed in the vertical quartz tube, and the inert gas provides an anaerobic environment and carrier gas for the biomass; the vertical quartz tube sequentially comprises a feeding area, a pyrolysis area, a tar removal area and a discharging area from top to bottom, wherein an inlet is arranged on the feeding area, an outlet is arranged at the bottom of the discharging area, biomass is added from the inlet, pyrolysis gas and biochar are generated after the biomass is pyrolyzed in the pyrolysis area, the biochar enters the tar removal area to form a biochar bed layer, the pyrolysis gas downwards flows through the tar removal area along with carrier gas to remove tar, and the biochar is discharged from the outlet; one side of the catalytic reforming zone is connected with the bottom end of the side wall of the vertical quartz tube of the discharging zone, the other side of the catalytic reforming zone is connected with the condensing zone, a catalyst is placed in the catalytic reforming zone, pyrolysis gas flow after tar removal is cracked and catalyzed by the catalytic reforming zone, and pyrolysis gas after pyrolysis and catalysis enters the condensing zone to be collected; the lower part of the catalytic reforming zone is connected with an inactivated catalyst collecting zone, the inactivated catalyst collecting zone is used for collecting the inactivated catalyst in the catalytic reforming zone, the upper part of the catalytic reforming zone is connected with a catalyst regenerating zone, and the catalyst regenerating zone is used for regenerating the inactivated catalyst; a spiral feeder is connected between the deactivated catalyst collecting area and the catalyst regenerating area, the deactivated catalyst is added into the catalyst regenerating area through the spiral feeder, and after being regenerated, the deactivated catalyst returns to the catalytic reforming area from the catalyst regenerating area.
Preferably, the catalyst regeneration zone comprises a box-type electric heating furnace, an opening is arranged at the upper part of the box-type electric heating furnace, deactivated catalyst is added into the catalyst regeneration zone through the opening, air is introduced into the catalyst regeneration zone, the bottom of the box-type electric heating furnace is a heat insulation layer, heat provided by the box-type electric heating furnace is prevented from directly radiating the catalytic reforming zone, the temperature of the catalytic reforming zone is overhigh, the side wall of the box-type electric heating furnace is a heat conduction layer, the heat provided by the box-type electric heating furnace is radiated to the pyrolysis zone and the tar removal zone of the vertical quartz tube through the side wall, and the catalytic reforming zone is used for providing heat for pyrolysis of biomass in the pyrolysis zone, tar removal of pyrolysis gas and pyrolysis catalysis of pyrolysis gas.
Preferably, the integrated device further comprises a controllable adjusting baffle, the controllable adjusting baffle comprises a first controllable adjusting baffle and a second controllable adjusting baffle, the first controllable adjusting baffle is arranged on the side wall of the vertical quartz tube in the pyrolysis zone, the second controllable adjusting baffle is arranged on the side wall of the vertical quartz tube in the tar removal zone, the controllable adjusting baffle is opposite to the side wall of the box-type electric heating furnace, the receiving quantity of the radiation heat of the side wall of the box-type electric heating furnace is adjusted, and the temperatures of the pyrolysis zone and the tar removal zone are controlled.
Preferably, the integrated device further comprises a stirring assembly, the stirring assembly comprises a stirrer, an impeller and a transmission device between the stirrer and the impeller, the stirrer and the impeller are coaxially arranged, the stirrer is placed between biomasses in the vertical quartz tube, the impeller is arranged at the opening of the box-type electric heating furnace, after the box-type electric heating furnace heats, air in the catalyst regeneration zone is heated and rises, the impeller is driven to rotate, and the impeller drives the stirrer to stir through the transmission device.
Preferably, the integrated device further comprises a valve, wherein the valve comprises a first valve, a second valve and a third valve; a first pipeline is connected between the catalyst regeneration zone and the catalytic reforming zone, and a first valve and a second valve are distributed on the first pipeline from top to bottom; and a second pipeline is connected between the catalytic reforming zone and the deactivated catalyst collecting zone, and third valves are distributed on the second pipeline and are heat-insulating valves.
Preferably, the integrated device further comprises a temperature controller, wherein the temperature controller comprises a first temperature controller, a second temperature controller and a third temperature controller, and the first temperature controller is arranged on the side wall of the vertical quartz tube of the pyrolysis zone and used for monitoring the temperature of the pyrolysis zone; the second temperature controller is arranged on the side wall of the vertical quartz tube in the tar removing area and is used for monitoring the temperature of the tar removing area; the third temperature controller is arranged on the catalytic reforming zone and is used for monitoring the temperature of the catalytic reforming zone.
Preferably, the integrated device further comprises a heat collection box, wherein the heat collection box is a cavity surrounded by a thermal resistance material layer, and the pyrolysis zone, the tar removal zone, the catalytic reforming zone and the catalyst regeneration zone of the vertical quartz tube are positioned in the cavity.
Preferably, the integrated device further comprises a flowmeter, the flowmeter comprises a first flowmeter and a second flowmeter, the gas device is connected with the vertical quartz tube through parallel pipelines, and the parallel pipelines comprise an upper pipeline and a lower pipeline; one end of the upper pipeline is connected with the gas device, and the other end of the upper pipeline is connected with the side wall of the vertical quartz tube in the feeding area; one end of the lower pipeline is connected with the gas device, and the other end of the lower pipeline is connected with the side wall of the vertical quartz tube in the discharging area; the first flowmeter is arranged on the upper pipeline and used for controlling the flow of inert gas in the upper pipeline; the second flowmeter is arranged on the lower pipeline and used for controlling the flow of inert gas in the lower pipeline; a quartz cotton interlayer is arranged at the joint of the vertical quartz tube and the catalytic reforming zone and the joint of the catalytic reforming zone and the condensation zone; the condensing zone comprises a condensing device and a gas collecting device, one side of the condensing device is connected with the catalytic reforming zone, the other side of the condensing device is connected with the gas collecting device, pyrolysis gas passing through the catalytic reforming zone is catalytically cracked and then enters the condensing device, condensing gas in the pyrolysis gas is condensed into liquid, and non-condensing gas enters the gas collecting device and is collected.
Preferably, a baffle plate is arranged at the opening of the box-type electric heating furnace, the impeller is arranged at the left side of the baffle plate, and the deactivated catalyst enters the catalyst regeneration zone from the right side of the baffle plate.
Preferably, the valve is an adiabatic valve, after the deactivated catalyst is regenerated in the catalyst regeneration zone, the first valve is opened, the second valve is closed, after the first pipeline between the first valve and the second valve is filled with the regenerated catalyst, the first valve is closed, the regenerated catalyst is stored in the first pipeline between the first valve and the second valve, when the temperature of the regenerated catalyst is reduced to the temperature of the catalytic reforming zone, the second valve is opened, and the regenerated catalyst returns to the catalytic reforming zone; the diameter of the inlet of the vertical quartz tube is larger than that of the outlet, so that the biomass is ensured to stay in the vertical quartz tube for a plurality of times.
The invention also provides a method for carrying out biomass continuous catalytic pyrolysis by using the biomass continuous catalytic pyrolysis integrated device regenerated by the catalyst, which comprises the following steps:
1) Opening a gas device, and introducing inert gas into the integrated device to ensure an anaerobic environment of the pyrolysis reaction;
2) Heating the catalyst regeneration zone to 850-900 ℃, receiving corresponding radiant heat by the pyrolysis zone, the tar removal zone and the catalytic reforming zone of the vertical quartz tube, wherein the temperature reached by the pyrolysis zone of the vertical quartz tube is 500-550 ℃, the temperature reached by the tar removal zone of the vertical quartz tube is 700-750 ℃, and the temperature reached by the catalytic reforming zone is 450-500 ℃;
3) Biomass is pyrolyzed in a pyrolysis zone of a vertical quartz tube to generate pyrolysis gas and biochar, the biochar forms a biochar bed layer, namely a tar removal zone, the pyrolysis gas downwards flows through the tar removal zone along with carrier gas to remove tar, pyrolysis gas flow after tar removal is pyrolyzed and catalyzed in a catalytic reforming zone, and pyrolysis gas after pyrolysis catalysis enters a condensing zone to be collected; under the action of gravity, the early biochar is discharged from the outlet of the discharging area, and the newly-entered biomass reacted biochar is used as a new biochar bed layer, so that continuous catalytic pyrolysis reaction is realized; in order to prevent the pyrolysis gas from escaping from the outlet, a certain flow of carrier gas is introduced from the upper pipeline to play a role of a gas barrier, so that the pyrolysis gas is prevented from passing through while biochar is allowed to fall down;
4) The catalyst in the catalytic reforming zone is deactivated and then is collected in a deactivated catalyst collecting zone, and then is sent to a catalyst regenerating zone through a screw feeder, the deactivated catalyst is calcined for 3-5 hours at 850-900 ℃ in the catalyst regenerating zone, carbon deposit is burnt out, the regeneration of the deactivated catalyst is realized, and then the deactivated catalyst is returned to the catalytic reforming zone.
Compared with the prior art, the invention has the following beneficial effects and advantages:
(1) The invention relates to a method for combining two processes of catalytic pyrolysis and catalyst regeneration which are commonly separated in the existing catalytic pyrolysis technology in the same set of device, thereby improving the reaction efficiency and greatly reducing the occupied space of the device.
(2) The invention can meet the heat requirement of the whole system by only needing one heat source. And radiating heat to the pyrolysis zone, the tar removal zone and the catalytic reforming zone by utilizing the excess heat quantity after the high-temperature reaction at 850-900 ℃ required by catalyst regeneration. The invention also utilizes the rising heat flow at the opening of the catalyst regeneration zone, the heat energy is converted into mechanical energy, and the impeller is driven to rotate so as to drive the stirrer, so that the heat quantity of the materials is more uniform. The invention realizes the graded utilization of energy and improves the utilization efficiency of heat.
(3) According to the invention, the controllable regulating baffles with different thermal resistances are respectively arranged in the catalyst regeneration zone and the pyrolysis zone, and the catalyst regeneration zone and the tar removal zone, the control of the absorbed radiant heat can be realized by regulating the opening of the baffles, the temperatures of the pyrolysis zone and the tar removal zone can be controlled in real time, and the flexibility of an experimental device is enhanced.
(4) According to the invention, solid residues after biomass pyrolysis reaction are used as a biochar layer, and the characteristics of loose and porous biochar are utilized to remove tar from pyrolysis gas, so that the deactivation rate of a catalyst in a subsequent catalytic reforming zone is slowed down, and the utilization efficiency of biomass and the catalyst is improved.
Drawings
Fig. 1 is a schematic diagram of a biomass continuous catalytic pyrolysis integrated device for catalyst regeneration provided in the examples.
Detailed Description
The present invention will be described in further detail with reference to specific examples.
Examples
As shown in fig. 1, the embodiment provides a biomass continuous catalytic pyrolysis integrated device for catalyst regeneration, which comprises a gas device 1, a vertical quartz tube 4, a catalyst regeneration zone 11, a catalytic reforming zone 14, an inactive catalyst collecting zone 17, a spiral feeder 18 and a condensation zone; the gas device 1 is connected to the side wall of the vertical quartz tube 4, inert gas and nitrogen are introduced into the vertical quartz tube 4, biomass is placed in the vertical quartz tube 4, and the nitrogen provides an anaerobic environment and carrier gas for the biomass; the vertical quartz tube 4 sequentially comprises a feeding area, a pyrolysis area, a tar removal area and a discharging area from top to bottom, wherein an opening is formed in the feeding area, an outlet is formed in the bottom of the discharging area, pyrolysis gas and biochar are generated after biomass is pyrolyzed in the pyrolysis area, the biochar enters the tar removal area to form a biochar bed, and the pyrolysis gas flows downwards along with carrier gas through the tar removal area to be removed of tar; one side of the catalytic reforming zone 14 is connected with the bottom end of the side wall of the vertical quartz tube 4 of the discharging zone, the other side is connected with the condensing zone, a catalyst ZSM-5 is placed in the catalytic reforming zone 14, pyrolysis gas flow after tar removal is subjected to pyrolysis catalysis through the catalytic reforming zone 14, and pyrolysis gas after pyrolysis catalysis enters the condensing zone to be collected; the lower part of the catalytic reforming zone 14 is connected with an inactive catalyst collecting zone 17, the inactive catalyst collecting zone 17 is used for collecting inactive catalyst in the catalytic reforming zone 14, the upper part is connected with a catalyst regenerating zone 11, and the catalyst regenerating zone 11 is used for regenerating the inactive catalyst; a screw feeder 18 is connected between the deactivated catalyst collecting zone 17 and the catalyst regeneration zone 11, and the deactivated catalyst is added into the catalyst regeneration zone 11 through the screw feeder 18, and after being regenerated, the deactivated catalyst returns from the catalyst regeneration zone 11 to the catalytic reforming zone 14.
The catalyst regeneration zone 11 comprises a box-type electric heating furnace, an opening is arranged at the upper part of the box-type electric heating furnace, deactivated catalyst is added into the catalyst regeneration zone 11 through the opening, air is introduced into the catalyst regeneration zone, the bottom of the box-type electric heating furnace is a heat insulation layer, heat provided by the box-type electric heating furnace is prevented from directly radiating the catalytic reforming zone 14, the temperature of the catalytic reforming zone 14 is overhigh, the side wall of the box-type electric heating furnace is a heat conduction layer, the heat provided by the box-type electric heating furnace is radiated to the pyrolysis zone and the tar removal zone of the vertical quartz tube 4 through the side wall, and the catalytic reforming zone 14 provides heat for pyrolysis of biomass in the pyrolysis zone, tar removal of pyrolysis gas and pyrolysis catalysis of pyrolysis gas.
The integrated device further comprises a controllable adjusting baffle, the controllable adjusting baffle comprises a first controllable adjusting baffle 8 and a second controllable adjusting baffle 9, the first controllable adjusting baffle 8 is arranged on the side wall of the vertical quartz tube 4 in the pyrolysis zone, the second controllable adjusting baffle 9 is arranged on the side wall of the vertical quartz tube 4 in the tar removal zone, the controllable adjusting baffle is opposite to the side wall of the box-type electric heating furnace, the receiving quantity of the radiation heat of the side wall of the box-type electric heating furnace is adjusted, and the temperatures of the pyrolysis zone and the tar removal zone are controlled.
The integrated device further comprises a stirring assembly, the stirring assembly comprises a stirrer 6, an impeller 10 and a transmission device between the stirrer 6 and the impeller 10, the stirrer 6 and the impeller 10 are coaxially arranged, the stirrer 6 is placed between biomasses in the vertical quartz tube 4, the impeller 10 is arranged at the opening of the box-type electric heating furnace, after the box-type electric heating furnace is heated, air in the catalyst regeneration zone 11 is heated and rises, the impeller 10 is driven to rotate, and the impeller 10 drives the stirrer 6 to stir through the transmission device.
The integrated device also comprises valves, wherein the valves comprise a first valve 12, a second valve 13 and a third valve 15; a first pipeline is connected between the catalyst regeneration zone 11 and the catalytic reforming zone 14, and a first valve 12 and a second valve 13 are distributed on the first pipeline from top to bottom; a second conduit is connected between the catalytic reforming zone 14 and the deactivated catalyst collection zone 17, and a third valve 15 is distributed over the second conduit, said valve being an adiabatic valve.
The integrated device further comprises a temperature controller, wherein the temperature controller comprises a first temperature controller 5, a second temperature controller 7 and a third temperature controller 16, and the first temperature controller 5 is arranged on the side wall of the vertical quartz tube 4 of the pyrolysis zone and is used for monitoring the temperature of the pyrolysis zone; the second temperature controller 7 is arranged on the side wall of the vertical quartz tube 4 of the tar removal zone and is used for monitoring the temperature of the tar removal zone; a third thermostat 16 is provided on the catalytic reforming zone 14 for monitoring the temperature of the catalytic reforming zone 14.
The integrated device further comprises a heat collection box 21, wherein the heat collection box 21 is a cavity surrounded by a thermal resistance material layer, and the pyrolysis zone and the tar removal zone of the vertical quartz tube 4, the catalytic reforming zone 14 and the catalyst regeneration zone 11 are positioned in the cavity.
The integrated device also comprises a flowmeter, wherein the flowmeter comprises a first flowmeter 2 and a second flowmeter 3, the gas device 1 is connected with the vertical quartz tube 4 through parallel pipelines, and the parallel pipelines comprise an upper pipeline and a lower pipeline; one end of the upper pipeline is connected with the gas device 1, and the other end is connected with the side wall of the vertical quartz tube 4 in the feeding area; one end of the lower pipeline is connected with the gas device 1, and the other end is connected with the side wall of the vertical quartz tube 4 in the discharging area; the first flowmeter 2 is arranged on the upper pipeline and is used for controlling the flow of inert gas in the upper pipeline; the second flowmeter 3 is arranged on the lower pipeline and is used for controlling the inert gas flow of the lower pipeline; a quartz cotton interlayer is arranged at the joint of the vertical quartz tube 4 and the catalytic reforming zone 14 and the joint of the catalytic reforming zone 14 and the condensation zone; the condensing zone comprises a condensing device 19 and a gas collecting device 20, one side of the condensing device 19 is connected with the catalytic reforming zone 14, the other side of the condensing device 19 is connected with the gas collecting device 20, pyrolysis gas passing through the catalytic reforming zone 14 is catalytically cracked and then enters the condensing device 19, condensing gas in the pyrolysis gas is condensed into liquid, and non-condensing gas enters the gas collecting device 20 and is collected.
A partition plate is arranged at the opening of the box-type electric heating furnace, an impeller 10 is arranged at the left side of the partition plate, and deactivated catalyst enters a catalyst regeneration zone 11 from the right side of the partition plate.
The embodiment also provides a method for continuous catalytic pyrolysis of biomass by using the integrated device, which comprises the following steps:
(1) The gas device 1 is filled with nitrogen, the gas device 1 is opened, the nitrogen is introduced into the integrated device, the anaerobic environment of biomass is ensured, and the gas flow of the upper pipeline and the lower pipeline is respectively controlled by the first flowmeter 2 and the second flowmeter 3 so as to ensure that the requirement of the integrated device is met;
(2) Starting a box-type electric heating furnace, heating the catalyst regeneration zone 11 to 900 ℃, receiving corresponding radiant heat by a pyrolysis zone, a tar removal zone and a catalytic reforming zone 14 of the vertical quartz tube 4, wherein the temperature reached by the pyrolysis zone of the vertical quartz tube 4 is 500 ℃, the temperature reached by the tar removal zone of the vertical quartz tube 4 is 750 ℃, the temperature reached by the catalytic reforming zone 14 is 450 ℃, and controlling the receiving quantity of radiant heat to the side wall of the box-type electric heating furnace by controlling the opening of a first controllable regulating baffle 8 and a second controllable regulating baffle 9 according to feedback of a first temperature controller 5, a second temperature controller 7 and a third temperature controller 16 so as to control the temperature; the heat collection box 21 surrounds the vertical quartz tube 4, the catalyst regeneration zone 11 and the catalytic reforming zone 14, and plays a role of collecting the radiant heat of the box-type electric heating furnace, so that the pyrolysis zone, the tar removal zone and the catalytic reforming zone of the vertical quartz tube 4 can reach the set temperature more easily. The heat collection box 21 is made of a specific heat resistance material, so that a certain heat dissipation capacity can be ensured to the outside, heat accumulation in the heat collection box 21 is avoided, and the heat stability of the whole integrated device is maintained.
(3) The biomass is put in from the opening of the vertical quartz tube 4, and the structure of the wide-in and narrow-out of the vertical quartz tube 4 can ensure that the biomass has a certain residence time in the flowing process. Along with the rising of high-temperature pyrolysis air in the box-type electric heating furnace, the impeller 10 is driven to rotate, the impeller 10 is further driven to stir by the stirrer 6, so that the heat distribution of biomass is more uniform, pyrolysis gas and biochar are generated after the biomass is pyrolyzed in a pyrolysis zone of the vertical quartz tube 4, the biochar forms a biochar bed layer, namely a tar removal zone, in the vertical quartz tube 4, the pyrolysis gas downwards flows through the tar removal zone along with carrier gas to remove tar, pyrolysis gas after tar removal is pyrolyzed and catalyzed by the catalytic reforming zone 14, the pyrolysis gas after pyrolysis catalysis enters a condensing device 19 of a condensing zone, condensable gas is condensed into liquid, and non-condensable gas is collected in a gas collecting bag 20; in addition, a path of carrier gas is transversely blown into the upper part of the opening of the vertical quartz tube 4 to form a gas barrier, so that pyrolysis gas cannot escape along with biomass from the outlet. A quartz cotton interlayer is arranged between the vertical quartz tube 4 and the catalytic reforming zone 14, so that pyrolysis gas can flow smoothly and materials can be prevented from passing through.
(4) After deactivation of the catalytic reforming zone 14, the third valve 15 is opened to allow the deactivated catalyst to fall into the deactivated catalyst collection zone 17. The deactivated catalyst is then fed into the catalyst regeneration zone 11 via a screw feeder 18 to burn off the carbon deposits and effect catalyst regeneration. To prevent the catalyst from being affected by the impeller 10 during the falling process, a partition plate is provided at the opening of the box-type electric heating furnace to divide the opening into two. The impeller is placed on the left side of the partition and the deactivated catalyst is placed in the furnace from the right side of the partition. The deactivated catalyst was calcined and regenerated in a box-type electric heating furnace at a high temperature of 900 c for 5 hours. The first valve 12 is then opened and the second valve 13 remains closed. When the pipe between the first valve 12 and the second valve 13 is full, the first valve 12 is closed. The regenerated catalyst is temporarily stored in the pipeline between the first valve 12 and the second valve 13, and simultaneously radiates heat to the periphery outwards for cooling. After the regenerated catalyst temperature is reduced to 500 ℃, the first valve 12 is kept closed, and the second valve 13 is opened, so that the regenerated catalyst falls into the catalytic reforming zone 14 to participate in the reaction. The joint of the catalytic reforming zone 14 and the pyrolysis gas channels at the left end and the right end is also provided with a quartz cotton interlayer, so that the flow of the pyrolysis gas is ensured and the catalyst is prevented from flowing out from the left end and the right end.
The embodiments of the present invention are not limited to the above examples, and any other changes, modifications, substitutions, combinations, and simplifications that do not depart from the spirit and principles of the invention should be made and equivalents should be construed as falling within the scope of the invention.
Claims (6)
1. The biomass continuous catalytic pyrolysis integrated device for regenerating the catalyst is characterized by comprising a gas device (1), a vertical quartz tube (4), a catalyst regeneration zone (11), a catalytic reforming zone (14), an inactive catalyst collecting zone (17), a spiral feeder (18) and a condensing zone; the gas device (1) is connected to the side wall of the vertical quartz tube (4), inert gas is introduced into the vertical quartz tube (4), biomass is placed in the vertical quartz tube (4), and the inert gas provides an anaerobic environment and carrier gas for the biomass; the vertical quartz tube (4) is sequentially provided with a feeding area, a pyrolysis area, a tar removal area and a discharging area from top to bottom, an inlet is arranged on the feeding area, an outlet is arranged at the bottom of the discharging area, biomass is added from the inlet, pyrolysis gas and biochar are generated after the biomass is pyrolyzed in the pyrolysis area, the biochar enters the tar removal area to form a biochar bed layer, the pyrolysis gas flows downwards along with carrier gas to the tar removal area to remove tar, and the biochar is discharged from the outlet; one side of the catalytic reforming zone (14) is connected with the bottom end of the side wall of the vertical quartz tube (4) of the discharging zone, the other side of the catalytic reforming zone is connected with the condensing zone, a catalyst is placed in the catalytic reforming zone (14), pyrolysis gas flow after tar removal is subjected to pyrolysis catalysis through the catalytic reforming zone (14), and pyrolysis gas after pyrolysis catalysis enters the condensing zone to be collected; the lower part of the catalytic reforming zone (14) is connected with an inactivated catalyst collecting zone (17), the inactivated catalyst collecting zone (17) is used for collecting the inactivated catalyst in the catalytic reforming zone (14), the upper part of the catalytic reforming zone is connected with a catalyst regenerating zone (11), and the catalyst regenerating zone (11) is used for regenerating the inactivated catalyst; a screw feeder (18) is connected between the deactivated catalyst collecting zone (17) and the catalyst regeneration zone (11), the deactivated catalyst is added into the catalyst regeneration zone (11) through the screw feeder (18), and after the deactivated catalyst is regenerated, the deactivated catalyst returns to the catalytic reforming zone (14) from the catalyst regeneration zone (11); the catalyst regeneration zone (11) comprises a box-type electric heating furnace, an opening is arranged at the upper part of the box-type electric heating furnace, an inactivated catalyst is added into the catalyst regeneration zone (11) through the opening, air is introduced into the catalyst regeneration zone, the bottom of the box-type electric heating furnace is provided with a heat insulation layer, heat provided by the box-type electric heating furnace is prevented from directly radiating the catalytic reforming zone (14), the temperature of the catalytic reforming zone (14) is overhigh, the side wall of the box-type electric heating furnace is provided with a heat conduction layer, the heat provided by the box-type electric heating furnace is radiated to the pyrolysis zone and the tar removal zone of the vertical quartz tube (4) through the side wall, and the heat is provided for pyrolysis of biomass in the pyrolysis zone, tar removal of pyrolysis gas and pyrolysis catalysis of pyrolysis gas; the integrated device further comprises a controllable adjusting baffle, the controllable adjusting baffle comprises a first controllable adjusting baffle (8) and a second controllable adjusting baffle (9), the first controllable adjusting baffle (8) is arranged on the side wall of the vertical quartz tube (4) in the pyrolysis zone, the second controllable adjusting baffle (9) is arranged on the side wall of the vertical quartz tube (4) in the tar removing zone, the controllable adjusting baffle is opposite to the side wall of the box-type electric heating furnace, the receiving amount of radiation heat of the side wall of the box-type electric heating furnace is adjusted, and the temperatures of the pyrolysis zone and the tar removing zone are controlled; the integrated device further comprises a stirring assembly, the stirring assembly comprises a stirrer (6), an impeller (10) and a transmission device between the stirrer (6) and the impeller (10), the stirrer (6) and the impeller (10) are coaxially arranged, the stirrer (6) is placed between biomasses in the vertical quartz tube (4), the impeller (10) is arranged at an opening of the box-type electric heating furnace, after the box-type electric heating furnace heats, air in the catalyst regeneration zone (11) is heated and rises to drive the impeller (10) to rotate, and the impeller (10) drives the stirrer (6) to stir through the transmission device; the integrated device further comprises a heat collection box (21), wherein the heat collection box (21) is a cavity surrounded by a heat resistance material layer, and a pyrolysis zone and a tar removal zone of the vertical quartz tube (4), a catalytic reforming zone (14) and a catalyst regeneration zone (11) are positioned in the cavity.
2. The biomass continuous catalytic pyrolysis integrated device for catalyst regeneration according to claim 1, characterized in that the integrated device further comprises valves comprising a first valve (12), a second valve (13) and a third valve (15); a first pipeline is connected between the catalyst regeneration zone (11) and the catalytic reforming zone (14), and a first valve (12) and a second valve (13) are distributed on the first pipeline from top to bottom; a second pipeline is connected between the catalytic reforming zone (14) and the deactivated catalyst collecting zone (17), and third valves (15) are distributed on the second pipeline, wherein the valves are heat-insulating valves.
3. The biomass continuous catalytic pyrolysis integrated device for catalyst regeneration according to claim 1, further comprising a temperature controller, wherein the temperature controller comprises a first temperature controller (5), a second temperature controller (7) and a third temperature controller (16), and the first temperature controller (5) is arranged on the side wall of a vertical quartz tube (4) of the pyrolysis zone and is used for monitoring the temperature of the pyrolysis zone; the second temperature controller (7) is arranged on the side wall of the vertical quartz tube (4) of the tar removal zone and is used for monitoring the temperature of the tar removal zone; the third temperature controller (16) is arranged on the catalytic reforming zone (14) and is used for monitoring the temperature of the catalytic reforming zone (14).
4. The biomass continuous catalytic pyrolysis integrated device for catalyst regeneration according to claim 1, characterized in that it further comprises a flow meter comprising a first flow meter (2) and a second flow meter (3), the gas device (1) and the vertical quartz tube (4) being connected by parallel pipes comprising an upper pipe and a lower pipe; one end of the upper pipeline is connected with the gas device (1), and the other end is connected with the side wall of the vertical quartz tube (4) of the feeding area; one end of the lower pipeline is connected with the gas device (1), and the other end is connected with the side wall of the vertical quartz tube (4) of the discharging area; the first flowmeter (2) is arranged on the upper pipeline and is used for controlling the inert gas flow of the upper pipeline; the second flowmeter (3) is arranged on the lower pipeline and is used for controlling the gas flow of the lower pipeline; a quartz cotton interlayer is arranged at the joint of the vertical quartz tube (4) and the catalytic reforming zone (14) and at the joint of the catalytic reforming zone (14) and the condensation zone; the condensing zone comprises a condensing device (19) and a gas collecting device (20), one side of the condensing device (19) is connected with the catalytic reforming zone (14), the other side of the condensing device is connected with the gas collecting device (20), pyrolysis gas passing through the catalytic reforming zone (14) is catalytically cracked, then enters the condensing device (19), condensable gas in the pyrolysis gas is condensed into liquid, and non-condensable gas enters the gas collecting device (20) to be collected.
5. The biomass continuous catalytic pyrolysis integrated device for catalyst regeneration according to claim 1, wherein a partition plate is arranged at the opening of the box-type electric heating furnace, the impeller (10) is arranged at the left side of the partition plate, and the deactivated catalyst enters the catalyst regeneration zone (11) from the right side of the partition plate.
6. A method for continuous catalytic pyrolysis of biomass using the catalyst regenerated biomass continuous catalytic pyrolysis integrated apparatus of any one of claims 1 to 5, characterized by comprising the steps of:
1) Opening a gas device (1), and introducing inert gas into the integrated device to ensure the anaerobic environment of biomass;
2) Heating the catalyst regeneration zone (11) to 850-900 ℃, receiving corresponding radiant heat by a pyrolysis zone, a tar removal zone and a catalytic reforming zone (14) of the vertical quartz tube (4), wherein the temperature reached by the pyrolysis zone of the vertical quartz tube (4) is 500-550 ℃, the temperature reached by the tar removal zone of the vertical quartz tube (4) is 700-750 ℃, and the temperature reached by the catalytic reforming zone (14) is 450-500 ℃;
3) Biomass is pyrolyzed in a pyrolysis zone of a vertical quartz tube (4) to generate pyrolysis gas and biochar, the biochar forms a biochar bed layer, namely a tar removal zone, the pyrolysis gas flows downwards along with carrier gas through the tar removal zone to remove tar, pyrolysis gas flow after tar removal is pyrolyzed and catalyzed by a catalytic reforming zone (14), and pyrolysis gas after pyrolysis and catalysis enters a condensation zone to be collected;
4) After the catalyst in the catalytic reforming zone (14) is deactivated, the catalyst is collected in a deactivated catalyst collecting zone (17), then is sent into a catalyst regeneration zone (11) through a screw feeder (18), the deactivated catalyst is calcined for 3-5 hours under the condition of 850-900 ℃ in the catalyst regeneration zone (11), carbon deposition is burnt out, the regeneration of the deactivated catalyst is realized, and then the catalyst returns to the catalytic reforming zone (14).
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0085821A1 (en) * | 1982-02-10 | 1983-08-17 | Herwig Michel-Kim | Process for the economic and environmentally non harmful use of a biomass |
| CN101100621A (en) * | 2007-07-03 | 2008-01-09 | 山东省科学院能源研究所 | Method and device for preparing biomass hydrogen-rich combustion gas |
| CN104212468A (en) * | 2014-09-26 | 2014-12-17 | 李涵晖 | Household biomass pyrolysis carbon-gas combined combustion method and cooking range |
| FI20146000A (en) * | 2014-11-14 | 2016-05-15 | Teknologian Tutkimuskeskus Vtt Oy | Process and apparatus for gasification of raw material and gaseous product |
| CN205501130U (en) * | 2016-01-13 | 2016-08-24 | 博广热能股份有限公司 | A kiln body heat radiation protection system for rotation limekiln |
| CN107043088A (en) * | 2016-12-13 | 2017-08-15 | 神雾科技集团股份有限公司 | The system and method that hydrogen is prepared using rubbish |
| CN107828431A (en) * | 2017-11-06 | 2018-03-23 | 南昌大学 | A kind of method of the converting fuel oil of shell class discarded object microwave radiation technology |
| CN208075564U (en) * | 2018-04-02 | 2018-11-09 | 黄丽敏 | A kind of highly effective environment-friendly type biological matter melting and heat preservation all-in-one oven |
| CN108913177A (en) * | 2018-07-12 | 2018-11-30 | 中国科学院上海高等研究院 | A kind of method and device of the biomass pyrolytic tar low temperature removing based on microwave hot spot |
| CN210085371U (en) * | 2019-05-13 | 2020-02-18 | 华南理工大学 | Biomass continuous catalytic pyrolysis integrated device for catalyst regeneration |
-
2019
- 2019-05-13 CN CN201910392362.2A patent/CN110066670B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0085821A1 (en) * | 1982-02-10 | 1983-08-17 | Herwig Michel-Kim | Process for the economic and environmentally non harmful use of a biomass |
| CN101100621A (en) * | 2007-07-03 | 2008-01-09 | 山东省科学院能源研究所 | Method and device for preparing biomass hydrogen-rich combustion gas |
| CN104212468A (en) * | 2014-09-26 | 2014-12-17 | 李涵晖 | Household biomass pyrolysis carbon-gas combined combustion method and cooking range |
| FI20146000A (en) * | 2014-11-14 | 2016-05-15 | Teknologian Tutkimuskeskus Vtt Oy | Process and apparatus for gasification of raw material and gaseous product |
| CN205501130U (en) * | 2016-01-13 | 2016-08-24 | 博广热能股份有限公司 | A kiln body heat radiation protection system for rotation limekiln |
| CN107043088A (en) * | 2016-12-13 | 2017-08-15 | 神雾科技集团股份有限公司 | The system and method that hydrogen is prepared using rubbish |
| CN107828431A (en) * | 2017-11-06 | 2018-03-23 | 南昌大学 | A kind of method of the converting fuel oil of shell class discarded object microwave radiation technology |
| CN208075564U (en) * | 2018-04-02 | 2018-11-09 | 黄丽敏 | A kind of highly effective environment-friendly type biological matter melting and heat preservation all-in-one oven |
| CN108913177A (en) * | 2018-07-12 | 2018-11-30 | 中国科学院上海高等研究院 | A kind of method and device of the biomass pyrolytic tar low temperature removing based on microwave hot spot |
| CN210085371U (en) * | 2019-05-13 | 2020-02-18 | 华南理工大学 | Biomass continuous catalytic pyrolysis integrated device for catalyst regeneration |
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