CN105907430B - A kind of devices and methods therefor of gasification of biomass producing synthesis gas - Google Patents
A kind of devices and methods therefor of gasification of biomass producing synthesis gas Download PDFInfo
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- CN105907430B CN105907430B CN201610450149.9A CN201610450149A CN105907430B CN 105907430 B CN105907430 B CN 105907430B CN 201610450149 A CN201610450149 A CN 201610450149A CN 105907430 B CN105907430 B CN 105907430B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/023—Reducing the tar content
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Abstract
The invention discloses a kind of devices and methods therefors of gasification of biomass producing synthesis gas, and the device mainly includes pyrolysis reactor, gasification reactor, reforming reactor, regeneration reactor and heat pipes.Biomass is pre-processed through potassium salt soln first in technical process, and pretreated biomass is pyrolyzed in pyrolysis reactor, and coke gasifies in gasification reactor, and gasification reactor is with regeneration reactor by recycling bed material heat-carrying and absorbing CO2Hydrogen-rich gas is generated, and enters reforming reactor using hydrogen-rich gas and is carried out by hydrogenation catalyst cracking and is reformed for pyrolysis gas.From there through being pyrolyzed, gasified, reformed and combustive regeneration obtains low tar, high concentration H under mild reaction temperature step by step2With the synthesis gas of CO, and simultaneously by-product be rich in potassium agrochemical, realize biomass thermal chemical conversion process heat step transmit, not only increase efficiency of energy utilization, and increase economic value added.
Description
Technical field
The present invention relates to a kind of method of gasification of biomass and its apparatus systems, belong to biomass resource utilization field.
Background technology
Gasification of biomass is one of the important channel that biomass thermal chemical conversion utilizes, and the synthesis gas produced can not only be used for gas
Fluid fuel, also can be used as the intermediate product of the chemical products such as methanol, dimethyl ether, FT synthetic oils, and biomass gasification technology has weight
The actual application value wanted.The main problem of the approach of biomass thermal chemical conversion at present is that (1) is closed when utilizing air direct gasification
At in gas, there are a large amount of N2, cause flow rate low, poor quality；(2) there are tar in gasification product, not only influence gas product
Matter, and the normal operation of upstream device is influenced, when carrying out tar catalytic reforming, catalyst carbon deposition inactivation is easily led to, to make
The about application of biomass gasifying hydrogen making technology.
In order to avoid air direct gasification leads in synthesis gas that there are a large amount of N2So that GAS QUALITY declines, and grinds in recent years
The person of studying carefully improves the active ingredient and calorific value of synthesis gas by the way of indirect heating, wherein main technical method includes：(1)
The pyrolytic gasification of biomass and coke burning are separated using classification gasification method, made a living object by inertia or catalyst bed material
The pyrolysis and gasification of matter provide heat, and in order to reduce tar content, pyrolytic gasification product carries out further reformation purification.(2)
By classification gasification method, the hydrogen that gasification obtains high-purity is carried out using coke, pyrolysis gas carries out burning and provides heat, and avoids
The generation of tar.
In order to overcome, tar conversion is not exclusively in biomass gasification process and reforming catalyst carbon distribution inactivation, raising are biological
The gasification utilization rate and system effectiveness of matter carbon, the present invention propose a kind of new classification gasification device and method.
Invention content
Technical problem：According in the limitation of the prior art, the object of the present invention is to provide a kind of biomass graded gasifications to produce
The devices and methods therefor of synthesis gas, to solve, existing biomass gasified synthesis gas calorific value is low, tar content is high, conversion removing is difficult
The problem of, it proposes a kind of by realizing that no tar, high concentration H are produced in biomass thermal chemical conversion under mild reaction temperature2And CO
The biomass gasification device and its method of synthesis gas, and can chemical fertilizer by-product of the coproduction acquisition rich in potassium.
Technical solution：A kind of device of gasification of biomass producing synthesis gas of the present invention includes pyrolysis reactor, gasified reverse
Answer device, reforming reactor, regeneration reactor, the first heat-transfer pipe, the second heat-transfer pipe, the first gas-solid separator, the second gas solid separation
Device, coke batcher, discharge nozzle and connecting line；In first reactor, pyrolysis reactor is placed on gasification reactor
Portion is separated between pyrolysis reactor and gasification reactor by isolation board, is connected with discharge nozzle by coke batcher, the first heat transfer
The both ends of pipe are respectively placed in pyrolysis reactor and gasification reactor, and feed inlet is equipped on pyrolysis reactor, and first gas goes out
Mouthful；Gasification reactor is equipped with gasifying medium inlet, second gas outlet, the import of first circulation bed material and the outlet of cycle bed material；
In a second reactor, reforming reactor is placed in regeneration reactor top, reforming reactor and regeneration reactor
Between separated by isolation board, the both ends of the second heat-transfer pipe are respectively placed in reforming reactor and regeneration reactor, reforming reactor
It is equipped with gas feed, third gas outlet, the charge door and discharge port of catalyst；Regeneration reactor is equipped with material inlet,
The import of second circulation bed material and air intlet and flue gas/material outlet；The gas feed of reforming reactor is located at reforming reaction
The lower part of device；
The cycle bed material outlet of gasification reactor is connect with the second circulation bed material import of regeneration reactor；Gasification reactor
Gas vent connect the import of the first gas-solid separator, the first gas outlet of pyrolysis reactor is with the first gas-solid separator
Gaseous phase outlet connects the gas feed of reforming reactor；Flue gas/material outlet of regeneration reactor connects the second gas-solid separator
The solid outlet of import, the second gas-solid separator connects the first circulation bed material import of gasification reactor.
The discharge nozzle, discharge nozzle import and discharge nozzle outlet are respectively placed in pyrolysis reactor and gasification reactor.
Pyrolysis reactor and reforming reactor are fixed bed or moving-burden bed reactor, gasification reactor be bubbling fluidized bed or
Spouted fluidized bed, regeneration reactor is recirculating fluidized bed or transports bed.
It is filled with cycle bed material in gasification reactor and regeneration reactor, and recycles bed material in 2 reactors
Cycle；Reforming reactor is filled with reforming catalyst.
The outlet of discharge nozzle is extend into the filling bed material of gasification reactor.
A kind of gasification process substep of biomass gasification device of the present invention carries out biomass pyrolysis process, pyrolysis gas/coke
Oily reforming process and coke gasification process, this method comprises the following steps：
1) it after the biomass of natural drying being crushed to 1mm first hereinafter, impregnating biomass using potassium salt soln, bakes dry
It is dry to be less than 20% to moisture content, obtain preprocessing biomass；
2) preprocessing biomass is pyrolyzed by feed inlet into the pyrolysis reactor, and heat is generated after pyrolytic reaction
Gas and coke are solved, pyrolysis gas enters reforming reactor, solid by first gas gas feed of the outlet through reforming reactor
Material coke is controlled by coke batcher enters gasification reactor by discharge nozzle；
3) coke carries out gasification reaction in gasification reactor with the vapor for entering gasification reactor, generates gaseous product
H2, CO and CO2, and CO2It reacts with the MgO/CaO in cycle bed material, is cured as MgCO3/CaCO3；4) gasification reaction
The gaseous product of device enters the first gas-solid separator by second gas outlet, after the biomass lime-ash isolation of purified that gas is carried
Reforming reactor is entered by reforming reactor gas access by gaseous phase outlet, the biomass lime-ash isolated is exported by lime-ash and arranged
Go out device；
5) enter in the pyrolysis gas of reforming reactor that macromolecular tar is under the effect of catalyst bed material, and from gasified reverse
Answer the hydrogen-rich gas H of device2O、H2, CO and CO2Reforming reaction and hydrocracking are carried out, H is eventually converted into2、CO、CO2And CH4It is small
Molecular gas product；
6) biomass enters regeneration reactor by the material inlet and air intlet of regeneration reactor with air/oxygen and is fired
It burns, the cycle bed material MgCO in gasification reactor3/CaCO3Regeneration reactor calcining is returned to again by regeneration reactor bed material import
It is raw, MgCO therein3/CaCO3It is decomposed into MgO/CaO and CO2, the cycle bed material after calcining is after the second gas-solid separator by gas
Change Reactor inlet and enter back into gasification reactor, thus recycles bed material and recycle in two reactors, and by regeneration reactor
Heat brings gasification reactor into；
7) flue gas that regeneration reactor generates heats supply gasification reactor after the second gas-solid separator into heat exchanger
Water supply, it is cooling after discharger.
The preprocessing biomass includes agricultural wastes, forestry waste；Pre-processing the potassium salt soln used includes
KNO3、K2CO3, the wherein quality proportioning of sylvite and biomass is 8%~30%.
Cycle bed material in gasification reactor and regeneration reactor is MgCO3/CaCO3/MgO/CaO/Al2O3/SiO2It is mixed
Object is closed, grain size is 1mm~3mm；Catalyst feed in reforming reactor be Ni-Li, Ni-Mo, Ni-Mg, Co-Li, Co-Mo or
Co-Mg is the composite catalyst of active constituent.
First heat pipe is by heat transfer in gasification reactor to pyrolysis reactor；Second heat pipe is by regeneration reactor
Heat transfer to reforming reactor, the heat transfer medium in the first heat pipe and the second heat pipe is Na or K and its mixture.
The temperature of the pyrolysis reactor in 400~600 DEG C, the temperature of gasification reactor at 600~750 DEG C, regeneration
The temperature of reactor is at 800~900 DEG C；The temperature of reforming reactor is at 600~800 DEG C.
Advantageous effect：The present invention separates biomass pyrolysis process and coke gasification process, and vapor is replaced using coke
In hydrogen obtain hydrogen-rich gas, by the hydrogen-rich gas enter reforming reactor promote tar hydrocracking and catalytic reforming,
To efficiently convert the tar in pyrolysis gas, the synthesis gas of low tar is obtained；
The reforming catalyst of tar of the present invention is utilized in the case where adding hydrogen, is avoided the carbon distribution of catalyst, is improved catalyst
Service life.
The present invention pre-processes biomass using sylvite, K therein2O not only catalytic coke gas at a lower temperature
Change and obtain hydrogen-rich gas, and the lime-ash after reaction is rich in K2O can be used as farmland fertilizer, improve the attached of biomass trans-utilization
It is value added.
Description of the drawings
Fig. 1 is the technical process and system and device schematic diagram of the present invention.
Pyrolysis reactor 1, gasification reactor 2, reforming reactor 3, regeneration reactor 4, the first heat-transfer pipe 5, the second heat transfer
Pipe 6, the first gas-solid separator 7, the second gas-solid separator 8, coke batcher 9, discharge nozzle 10.
Specific implementation mode
A kind of devices and methods therefor of gasification of biomass of the present invention is described in detail below in conjunction with the accompanying drawings.
The method of the gasification of biomass producing synthesis gas of the present invention is the generation in order to avoid tar, promotes coke relatively low
At a temperature of realize Efficient Conversion, sylvite pretreatment has been carried out to biomass first, and classification carries out under mild reaction conditions
The reformation of biomass pyrolytic, coke gasification and tar, the hydrogen-rich gas obtained using coke gasification is carried out to tar plus hydrogen is split
Change and reform, to obtain high concentration H2With the synthesis gas of CO, promote tar conversion, improves coke gasification utilization rate.
The device of the gasification of biomass producing synthesis gas of the present invention, including pyrolysis reactor 1, gasification reactor 2 are reformed anti-
Answer device 3, regeneration reactor 4, the first heat-transfer pipe 5, the second heat-transfer pipe 6, the first gas-solid separator 7, the second gas-solid separator 8, coke
Charcoal batcher 9, discharge nozzle 10 and connecting line.In first reactor, pyrolysis reactor 1 is placed on gasification reactor 2
Portion is separated between pyrolysis reactor 1 and gasification reactor 2 by isolation board, is connected by coke batcher 9 and discharge nozzle 10；
In second reactor, reforming reactor 3 is placed in 4 top of regeneration reactor, between reforming reactor 3 and regeneration reactor 4 by
Isolation board separates；And first the both ends of heat-transfer pipe 5 be respectively placed in pyrolysis reactor 1 and gasification reactor 2；And second heat-transfer pipe 6
Both ends be respectively placed in reforming reactor 3 and regeneration reactor 4.Wherein, pyrolysis reactor includes feed inlet 1A, gas vent
1B；Gasification reactor 2 includes gasifying medium inlet 2A, gas vent 2C, and cycle bed material import 2B exports 2D with cycle bed material；
In second reactor, reforming reactor 3 includes gas feed 3A, gas vent 3C, the charge door 3B and discharge port of catalyst
3D；Regeneration reactor 4 includes material inlet 4A, recycles bed material import 4B and air intlet 4C and flue gas/material outlet 4D；
The gas feed 3A of reforming reactor 3 is located at the lower part of reforming reactor 3.
In addition, the outlet the discharge nozzle import 10A and discharge nozzle 10B of discharge nozzle 10 is respectively placed in pyrolysis reactor 1 and gasification
In reactor 2, and it is internal equipped with coke dispenser 9；
The cycle bed material outlet 2D of gasification reactor 2 is connect with the cycle bed material import 4B of regeneration reactor 4；Gasification reaction
The first gas of the import 7A of the first gas-solid separator of gas vent 2C connections 7 of device 2, pyrolysis reactor 1 export 1B and first
The gas feed 3A of the gaseous phase outlet 7B connections reforming reactor 3 of gas-solid separator 7；Flue gas/material outlet of regeneration reactor 4
4D meets the import 8A of the second gas-solid separator 8, and the solid outlet 8C of the second gas-solid separator 8 connects the first of gasification reactor 2 and follows
Ring bed material import 2B.
Preferred pyrolysis reactor 1 and reforming reactor 3 are fixed bed or moving-burden bed reactor, and gasification reactor 2 is drum
Fluid bed or spouted fluidized bed are steeped, regeneration reactor 4 is recirculating fluidized bed or transports bed；And gasification reactor 2 and regeneration are anti-
It answers and is filled with cycle bed material in device 4, and recycle bed material and recycled in 2 reactors；Preferred pyrolysis reactor 1 goes out
Expects pipe outlet 10B is extend into the filling bed material of gasification reactor 2；Preferred reforming reactor 3 is filled with reforming catalyst；
A kind of biomass gasification method provided by the invention, includes the following steps：
Step 1, first by the biomass of natural drying include agricultural wastes, forestry waste etc. be crushed to 1mm with
Under, utilize potassium salt soln such as KNO3、K2CO3Deng, it is 8%~30% dipping biomass according to the quality proportioning of sylvite and biomass,
Biomass baking after dipping is dried to moisture content and is less than 20%, obtains preprocessing biomass；
Step 2, pretreated biomass are pyrolyzed by feed inlet 1A into the pyrolysis reactor 1, anti-through being pyrolyzed
Should after generate pyrolysis gas and coke, pyrolysis gas enters reformation by gas feed 3A of the gas vent 1B through reforming reactor 3
Reactor 3, coke batcher 9 control residence time of the biomass in pyrolysis reactor, and then solid material coke is by going out
Expects pipe 10 enters gasification reactor 2；
Step 3, coke carry out gasification reaction with the vapor for entering gasification reactor 2 in the gasification reactor 2, and water steams
Gas and the mass ratio of biomass are：0.3~2, generate gaseous product H2, CO and CO2, and CO2With the MgO/ in cycle bed material
CaO reacts, and is cured as MgCO3/CaCO3；
The gaseous product of step 4, gasification reactor 2 enters the first gas-solid separator 7 by exporting 2C, and gas is carried
Reforming reactor 3 is entered by 3 gas access 3A of reforming reactor by gaseous phase outlet 7B after biomass lime-ash isolation of purified, is detached
The biomass lime-ash gone out exports 7C dischargers by lime-ash；
Step 5, into macromolecular tar in the pyrolysis gas of reforming reactor 3 catalyst bed material effect under, with from
The gas H of gasification reactor 42O、H2, CO and CO2Reforming reaction and hydrocracking are carried out, H is eventually converted into2、CO、CO2And CH4
Micro-molecular gas product；
Step 6, biomass enter regeneration instead with air/oxygen by the material inlet 4A and air intlet 4C of regeneration reactor 4
Device 4 is answered to burn, the cycle bed material MgCO in gasification reactor 23/CaCO3Regeneration is returned to by regeneration reactor bed material import 4B
Reactor calcination and regeneration, MgCO therein3/CaCO3It is decomposed into MgO/CaO and CO2, the cycle bed material after calcining is through the second gas-solid
Gasification reactor 2 is entered back by gasification reactor import 2B after separator 8, bed material is thus recycled and recycles in two reactors,
And bring the heat of regeneration reactor 4 into gasification reactor 2；
Step 7, the flue gas that regeneration reactor 4 generates heat supply gas after the second gas-solid separator 8, into heat exchanger
The water supply for changing reactor 2 generates vapor, discharger after flue gas cooling.
Wherein, the first heat pipe 5 by heat transfer in gasification reactor 2 to pyrolysis reactor 1；Second heat pipe 6 will regenerate anti-
Answer the heat transfer of device 4 to reforming reactor 3.Heat transfer medium in 5 and second heat pipe 6 of preferred first heat pipe be Na or K and
Its mixture；
The temperature of preferred pyrolysis reactor 1 in 400~600 DEG C, the temperature of gasification reactor 2 at 600~750 DEG C, then
The temperature of raw reactor 4 is at 800~900 DEG C, and the temperature of reforming reactor 3 is at 600~800 DEG C；
Cycle bed material in preferred gasification reactor 2 and regeneration reactor 4 is MgCO3/CaCO3/Al2O3/MgO/CaO/
SiO2Mixture, grain size be 1mm~3mm；
Catalyst feed in preferred reforming reactor 3 is Ni-Li, Ni-Mo, Ni-Mg, Co-Li, Co-Mo or Co-Mg
For the composite catalyst of active constituent；
Under the conditions of preferred, H that the synthesis gas main component of gaseous product is 50%~75%2, 10%~30% CO,
5%~25%CO2With minimal amount of CH4；Tar content is less than 500mg/Nm3；The K of biomass lime-ash2O content is more than 40%, can
As agrochemical byproduct.
Example 1：Wheat straw biomass
Agricultural wastes straw is raw material, and gasification process is as described above：Straw is crushed to 0.3-0.6mm or so, utilizes
100g K2CO3Solution 2000mL is configured, the broken straw 1h of 1000g are impregnated under room temperature, drier is then fed into and dries to containing
Below water 10%；Pretreated straw is sent into pyrolysis reactor, 600 DEG C of pyrolysis reaction temperature, and 700 DEG C of gasification temperature is reformed
750 DEG C of reaction temperature, 900 DEG C of combustion reaction temperature, gasification reactor are sent into vapor/straw mass ratio 0.5, and cycle bed material is
Al2O3And CaCO3/ CaO, the two proportioning 1:5, CaCO3/ CaO internal circulating loads and biomass quality proportioning 4:1, reforming catalyst is
15%Ni-3%Li/Al2O3；The synthesis gas obtained is reformed in gasification, by the gas componant H of cooling and purifying2：65.9%, CO：
19.5%, CO2：14.1%, CH4<0.25%, gas yield：1.02Nm3/ kg, tar<500mg/Nm3, lime-ash K2O content~
50%.
Example 2：Wheat straw biomass
Agricultural wastes straw is raw material, and gasification process is as described above：Straw is crushed to 0.3-0.6mm or so, utilizes
150g K2CO3Solution 3000mL is configured, the broken straw 1h of 1000g are impregnated under room temperature, drier is then fed into and dries to containing
Below water 10%；Pretreated straw is sent into pyrolysis reactor, 700 DEG C of reaction temperature, 750 DEG C of gasification temperature, reforming reaction
750 DEG C of temperature, 900 DEG C of combustion reaction temperature, gasification reactor are sent into vapor/straw mass ratio 0.4, and cycle bed material is Al2O3
And CaCO3/ CaO, the two proportioning 2:1, CaCO3/ CaO internal circulating loads and biomass quality proportioning 2:1, reforming catalyst 15%Ni-
10%Mg/Al2O3；The synthesis gas obtained is reformed in gasification, by the gas componant H of cooling and purifying2：60.2%, CO：24.2%,
CO2：15.2%, CH4<0.3%, gas yield：1.03Nm3/ kg, tar<400mg/Nm3, lime-ash K2O content~60%.
Claims (10)
1. a kind of device of gasification of biomass producing synthesis gas, it is characterised in that：The device includes pyrolysis reactor (1), gasification
Reactor (2), reforming reactor (3), regeneration reactor (4), the first heat-transfer pipe (5), the second heat-transfer pipe (6), the first gas-solid point
From device (7), the second gas-solid separator (8), coke batcher (9), discharge nozzle (10) and connecting line；In first reactor
In, pyrolysis reactor (1) is placed in gasification reactor (2) top, by being isolated between pyrolysis reactor (1) and gasification reactor (2)
Plate separates, and is connected by coke batcher (9) and discharge nozzle (10), the both ends of the first heat-transfer pipe (5) are respectively placed in pyrolytic reaction
In device (1) and gasification reactor (2), feed inlet (1A) is equipped on pyrolysis reactor (1), first gas exports (1B)；Gasification
Reactor (2) is equipped with gasifying medium inlet (2A), and second gas exports (2C), first circulation bed material import (2B) and circulation fluidized bed
Material outlet (2D)；
In a second reactor, reforming reactor (3) is placed in regeneration reactor (4) top, and reforming reactor (3) and regeneration are anti-
It answers and is separated by isolation board between device (4), the both ends of the second heat-transfer pipe (6) are respectively placed in reforming reactor (3) and regeneration reactor
(4) in, reforming reactor (3) is equipped with gas feed (3A), and third gas exports (3C), the charge door (3B) of catalyst and goes out
Material mouth (3D)；Regeneration reactor (4) is equipped with material inlet (4A), second circulation bed material import (4B) and air intlet
(4C) and flue gas/material outlet (4D)；The gas feed (3A) of reforming reactor (3) is located at the lower part of reforming reactor (3)；
The cycle bed material outlet (2D) of gasification reactor (2) is connect with the second circulation bed material import (4B) of regeneration reactor (4)；
The gas vent (2C) of gasification reactor (2) connects the import (7A) of the first gas-solid separator (7), and the of pyrolysis reactor (1)
One gas vent (1B) connect the gas feed of reforming reactor (3) with the gaseous phase outlet (7B) of the first gas-solid separator (7)
(3A)；Flue gas/material outlet (4D) of regeneration reactor (4) connects the import (8A) of the second gas-solid separator (8), the second gas-solid point
Solid outlet (8C) from device (8) connects the first circulation bed material import (2B) of gasification reactor (2).
2. the device of gasification of biomass producing synthesis gas according to claim 1, it is characterised in that：The discharge nozzle
(10), discharge nozzle import (10A) and discharge nozzle outlet (10B) are respectively placed in pyrolysis reactor (1) and gasification reactor (2).
3. the device of gasification of biomass producing synthesis gas according to claim 1, it is characterised in that：Pyrolysis reactor (1)
With reforming reactor (3) be fixed bed or moving-burden bed reactor, gasification reactor (2) be bubbling fluidized bed or spouted fluidized bed,
Regeneration reactor (4) is recirculating fluidized bed or transports bed.
4. the device of gasification of biomass producing synthesis gas according to claim 1, it is characterised in that：Gasification reactor (2)
Be filled with cycle bed material in regeneration reactor (4), and recycle bed material and recycled in 2 reactors；Reforming reactor
(3) it is filled with reforming catalyst.
5. the device of gasification of biomass producing synthesis gas according to claim 1 or 2, it is characterised in that：Discharge nozzle (10)
Outlet (10B) extend into the filling bed material of gasification reactor (2).
6. a kind of gasification process using the device of gasification of biomass producing synthesis gas described in claim 1, it is characterised in that：It should
Method substep carries out biomass pyrolysis process, pyrolysis gas/coke tar reforming process and coke gasification process, and this method includes following step
Suddenly：
1) after the biomass of natural drying being crushed to 1mm first hereinafter, impregnating biomass using potassium salt soln, baking is dried to
Moisture content is less than 20%, obtains preprocessing biomass；
2) preprocessing biomass is pyrolyzed by feed inlet (1A) into the pyrolysis reactor (1), is produced after pyrolytic reaction
Raw pyrolysis gas and coke, pyrolysis gas are entered by gas feed (3A) of the first gas outlet (1B) through reforming reactor (3)
Reforming reactor (3), solid material coke enter gasification reactor by coke batcher (9) control by discharge nozzle (10)
(2)；
3) coke carries out gasification reaction in gasification reactor (2) with the vapor for entering gasification reactor (2), generates gas production
Object H2, CO and CO2, and CO2It reacts with the MgO-CaO in cycle bed material, is cured as MgCO3-CaCO3；
4) gaseous product of gasification reactor (2) enters the first gas-solid separator (7) by second gas outlet (2C), and gas is taken
Reforming reaction is entered by reforming reactor gas feed (3A) by gaseous phase outlet (7B) after the biomass lime-ash isolation of purified of band
Device (3), the biomass lime-ash isolated export (7C) discharger by lime-ash；
5) enter in the pyrolysis gas of reforming reactor (3) that macromolecular tar is under the effect of catalyst bed material, and from gasified reverse
Answer the hydrogen-rich gas H of device2O、H2, CO and CO2Reforming reaction and hydrocracking are carried out, H is eventually converted into2、CO、CO2And CH4It is small
Molecular gas product；
6) biomass enters regenerative response with air-oxygen by the material inlet (4A) and air intlet (4C) of regeneration reactor (4)
Device (4) burns, the cycle bed material MgCO in gasification reactor (2)3-CaCO3By regeneration reactor second circulation bed material into
Mouth (4B) returns to regeneration reactor calcination and regeneration, MgCO therein3-CaCO3It is decomposed into MgO-CaO and CO2, the cycle after calcining
Bed material enters back into gasification reactor (2) after the second gas-solid separator (8) by first circulation bed material import (2B), thus circulation fluidized bed
Material recycles in two reactors, and brings the heat of regeneration reactor (4) into gasification reactor (2)；
7) flue gas that regeneration reactor (4) generates heats supply gasification reaction after the second gas-solid separator (8) into heat exchanger
The water supply of device (2), discharger after cooling.
7. gasification process according to claim 6, it is characterised in that：The preprocessing biomass includes agriculture waste
Object, forestry waste；It includes KNO to pre-process the potassium salt soln used3Or K2CO3, the quality proportioning of wherein sylvite and biomass is
8%~30%.
8. gasification process according to claim 6, which is characterized in that in gasification reactor (2) and regeneration reactor (4)
Cycle bed material is MgCO3-CaCO3-MgO-CaO-Al2O3-SiO2Mixture, grain size be 1mm~3mm；In reforming reactor (3)
Catalyst feed be composite catalyst that Ni-Li, Ni-Mo, Ni-Mg, Co-Li, Co-Mo or Co-Mg are active constituent.
9. gasification process according to claim 6, which is characterized in that first heat-transfer pipe (5) is by gasification reactor
(2) heat transfer gives pyrolysis reactor (1) in；Second heat-transfer pipe (6) is by the heat transfer of regeneration reactor (4) to reforming reaction
Device (3), the heat transfer medium in the first heat-transfer pipe and the second heat-transfer pipe are Na or K and its mixture.
10. gasification process according to claim 6, which is characterized in that the temperature of the pyrolysis reactor (1) is 400
~600 DEG C, the temperature of gasification reactor (2) at 600~750 DEG C, the temperature of regeneration reactor (4) is 800~900 DEG C；It reforms
600~800 DEG C of the temperature of reactor.
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