CN106196027B - A kind of multi-cell fluidized bed device of solid fuel chemistry chain conversion - Google Patents
A kind of multi-cell fluidized bed device of solid fuel chemistry chain conversion Download PDFInfo
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- CN106196027B CN106196027B CN201610566651.6A CN201610566651A CN106196027B CN 106196027 B CN106196027 B CN 106196027B CN 201610566651 A CN201610566651 A CN 201610566651A CN 106196027 B CN106196027 B CN 106196027B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
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- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention belongs to chemical process equipment technical field, it is related to a kind of multi-cell fluidized bed device of solid fuel chemistry chain conversion, multicell fuel reactor is divided into I rooms using bumper plate, II rooms and III rooms, air reactor is separated by partition with the I rooms of multicell fuel reactor and is connected by material-returning device, the top of air reactor is connected with the first cyclone separator, the lower end of first cyclone separator and the second cyclone separator is connected by the first flow control apparatus and the second flow control apparatus with multicell fuel reactor respectively, the bottom of multicell fuel reactor is equipped with the pre- distributing chamber of first gas and the pre- distributing chamber of second gas, first gas distribution grid and second gas distribution grid are respectively equipped between multicell fuel reactor and the pre- distributing chamber of first gas and the pre- distributing chamber of second gas；The side of multicell fuel reactor is equipped with solids feeder；Its is simple in structure, easy to operate, and raw material is easy to get, and reaction is abundant, and cost is low, and heat utilization ratio is high.
Description
Technical field：
The invention belongs to chemical process equipment technical field, is related to a kind of for solid fuel chemistry chains such as coal, biomass
The multi-cell fluidized bed device of conversion.
Background technology：
Chemical chain technology (Chemical-Looping technology) utilizes for the clean and effective of the energy and provides one kind
New approaches, the technology need not consume additional energy and CO can be achieved2Interior separation；Can realize the cascade utilization of energy, make be
The overall thermal efficiency of system is improved；Heating power type and fuel type NO can also be controlled at the same timexGeneration.
The principle of chemical chain technology is exactly the change that will be given using solid carrier (predominantly transition metal oxide and CaO)
Learn reaction and be decomposed into oxidation/reduction reaction or absorption/desorption reaction enclosure, wherein solid carrier can carry out reacting it at two kinds
Between transmit oxygen/carbon dioxide and heat, by taking burning chemistry chains process as an example, oxygen carrier that the oxygen carrier of reduction-state carries out in atmosphere
The reduction reaction that the oxygen carrier of reaction and oxidation state carries out in gaseous fuel, oxygen carrier are followed in the case where aoxidizing and reducing two kinds of atmosphere
Ring alternately reacts, and realizes the transfer of oxygen and the burning of fuel.Since fuel does not contact directly with free oxygen in air, but
Reacted with the oxygen of compound state in oxygen carrier, to realize CO2Interior separation.
At present, chemical chain process research is mostly to the burning chemistry chains of the gaseous fuels such as natural gas and synthesis gas and reformed
The research of journey, in recent years both at home and abroad just the chemical chain process of the solid fuels such as coal, biomass and solid refuse was paid close attention to and
Research.Compared with aerochemistry chain process, greatest difficulty existing for the chemical chain process of solid fuel is in fuel reactor
The reaction rate of solid-solid reaction is too small, causes to react insufficient and CO2Capture rate reduce, increase oxygen carrier and solid combustion
The time of contact of material can be with the efficient hardening extent of reaction.
Solid fuel chemistry chain process mainly includes burning chemistry chains (chemical looping combustion), changes
Learn chain gasification (chemical looping gasification), calcium base chemical chain capture CO2(calcium chemical
Looping) process, the reaction that air reactor carries out are strong exothermal reaction, and the reaction that fuel reactor carries out is mostly to absorb heat instead
Should, rationally can improve process efficiency using the heat between each reaction, especially during chemical chain gasification, heat and
When transmit gasification reaction in fuel reactor carried out with decisive role, it is favourable to the whole utilization of whole process heat
In raising process efficiency.Existing apparatus uses single chamber mostly for fuel reactor, insufficient in order to solve solid fuel reaction
The problem of, it usually needs a carbon grabber is connected after combustion reactor, which adds the operation difficulty of reactor,
On the other hand, connected between fuel reactor and air reactor by flow control valve (looping seal), air reaction
The heat that device produces mainly is downloaded to fuel reactor by solid carrier, so that the transmission of heat and utilization ratio drop significantly
It is low.It is the endothermic reaction particularly with solid fuel gasification reaction, is unfavorable for the progress of gasification reaction.
The content of the invention
It is an object of the invention to overcome shortcoming existing in the prior art, seek design and a kind of solid fuel chemistry chain is provided
The multi-cell fluidized bed device of conversion, the structure-reinforced reaction of multicell, while strongly exothermic air reactor are made by fuel reactor
The integral structure that partition plate is separated by middle only is designed as with augmentation of heat transfer with the fuel reactor of heat absorption.
To achieve these goals, agent structure of the invention include the first flow control apparatus, the first cyclone separator,
Second flow control apparatus, the second cyclone separator, air reactor, multicell fuel reactor, feeding-in solid body device, the first gas
The pre- distributing chamber of body distribution grid, first gas, second gas distribution grid, the pre- distributing chamber of second gas, material-returning device and ash discharging hole；It is empty
The reative cell of solid/liquid/gas reactions device lower part and multicell fuel reactor forms L-type or matrix pattern structure, is adopted among multicell fuel reactor
The I rooms communicated, II rooms and III rooms are divided into first baffle and second baffle, first baffle top communicates, second baffle lower part phase
Logical, height of baffle plate is the 1/2~3/4 of multicell fuel reactor height；Air reactor and the I rooms of multicell fuel reactor pass through
Partition plate is kept apart, and air reactor is connected with the I rooms of multicell fuel reactor by material-returning device, and air reactor is higher by multicell
The cross section of fuel reactor part is the 1/3~2/3 of lower cross section diameter, highly 2~5 times for lower height；Air
The top of reactor is connected with the first cyclone separator, the lower end of the first cyclone separator by the first flow control apparatus with it is more
Room fuel reactor connection, the volume of the first cyclone separator are 1.5~4 times of the second cyclone separator；Second cyclonic separation
The lower end of device is connected by the second flow control apparatus with multicell fuel reactor；The bottom of multicell fuel reactor is equipped with side by side
The pre- distributing chamber of first gas and the pre- distributing chamber of second gas of structure, multicell fuel reactor and the pre- distributing chamber of first gas and the
First gas distribution grid and second gas distribution grid are respectively equipped between the pre- distributing chamber of two gases；The side of multicell fuel reactor
Equipped with solids feeder, solid carrier and coal are reacted by feeding-in solid body device into multicell fuel reactor.
Multicell fuel reactor of the present invention and air reactor lower part are square or L-shaped integral multicell fluidisation
Bed structure, air reactor are fast fluidized bed, and multicell fuel reactor is bubbling fluidized bed, air reactor and multicell fuel
Reactor realizes solid carrier circular regeneration in two reactors by cyclone separator and flow control apparatus respectively.
Fluidizing agent in air reactor of the present invention is air, and reaction temperature is 950 DEG C~1200 DEG C, and pressure is
Normal pressure；Fluidizing agent in multicell fuel reactor uses CO2And/or vapor, reaction temperature is at 800~1000 DEG C, pressure
For normal pressure or pressurization.
Material-returning device of the present invention is flow control apparatus, or by air reactor and multicell fuel reactor it
Between partition plate on perforate and plus baffle complete, in the center of partition plate position on the upper side, material-returning device is used to control solid position of opening
The internal circulating load of carrier and prevent gas anti-channeling between two reactors.
The multi-cell fluidized bed device of solid fuel chemistry chain of the present invention conversion by varying solid carrier type with
And the proportioning of solid carrier and solid fuel, complete burning chemistry chains, gasification or the hydrogen manufacturing of solid fuel, the solid carrier of use
Including Fe2O3、CuO、NiO、CaSO4And CaO, wherein CaO play capture CO2Effect, other be oxygen carrier effect.
First cyclone separator of the present invention is used to separate the gases such as oxygen denuded air and solid carrier, the second cyclonic separation
Device separating synthetic gas or CO2Deng the solid fuel ash content such as gas and coal ash.
The agent structure of the multi-cell fluidized bed device of solid fuel chemistry chain conversion of the present invention further includes the 3rd whirlwind
Separator, the 3rd cyclone separator are connected with the II rooms top of multicell fuel reactor, its height in the first cyclone separator and
Between second cyclone separator.
The present invention is in use, oxygen carrier and coal are entered the I rooms of multicell fuel reactor, vapor by feeding-in solid body device
And/or CO2Enter the pre- distributing chamber of first gas as fluidizing agent, then flowed material by first gas distribution grid
Change, with the fluidisation of material, the material II rooms and III rooms Jing Guo multicell fuel reactor successively, oxygen carrier and coal fully react
The gas generated afterwards condenses to obtain CO/H by the second cyclone separator2The CO of high-quality synthesis gas or high-purity2, the second rotation
The solid that wind separator lower part obtains is coal ash；Oxygen carrier becomes reduction after the indoor reaction completely of multicell fuel reactor three
The oxygen carrier of state, the oxygen carrier of reduction-state enter air reactor through material-returning device, and the oxygen carrier of reduction-state is in air reactor
In be oxidized to the oxygen carrier of oxidation state, the oxygen carrier of reduction-state regains oxygen, and the oxygen carrier of oxidation state is through the first whirlwind point
Enter first-class dynamic control device after being separated from device, be again introduced into multicell fuel reactor, oxygen carrier completes a redox
Circulation, the gas discharged by the first cyclone separator is oxygen deprivation N2, coal ash energy conduct that the second cyclone separator lower part obtains
Make heat carrier and enter multicell fuel reactor, or discharged by ash discharging hole.
Compared with prior art, the present invention one is to use multi-cell fluidized bed device, solid fuel and solid carrier are enhanced
Between reaction；Second, making Btu utilization more reasonable, the heat of air reactor reaction generation can directly be utilized for firing
Expect that reactor provides heat；Third, the arrangement in space is more simplified, make chemical chain process integrated；Its is simple in structure, operation side
Just, raw material is easy to get, and reaction is abundant, and cost is low, and heat utilization ratio is high.
Brief description of the drawings：
Fig. 1 is the agent structure principle schematic of the embodiment of the present invention 1.
Fig. 2 is the agent structure principle schematic of the embodiment of the present invention 2.
Fig. 3 is the agent structure principle schematic of the embodiment of the present invention 3.
Embodiment：
The invention will be further described by way of example and in conjunction with the accompanying drawings.
The agent structure of the present embodiment includes the first flow control apparatus 1, the flowing control of the first cyclone separator 2, second
Device 3, the second cyclone separator 4, air reactor 5, multicell fuel reactor 6, feeding-in solid body device 7, first gas distribution
The pre- distributing chamber 9 of plate 8, first gas, second gas distribution grid 10, the pre- distributing chamber 11 of second gas, material-returning device 12 and ash discharging hole
13；The reative cell of 5 lower part of air reactor and multicell fuel reactor 6 forms L-type or matrix pattern structure, multicell fuel reactor
The I rooms communicated, II rooms and III rooms are divided into using first baffle B and second baffle C among 6, first baffle B tops communicate, and second
Baffle C lower parts communicate, and height of baffle plate is the 1/2~3/4 of 6 height of multicell fuel reactor；Air reactor 5 and multicell fuel are anti-
The I rooms of device 6 are answered to keep apart by partition plate A, air reactor 5 and the I rooms of multicell fuel reactor 6 are connected by material-returning device 12
Logical, the cross section that air reactor 5 is higher by 6 part of multicell fuel reactor is the 1/3~2/3 of lower cross section diameter, height
For 2~5 times of lower height；The top of air reactor 5 is connected with the first cyclone separator 2, under the first cyclone separator 2
End is connected by the first flow control apparatus 1 with multicell fuel reactor 6, and the volume of the first cyclone separator 2 is the second whirlwind
1.5~4 times of separator 4；The lower end of second cyclone separator 4 passes through the second flow control apparatus 3 and multicell fuel reactor 6
Connection；The bottom of multicell fuel reactor 6 is equipped with the pre- distributing chamber 9 of first gas and the pre- distributing chamber of second gas of side by side configuration
11, it is respectively equipped with first gas between multicell fuel reactor 6 and the pre- distributing chamber 9 of first gas and the pre- distributing chamber 11 of second gas
Distribution grid 8 and second gas distribution grid 10；The side of multicell fuel reactor 6 is equipped with solids feeder 7, and solid carrier and coal lead to
Feeding-in solid body device 7 is crossed to be reacted into multicell fuel reactor 6.
Multicell fuel reactor 6 described in the present embodiment and 5 lower part of air reactor are square or L-shaped integral multicell
Fluidized-bed structure, air reactor 5 are fast fluidized bed, and multicell fuel reactor 6 is bubbling fluidized bed, 5 He of air reactor
Multicell fuel reactor 6 realizes that solid carrier circulates again in two reactors by cyclone separator and flow control apparatus respectively
It is raw.
Fluidizing agent described in the present embodiment in air reactor 5 is air, and reaction temperature is 950 DEG C~1200 DEG C, pressure
Power is normal pressure；6 fluidizing agent uses CO in multicell fuel reactor2And/or vapor, reaction temperature at 800~1000 DEG C,
Pressure is normal pressure or pressurization.
Material-returning device 12 described in the present embodiment is flow control apparatus, or by anti-in air reactor 5 and multicell fuel
Answer perforate on the partition plate A between device 6 and add baffle to complete, position of opening is used in the center of partition plate A position on the upper side, material-returning device 12
In control solid carrier internal circulating load and prevent gas anti-channeling between two reactors.
Described in the present embodiment solid fuel chemistry chain convert multi-cell fluidized bed device by varying solid carrier type
And the proportioning of solid carrier and solid fuel, burning chemistry chains, gasification or the hydrogen manufacturing of solid fuel are completed, the solid of use carries
Body includes Fe2O3、CuO、NiO、CaSO4And CaO, wherein CaO play capture CO2Effect, other be oxygen carrier effect.
First cyclone separator 2 described in the present embodiment is used to separate the gases such as oxygen denuded air and solid carrier, the second whirlwind
4 separating synthetic gas of separator or CO2Deng the solid fuel ash content such as gas and coal ash.
The agent structure for the multi-cell fluidized bed device that solid fuel chemistry chain described in the present embodiment converts further includes the 3rd rotation
Wind separator 14, the 3rd cyclone separator are connected with the II rooms top of multicell fuel reactor, its height is in the first cyclonic separation
Between device and the second cyclone separator.
In use, oxygen carrier and coal are entered the I rooms of multicell fuel reactor 6 by feeding-in solid body device 7, water steams the present embodiment
Gas and/or CO2Enter the pre- distributing chamber 9 of first gas as fluidizing agent, then carry out material by first gas distribution grid 8
Fluidisation, with the fluidisation of material, the material II rooms and III rooms Jing Guo multicell fuel reactor 6 successively, oxygen carrier and coal are fully anti-
The gas that should be generated afterwards obtains CO/H by the condensation of the second cyclone separator 42The CO of high-quality synthesis gas or high-purity2, second
The solid that 4 lower part of cyclone separator obtains is coal ash；Oxygen carrier becomes after the indoor reaction completely of multicell fuel reactor 6 three
The oxygen carrier of reduction-state, the oxygen carrier of reduction-state enter air reactor 5 through material-returning device 12, and the oxygen carrier of reduction-state is in air
The oxygen carrier of oxidation state is oxidized in reactor 5, the oxygen carrier of reduction-state regains oxygen, and the oxygen carrier of oxidation state is through first
Cyclone separator 2 enters first-class dynamic control device 1 after separating, and is again introduced into multicell fuel reactor 6, and oxygen carrier completes one
Redox cycle, the gas discharged by the first cyclone separator 2 is oxygen deprivation N2, 4 lower part of the second cyclone separator obtains
Coal ash can make heat carrier and enter multicell fuel reactor 6, or be discharged by ash discharging hole 13.
Embodiment 1：
Multicell fuel reactor 6 described in the present embodiment is sleeping mesh font side by side, and centre is separated by two baffles, multicell combustion
The I rooms and II rooms lower end for expecting reactor 6 communicate, and II rooms and III rooms upper end communicate, in use, being fired using vapor as multicell
Expect the fluidizing agent of reactor 6, material CaSO4Oxygen carrier and Shenmu Coal, CaSO4Amount of substance ratio with Shenmu County's carbon content in coal is 1:
2, by CaSO4Enter the I rooms of multicell fuel reactor 6 by feeding-in solid body device 7 with Shenmu Coal, efficiency of carbon con version is fired by existing single chamber
The 75% of material reactor brings up to more than 95%.
Embodiment 2：
Multicell fuel reactor 6 described in the present embodiment is by barrier partitions into three cell structures, three Room of multicell fuel reactor 6
It is distributed in matrix pattern with air reactor 5, is not communicated between air reactor 5 and the I rooms of multicell fuel reactor 6, multicell combustion
The I rooms and II rooms upper end for expecting reactor 6 communicate, and the II rooms and III rooms lower end of multicell fuel reactor 6 communicate, and multicell fuel is anti-
Device 6III rooms are answered to be connected with air reactor material-returning device 12, in use, using stream of the vapor as multicell fuel reactor 6
Change medium and carry out coal chemistry chain gasification reaction, material Fe2O3Oxygen carrier and Shenmu Coal, obtain from 4 top of the second cyclone separator
It is condensed after gas componant be：CO=28%, H2=52%, CO2=8%, efficiency of carbon con version is also by existing single chamber fuel reaction
The 85% of device brings up to more than 98%.
Embodiment 3：
The present embodiment increases by the 3rd cyclone separator 14 on the basis of embodiment 2, and air reactor 5 and multicell fuel are anti-
Answer and be not communicated between the I rooms of device 6, the I rooms and II rooms upper end of multicell fuel reactor 6 communicate, by returning charge between II rooms and III rooms
Device 12 is connected, and III rooms are equally connected with air reactor 24 by material-returning device 12, in use, by material Fe2O3Oxygen carrier,
CaO and Shenmu Coal are entered the I rooms of multicell fuel reactor 6 by solids feeder 7, and vapor does fluidizing agent and enters first gas
Pre- distributing chamber 9, is then fluidized material by the hundred millionth gas distribution grid 8, and with the fluidisation of material, material passes through II respectively
Room simultaneously carries out coal gasification and CaO captures CO into III rooms, oxygen carrier and Shenmu Coal by material-returning device in I rooms and II rooms2's
After reaction, the gas of generation obtains high-purity H by the condensation of the second cyclone separator 42, material completes CaCO in III rooms3Point
Solution, obtain high-purity carbon dioxide gas by the separation top of the 3rd cyclone separator 13, then material by material-returning device into
Enter the regeneration that air reactor 5 completes oxygen carrier, the oxygen carrier of oxidation state is first-class through being segregated into for the first cyclone separator 2
Dynamic control device 1, is again introduced into multicell fuel reactor 6, and oxygen carrier/carbon body completes a redox cycle and absorption De contamination
Circulation, the gas discharged by the first cyclone separator 2 is oxygen deprivation N2, the hot coal ash that 4 lower part of the second cyclone separator obtains can
To reenter multicell fuel reactor 6 as heat carrier, it can also be discharged by ash discharging hole d, since coal and oxygen carrier precursor reactant are
The endothermic reaction, CaCO3Decomposition reaction is the endothermic reaction, and reduction-state oxygen carrier oxidating is strong exothermal reaction, the integration of reactor
Design can rationally utilize the heat of each reaction.
The H that the present embodiment obtains2Purity is 95%, CO2Purity is 96%, and efficiency of carbon con version is also by existing single chamber fuel reaction
The 85% of device brings up to more than 95%.
Claims (7)
1. a kind of multi-cell fluidized bed device of solid fuel chemistry chain conversion, it is characterised in that agent structure includes the first flowing and controls
Device processed, the first cyclone separator, the second flow control apparatus, the second cyclone separator, air reactor, multicell fuel reaction
Device, feeding-in solid body device, first gas distribution grid, the pre- distributing chamber of first gas, second gas distribution grid, second gas are distributed in advance
Room, material-returning device and ash discharging hole；The reative cell of air reactor lower part and multicell fuel reactor forms L-type or matrix pattern knot
Structure, multicell fuel reactor centre are divided into the I rooms communicated, II rooms and III rooms, first baffle using first baffle and second baffle
Top communicates, and second baffle lower part communicates, and height of baffle plate is the 1/2~3/4 of multicell fuel reactor height；Air reactor with
The I rooms of multicell fuel reactor are kept apart by partition plate, and air reactor and the I rooms of multicell fuel reactor pass through material-returning device
Connection, the cross section that air reactor is higher by multicell fuel reactor part are the 1/3~2/3 of lower cross section diameter, height
For 2~5 times of lower height；The top of air reactor is connected with the first cyclone separator, the lower end of the first cyclone separator
Connected by the first flow control apparatus with multicell fuel reactor, the volume of the first cyclone separator is the second cyclone separator
1.5~4 times；The lower end of second cyclone separator is connected by the second flow control apparatus with multicell fuel reactor；Multicell
The bottom of fuel reactor is equipped with the pre- distributing chamber of first gas and the pre- distributing chamber of second gas of side by side configuration, multicell fuel reaction
First gas distribution grid and second gas point are respectively equipped between device and the pre- distributing chamber of first gas and the pre- distributing chamber of second gas
Fabric swatch；The side of multicell fuel reactor is equipped with solids feeder, solid carrier and coal and enters multicell by feeding-in solid body device
Fuel reactor is reacted；In use, oxygen carrier and coal are entered the I rooms of multicell fuel reactor, water by feeding-in solid body device
Steam and/or CO2 enter the pre- distributing chamber of first gas as fluidizing agent, then carry out material by first gas distribution grid
Fluidisation, with the fluidisation of material, the material II rooms and III rooms Jing Guo multicell fuel reactor successively, oxygen carrier and coal are fully anti-
The gas that should be generated afterwards condenses to obtain CO/H2 high-quality synthesis gas or the CO2 of high-purity by the second cyclone separator, and second
The solid that cyclone separator lower part obtains is coal ash；Oxygen carrier becomes also after the indoor reaction completely of multicell fuel reactor three
The oxygen carrier of ortho states, the oxygen carrier of reduction-state enter air reactor through material-returning device, and the oxygen carrier of reduction-state is in air reaction
The oxygen carrier of oxidation state is oxidized in device, the oxygen carrier of reduction-state regains oxygen, and the oxygen carrier of oxidation state is through the first whirlwind
Enter first-class dynamic control device after separator separation, be again introduced into multicell fuel reactor, oxygen carrier completes an oxidation also
Original circulation, the gas discharged by the first cyclone separator is oxygen deprivation N2, and the coal ash that the second cyclone separator lower part obtains can be made
Enter multicell fuel reactor to make heat carrier, or discharged by ash discharging hole.
2. the multi-cell fluidized bed device of solid fuel chemistry chain conversion according to claim 1, it is characterised in that the multicell
Fuel reactor and air reactor lower part are square or L-shaped integral multi-cell fluidized bed structure, and air reactor is fast
Fast fluid bed, multicell fuel reactor are bubbling fluidized bed, and air reactor and multicell fuel reactor pass through whirlwind point respectively
Solid carrier circular regeneration in two reactors is realized from device and flow control apparatus.
3. the multi-cell fluidized bed device of solid fuel chemistry chain conversion according to claim 1, it is characterised in that the air
Fluidizing agent in reactor is air, and reaction temperature is 950 DEG C~1200 DEG C, and pressure is normal pressure；In multicell fuel reactor
Fluidizing agent use CO2And/or vapor, for reaction temperature at 800~1000 DEG C, pressure is normal pressure or pressurization.
4. the multi-cell fluidized bed device of solid fuel chemistry chain conversion according to claim 1, it is characterised in that the returning charge
Device is flow control apparatus, or passes through perforate on the partition plate between air reactor and multicell fuel reactor and plus baffle
Complete, in the center of partition plate position on the upper side, material-returning device is used to control the internal circulating load of solid carrier and prevents that two is anti-position of opening
Answer gas anti-channeling between device.
5. the multi-cell fluidized bed device of solid fuel chemistry chain conversion according to claim 1, it is characterised in that the solid
The multi-cell fluidized bed device of chemistry of fuel chain conversion by varying solid carrier type and solid carrier and solid fuel
Proportioning, completes burning chemistry chains, gasification or the hydrogen manufacturing of solid fuel, the solid carrier of use includes Fe2O3、CuO、NiO、CaSO4
And CaO, wherein CaO play capture CO2Effect, other be oxygen carrier effect.
6. the multi-cell fluidized bed device of solid fuel chemistry chain conversion according to claim 1, it is characterised in that described first
Cyclone separator is used to separate oxygen denuded air and solid carrier, the second cyclone separator separating synthetic gas or CO2With coal ash.
7. the multi-cell fluidized bed device of solid fuel chemistry chain conversion according to claim 1, it is characterised in that the solid
The agent structure of the multi-cell fluidized bed device of chemistry of fuel chain conversion further includes the 3rd cyclone separator, the 3rd cyclone separator with
The II rooms top of multicell fuel reactor is connected, its height is between the first cyclone separator and the second cyclone separator.
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| CN110437882B (en) * | 2019-08-21 | 2020-09-29 | 青岛科技大学 | Low-rank coal and biomass graded utilization device and method based on chemical chain |
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