CN114540084B - Biomass gasification thermal carbon co-production system with independent oxidation chambers - Google Patents
Biomass gasification thermal carbon co-production system with independent oxidation chambers Download PDFInfo
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- CN114540084B CN114540084B CN202011329122.7A CN202011329122A CN114540084B CN 114540084 B CN114540084 B CN 114540084B CN 202011329122 A CN202011329122 A CN 202011329122A CN 114540084 B CN114540084 B CN 114540084B
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- 238000002309 gasification Methods 0.000 title claims abstract description 161
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 132
- 230000003647 oxidation Effects 0.000 title claims abstract description 131
- 239000002028 Biomass Substances 0.000 title claims abstract description 88
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 32
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 166
- 239000003546 flue gas Substances 0.000 claims abstract description 166
- 238000006243 chemical reaction Methods 0.000 claims abstract description 40
- 238000000034 method Methods 0.000 claims abstract description 39
- 230000008569 process Effects 0.000 claims abstract description 34
- 230000001105 regulatory effect Effects 0.000 claims abstract description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 17
- 239000001301 oxygen Substances 0.000 claims abstract description 17
- 238000002485 combustion reaction Methods 0.000 claims abstract description 16
- 238000001514 detection method Methods 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 50
- 238000009826 distribution Methods 0.000 claims description 39
- 239000000463 material Substances 0.000 claims description 36
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 20
- 230000001965 increasing effect Effects 0.000 claims description 19
- 230000001590 oxidative effect Effects 0.000 claims description 19
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 10
- 239000001569 carbon dioxide Substances 0.000 claims description 10
- 238000006722 reduction reaction Methods 0.000 claims description 10
- 238000005336 cracking Methods 0.000 claims description 9
- 238000000605 extraction Methods 0.000 claims description 8
- 239000002893 slag Substances 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 6
- 229910001294 Reinforcing steel Inorganic materials 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000012423 maintenance Methods 0.000 claims description 3
- 230000001276 controlling effect Effects 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 description 8
- 239000000779 smoke Substances 0.000 description 7
- 239000003610 charcoal Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 4
- 239000003575 carbonaceous material Substances 0.000 description 4
- 238000012544 monitoring process Methods 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 238000000889 atomisation Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 2
- 238000004200 deflagration Methods 0.000 description 2
- 238000005474 detonation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000033001 locomotion Effects 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 238000011946 reduction process Methods 0.000 description 2
- 238000007790 scraping Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000012840 feeding operation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 239000002918 waste heat 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
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23B—METHODS OR APPARATUS FOR COMBUSTION USING ONLY SOLID FUEL
- F23B90/00—Combustion methods not related to a particular type of apparatus
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a biomass gasification thermal carbon co-production system with independent oxidation chambers, which relates to the technical field of biomass comprehensive utilization equipment and comprises an oxidation furnace and a gasification furnace which are independently arranged, wherein the oxidation furnace is connected with the gasification furnace through a flue gas pipe, a flue gas pipe valve is arranged on the flue gas pipe, the flue gas pipe is also connected with one end of a flue gas circulating pipe, the other end of the flue gas circulating pipe is communicated with an oxidation chamber of the oxidation furnace, a flue gas circulating valve and a flue gas circulating fan are respectively arranged on the flue gas circulating pipe, and an oxygen detection device, a temperature sensor and a flowmeter are respectively arranged on a pipeline of the flue gas pipe between the flue gas pipe valve and the oxidation furnace. The oxidation furnace is independently arranged, the oxidation process (combustion) is independently controlled, the reaction intensity can be easily controlled, the biomass gasification production process can be conveniently and rapidly regulated and controlled in a wide range by controlling the reaction intensity of the oxidation furnace, and the high-quality gas-carbon co-production is realized.
Description
Technical Field
The invention belongs to the technical field of biomass comprehensive utilization equipment, and particularly relates to a biomass gasification thermal carbon co-production system provided with an independent oxidation furnace, wherein the biomass is subjected to pyrolysis gasification and then simultaneously produces combustible gas and biomass carbon.
Background
Biomass gasification, which can be divided into char production and non-char production from product residues, wherein the biomass gasification has low biomass utilization rate, and the biomass gasification has high biomass utilization rate; the movement form of biomass materials in the gasification process can be divided into a moving bed and a fixed bed, wherein the former has high gasification efficiency but the quality of produced carbon is the lowest, and the latter has low gasification efficiency but the quality of produced carbon is higher than the former.
When a biomass gasification system requiring carbon production is built, a fixed bed is a dominant technical scheme.
The fixed bed biomass gasification can be divided into updraft type and downdraft type according to the moving direction of gas production and biomass materials, and is characterized in that biomass moves from top to bottom in the gasification process, updraft type fixed bed gas is pumped and discharged from top to bottom, and downdraft type fixed bed gas is pumped and discharged from top to bottom.
From the reaction mechanism, the updraft type fixed bed biomass gasification is divided into preheating, cracking, reduction and oxidation processes from top to bottom, and the downdraft type fixed bed is divided into preheating, cracking, oxidation and reduction processes from top to bottom. The oxidation process is exothermic, other processes absorb heat, no heat released by the oxidation process is generated, other processes are difficult to finish, and the amount of heat provided by the oxidation process is a main factor for determining the gasification rate.
At present, the conventional technology adopted for co-production of the domestic hot carbon is that no matter which bed type is adopted, all four reaction processes are completed in one container, and the four reaction processes cannot be independently controlled, so that the regulation and control range is narrow and the regulation speed is low, and meanwhile, an oxidation product (ash) is doped in the product carbon, so that the carbon yield is low and the quality of the product carbon is poor.
Because of the limitation of the reaction mechanism, the downdraft type fixed bed has high heat value of the combustible gas, but only the biomass with finer granularity, better oxidability and better gasifying property can be adopted, and has the narrowest regulating range and slowest regulating speed; although the updraft type fixed bed is better in controllability than the downdraft type fixed bed, because moisture in the material layer does not participate in the reaction, the gas production heat value is lower than that of the downdraft type, and meanwhile, if the particles are large, the oxidability is poor, or the adjustment is out of the allowable range, the gasification process is possibly difficult to continuously produce.
Disclosure of Invention
The invention aims to solve the technical problems of low biomass gasification cracking efficiency, poor adjustability and poor quality of biomass charcoal in the prior art, and provides a biomass gasification charcoal co-production system with an independent oxidation furnace.
The technical scheme provided by the invention is as follows:
the utility model provides a living beings gasification thermal carbon coproduction system with independent oxidation furnace, its characterized in that, including oxidation furnace and the gasifier that independently set up, the oxidation furnace with the gasifier passes through the flue gas union coupling, be equipped with the flue gas pipe valve on the flue gas pipe, the flue gas pipe still is connected with the one end of flue gas circulating pipe, the other end of flue gas circulating pipe with the oxidation cavity intercommunication of oxidation furnace, be equipped with flue gas circulating valve and flue gas circulating fan on the flue gas circulating pipe respectively, the flue gas pipe be in the flue gas pipe valve with be equipped with oxygen detection device, temperature sensor and flowmeter on the pipeline between the oxidation furnace respectively.
Preferably, the gasification furnace is an updraft fixed bed gasification furnace. The updraft type fixed bed has good controllability and low requirements on granularity, oxidability and gasification of biomass.
Preferably, a first fire grate is arranged at the bottom of the gasification furnace, the gasification furnace is divided into an upper cavity and a lower cavity by the first fire grate, a gas distribution device is fixed in the upper cavity, a flue gas pipe penetrates through the furnace wall of the gasification furnace and is led into the gas distribution device, and a gas distribution plate is arranged at the outlet of the flue gas pipe. The gas distribution plate enables the first-stage gas distribution to be realized before the flue gas enters the gas distribution device, the flue gas reacts with biomass through the gas distribution device, the second-stage gas distribution is realized, the contact area between the flue gas and biomass in the gasification furnace is further increased, the utilization efficiency of the heat energy of the flue gas is improved, and the reaction speed is accelerated.
Preferably, the gas distribution device is in a multi-layer pagoda shape, each layer is provided with a plurality of gas distribution holes, the bottom of the gas distribution device is in a closed structure, and the gas distribution device is fixed on the inner wall of the gasification furnace through reinforcing steel bars. The gas distribution area of the gas distribution device with the increased pagoda shape is increased, namely the number of gas distribution holes is increased.
Preferably, a discharge hopper is arranged at the bottom of the first grate, the space between the first grate and the discharge hopper forms the lower cavity, a hollow water-cooled wall is arranged on the outer wall of the discharge hopper, and a water inlet and a water outlet are respectively arranged on the hollow water-cooled wall. The carbon materials entering the cold water discharging hopper in the hollow water cooling wall are cooled, so that scalding is prevented.
Preferably, the water outlet is connected with a water pipe inlet arranged on the outer wall of the oxidation furnace, the water pipe is provided with a first branch pipe and a second branch pipe, the first branch pipe is connected with a heat user, the second branch pipe is communicated with the flue gas pipe, and water pipe valves are respectively arranged on the first branch pipe and the second branch pipe. The water flowing out of the water outlet absorbs the heat transferred by the discharge hopper, the heat is further absorbed on the outer wall of the oxidation furnace, the generated hot water is used for heating users on one hand, and on the other hand, the generated hot water can be used for vaporizing the water in the flue gas pipe to generate water vapor to participate in the subsequent-stage reaction.
Preferably, the bottom of the discharging hopper is provided with a discharging valve, a screw conveyer is arranged below the discharging valve, the upper part of the gasification furnace is provided with a gasification feed hopper, a cover plate at the top of the gasification furnace is respectively provided with an ultrasonic material level gauge, a rotary electric scraper and an extraction air pipe, and an induced draft fan is arranged on the extraction air pipe. The gasified material enters a gasification furnace reaction cavity from a gasification material hopper, the surface of the gasified material is scraped by a rotary electric scraper, the material level height is detected by an ultrasonic material level meter, whether feeding is carried out or not is determined, after carbon generated by reaction enters a discharge hopper, a discharge valve is opened, and the carbon is discharged from a carbon outlet under the action of a screw conveyor; the charcoal gas generated by the reaction is pumped out from the air pumping pipe under the action of the induced draft fan.
Preferably, the oxidation furnace comprises an oxidation chamber, an oxidation material inlet and a flue gas outlet are formed in the side wall of the upper portion of the oxidation chamber, the flue gas outlet is connected with the flue gas pipe, a second fire grate is arranged below the interior of the oxidation chamber and connected with a slag discharging port, a wind inlet fan is arranged on the outer wall of the bottom of the oxidation chamber, and a pressure gauge is further arranged on the oxidation chamber. The oxidized material enters the oxidizing chamber of the oxidizing furnace from the oxidized material inlet, the air inlet machine is started to introduce air, the flue gas generated after the oxidized material is combusted is counted into the gasification furnace through the flue gas pipe, and residues generated by reaction combustion are discharged from the slag discharge port through the second grate.
The working method of the biomass gasification thermal carbon co-production system provided with the independent oxidation furnace comprises the following steps:
after the biomass is oxidized and combusted in an oxidizing furnace, a large amount of heat and carbon dioxide are generated in the form of flue gas, and the flue gas enters a gasification furnace through a flue gas pipe;
the heat and the carbon dioxide quantity entering the gasification furnace can be regulated by regulating the air inflow, the feeding quantity and the deslagging speed of the oxidation furnace and the readings on an oxygen detection device, a temperature sensor and a flowmeter on a flue gas pipe, so that the intensity and the reaction degree of the rear-stage gasification in the gasification furnace are regulated;
when the temperature of the flue gas does not reach the temperature of the post-stage reaction, the flue gas circulation valve and the flue gas circulation fan are started, so that part of the flue gas flows back to the oxidation furnace through the flue gas circulation pipe to be heated again and then is used for the post-stage reaction.
Preferably, the working method of the biomass gasification combined-heat-carbon production system provided with the independent oxidation furnace comprises the following steps:
a: when the gasification furnace is started, a small amount of air is introduced into the oxidation furnace, the lowest combustion state is maintained, the temperature of the flue gas is monitored by a temperature sensor to be lower than the cracking temperature of biomass in the gasification furnace, the flow of the flue gas is accumulated by a flowmeter, and the air introduction amount of the oxidation furnace is gradually increased until the flue gas replaces all air in the gasification furnace;
b: during normal operation, the air inflow of the oxidation furnace is maintained to be lower than the air inflow required by full combustion of fuel in the oxidation furnace, the oxygen detection device is used for monitoring that the flue gas does not contain or contains trace oxygen, and the air inflow of the oxidation furnace is regulated to adjust the temperature and flow of the flue gas, so that the heat of the flue gas meets the requirement of the subsequent biomass gasification process;
in the using process, when the combustion process reaches the maximum set value, the biomass gas of the later stage can not be satisfied
The amount of heat required for the chemical conversion is regulated by any one or more of the following modes:
biomass with higher heat value is used as oxidized fuel;
the air inflow of the oxidizing furnace is increased within the range of the air inflow permitted by the gasifying furnace, so that the biomass at the bottom in the gasifying furnace can be partially oxidized, namely, the oxidizing and exothermic processes also occur in the gasifying furnace, and the biomass combustible gas yield of the whole device is further improved;
the flue gas circulation pipe is started, so that part of flue gas is heated for subsequent reaction;
under the condition that the temperature of the flue gas exceeds a certain temperature, a certain amount of water can be sprayed into the flue gas, and after the water is gasified in a flue gas pipe, the water enters a gasification furnace to participate in reduction reaction in gasification, so that the heat value of the combustible gas is improved;
when the gasification furnace requires extremely low load, the opening of the smoke tube valve can be closed, the smoke circulating valve is opened, and the smoke circulating fan is started, so that the oxidation furnace is in a basic maintenance state, and when the gasification output needs to be increased, the gasification furnace does not need to be re-ignited, and only the smoke circulating fan, the smoke circulating valve and the large smoke tube valve need to be closed or closed.
By adopting the technical means, the following technical effects are achieved:
1. the oxidation furnaces are independently arranged, the oxidation process (combustion) is independently carried out and is independently controlled, the reaction intensity can be easily controlled, and the biomass gasification production process can be conveniently and quickly regulated and controlled in a wide range by controlling the reaction intensity of the oxidation furnaces, so that the high-quality gas-carbon co-production is realized;
2. ash produced in the oxidation process (combustion) is not doped in the produced carbon, so that the carbon production rate and the carbon production quality are far higher than those of a common fixed bed and are higher than those of a moving bed;
3. spraying a certain amount of water into high-temperature flue gas generated by the oxidation furnace before entering the gasification furnace, and carrying out high-temperature gasification in a flue gas pipeline and then carrying out gasification reduction reaction with subsequent biomass in the gasification furnace to obtain combustible gas with higher heat value;
4. according to the heat required by gasification of different biomass, the heat of the flue gas entering the gasification furnace can be adjusted by adjusting the variety of the biomass oxidation materials, the oxygen amount and flow of the flue gas pipe, spraying water into the flue gas and the like, so that the bed type biomass gasification furnace can gasify any biomass;
5. when the high-value biomass is used as the gasification raw material, biomass different from the gasification material in the oxidation furnace can be selected as biomass in the oxidation furnace, so that the cost is reduced, or higher flue gas heat is obtained, and the heat-carbon co-production capacity is improved;
6. in the starting stage, the combustible gas is mixed with fresh air, the temperature is uncontrollable, and the explosion safety accident is easy to occur; in the starting stage, the load of the oxidation furnace is gradually increased, the exhaust gas amount and the air temperature of the oxidation furnace mainly comprising carbon dioxide are gradually increased, the air stored in the oxidation furnace is gradually replaced and the temperature is gradually increased, when the concentration of combustible gas in the oxidation furnace reaches the deflagration range, no oxygen exists in the oxidation furnace, and deflagration accidents of the oxidation furnace can be avoided;
7. before the oxidation furnace reaches the gasification furnace gas distribution point, micro-positive pressure operation is adopted, even if the system is not tight, the carbon dioxide-based oxidation furnace exhaust gas leaks to the atmosphere, and the gasification furnace has no combustibility; the gasification furnace is started to run at the upper layer of gasification materials by adopting micro negative pressure, even if the system is not tight, no combustible gas leaks into the atmosphere, meanwhile, because the reduction reaction in the gasification furnace is an endothermic reaction, the generated combustible gas has lower temperature and can not reach the detonation point, even if a small amount of air leaks in, the detonation can not occur, and the safety of the whole system can be effectively ensured;
8. cooling water is used before carbon removal, the carbon removal temperature is reduced, waste heat is recycled, and meanwhile the possibility of personnel and equipment accidents caused by overhigh carbon removal temperature can be reduced;
9. compared with the existing gasification device, the emergency shutdown mechanism is especially arranged. When an emergency stop is needed, the feeding is stopped, and the oxidizing furnace is cut off to supply air and heat to the gasification furnace. As the gasification furnace reaction is a reduction endothermic reaction, no heat source exists, the reaction can be stopped quickly, the temperature is reduced quickly, and accidents can be prevented from occurring and expanding; and after the oxidation furnace does not output flue gas to the outside, the carbon dioxide can quickly inhibit the oxidation combustion process to stop the furnace. When the conventional scheme is used for emergency furnace stopping, because the entering air contains oxygen, even if the external air inlet is cut off, the reaction can be continued until the air entering the equipment is completely consumed, the furnace can be really stopped, the process is long, the temperature is high, and accidents or expansion accidents can occur.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
in the figure: 1. an oxidation furnace; 101. an oxidation chamber; 102. an oxidation material inlet; 103. a wind inlet machine; 104. a second grate; 105. a slag discharge port; 106. a flue gas outlet; 107. an observation port; 108. a water pipe; 108-1, a first branch pipe; 108-2, a second branch pipe; 108-3, a water pipe valve; 108-4, a water jacket; 108-5, an atomization device; 108-6, a pressure pump; 109. a flue gas circulation pipe; 110. a flue gas circulating fan; 111. a flue gas recirculation valve; 112. a pressure gauge; 2. a flue pipe; 3. an oxygen detecting device; 4. a temperature sensor; 5. a flow meter; 6. a gasification furnace; 7. a flue gas distribution device; 701. air holes are distributed; 702. an air distribution plate; 703. reinforcing steel bars; 8. a first grate; 801. a hole; 802. an electric gear; 9. discharging a hopper; 901. a hollow water-cooled wall; 901-1, a water inlet; 901-2, a water outlet; 902. a discharge valve; 10. a screw conveyor; 10-1, a carbon material outlet; 11. a gasification feed inlet; 12. an electric flashboard; 13. rotating the electric scraper; 14. an ultrasonic level gauge; 15. drawing out the air pipe; 16. an insert temperature sensor; 17. a smoke pipe valve; 18. a pressure gauge, 19, a draught fan; 20. and (3) a bracket.
Detailed Description
As shown in fig. 1, a biomass gasification thermal carbon co-production system with independent oxidation furnaces is characterized by comprising an oxidation furnace and a gasification furnace which are independently arranged, wherein the oxidation furnace is connected with the gasification furnace 6 through a flue gas pipe 2, a flue gas pipe valve 17 is arranged on the flue gas pipe 2, the flue gas pipe 2 is also connected with one end of a flue gas circulation pipe 109, the other end of the flue gas circulation pipe 109 is communicated with an oxidation chamber 101 of the oxidation furnace 1, a flue gas circulation valve 111 and a flue gas circulation fan 110 are respectively arranged on the flue gas circulation pipe 109, an oxygen detection device 3, a temperature sensor 4 and a flowmeter 5 are respectively arranged on a pipeline between the flue gas pipe valve 17 and the oxidation furnace 1, and the gasification furnace 6 is an updraft type fixed bed gasification furnace.
The gasification furnace is characterized in that a first fire grate 8 is arranged at the bottom of the gasification furnace 6, the gasification furnace is divided into an upper cavity and a lower cavity by the first fire grate 8, a gas distribution device 7 is fixed in the upper cavity, a flue gas pipe 2 penetrates through the wall of the gasification furnace 6 and is led into the gas distribution device 7, a gas distribution plate 702 is arranged at the outlet of the flue gas pipe 2, the gas distribution device 7 is fixed on the inner wall of the gasification furnace 6 through reinforcing steel bars 703, the gas distribution device 7 is in a multi-layer pagoda shape, a plurality of gas distribution holes 701 are formed in each layer, and the bottom of the gas distribution device 7 is of a closed structure. The flue gas pipe 2 passes through the wall of the gasification furnace 6 and is sealed by welding and the like.
The bottom of the gas distribution device 7 is provided with a steel plate, the flue gas pipe 2 penetrates through the steel plate to penetrate into the gas distribution device 7, and the flue gas pipe and the steel plate are arranged in a sealing mode with the steel plate through a flange or a welding mode.
The first fire grate 8 is a circumferential fire grate, a circle of holes 801 with the same thickness as the gasified material are arranged on the periphery of the first fire grate 8, and the first fire grate 8 rotates under the drive of the electric gear 802, so that the carbon material generated by the reaction is discharged.
The air distribution device 7 is arranged above the first fire grate 8 and does not shade the holes 801 of the first fire grate 8, and the bottom of the air distribution device 7 can be in contact with the top of the first fire grate 8 but is not fixed. The flue gas pipe 2 passes through the center of the first fire grate 8 before entering the gas distribution device 7, the flue gas pipe 2 and the first fire grate 8 are not fixed, and the first fire grate 8 can do circular motion relative to the flue gas pipe 2.
The bottom of the first fire grate 8 is provided with a discharge hopper 9, a space between the first fire grate 8 and the discharge hopper 9 forms the lower cavity, the outer wall of the discharge hopper 9 is provided with a hollow water-cooled wall 901, and the hollow water-cooled wall 901 is respectively provided with a water inlet 901-1 and a water outlet 901-2. The water outlet 901-2 is connected with an inlet of a water pipe 108 arranged on the outer wall of the oxidation furnace 1, the outlet of the water pipe 108 is provided with a first branch pipe 108-1 and a second branch pipe 108-2, the first branch pipe 108-1 is connected with a heat user, the second branch pipe 108-2 is communicated with the flue gas pipe 2, and the first branch pipe 108-1 and the second branch pipe 108-2 are respectively provided with a water pipe valve 108-3.
In order to increase the contact area of water and flue gas and increase the vaporization efficiency of water, the outer wall of the flue gas pipe 2 is provided with a water jacket 108-4, the inlet of the water jacket 108-4 is connected with the outlet of the second branch pipe 108-2, the outlet of the water jacket 108-4 is connected with the flue gas pipe 2, and a plurality of atomization devices 108-6 are further arranged at the outlet of the water jacket 108-4. The water jacket 108-4 is also provided with a pressure pump 108-6 for enhancing the atomization effect.
A discharge valve 902 is arranged at the bottom of the discharge hopper 9, a screw conveyor 10 is arranged below the discharge valve 902, a gasification material feed hopper 11 is arranged at the upper part of the gasification furnace 6, the gasification furnace top cover plate is respectively provided with an ultrasonic material level gauge 14, a rotary electric scraper 13 and an extraction air pipe 15, the extraction air pipe 15 is provided with an induced draft fan 19, and flammable gas is sucked and conveyed to a place to be utilized in a negative pressure suction mode. The ultrasonic level gauge 14 is used for measuring the level height in the gasifier 6, and the rotary electric scraper 13 is used for scraping the surface of the biomass gasification material in the gasifier 6.
A plurality of plug-in temperature sensors 16 are arranged on the side wall of the gasification furnace 6 up and down and are used for measuring the temperatures of different material level heights in the gasification furnace 6; the side wall of the gasification furnace 6 and the position above the material level are provided with pressure gauges 18 for measuring the pressure of combustible gas in the gasification furnace.
The oxidizing furnace 1 comprises an oxidizing chamber 101, an oxidizing material inlet 102 and a flue gas outlet 106 are formed in the side wall of the upper portion of the oxidizing chamber 101, the flue gas outlet 106 is connected with the flue gas pipe 2, a second fire grate 104 is arranged below the inner portion of the oxidizing chamber 101, the second fire grate 104 is connected with a slag discharging port 105, a blower 103 is arranged on the outer wall of the bottom of the oxidizing chamber 101, a pressure gauge 112 is further arranged on the oxidizing chamber 101 and used for monitoring the pressure of the oxidizing chamber 101, and a plurality of observation ports 107 are further formed in the oxidizing chamber 101 and used for observing the combustion condition of the oxidizing furnace 2.
The bottom of the gasification furnace 6 is provided with a bracket 20 for supporting and fixing.
Each biomass gasification process for producing biomass combustible gas and biomass charcoal comprises four processes of oxidation, reduction, gasification cracking and preheating drying, wherein only the oxidation process releases heat, and other processes absorb heat, but the oxidation process is a process for consuming biomass, and does not produce combustible gas, and does not produce biomass charcoal if the oxidation reaction is thorough. Without the heat generated by the oxidation process or external supplemental heat, several other processes would be difficult to occur or difficult to sustain. The temperature of the oxidation process can reach 1000-1200 ℃, and the main reaction formula is as follows:
c (Biomass) +O 2 (air) =co 2 +heat quantity
The reduction process is generally best at 700-900 ℃, and the main reaction formula is as follows:
c (Biomass) +CO 2 (pre-flue gas) +heat=2co (combustible gas component)
C (Biomass) +H 2 O (injection of pre-flue gas) +heat=co+h 2 (combustible gas component)
C (Biomass) +H 2 +heat=ch 4 (combustible gas component)
The biomass pyrolysis process generally occurs at 300-700 ℃, mainly comprises the high-temperature degradation of biomass organic matter components to generate combustible volatile matters, CH 4 、H 2 CO, firewood (CH) 1.4 O 0.6 ) And a small amount of carbon dioxide.
The preheating and drying process does not generate new materials, but is only a process of absorbing heat and volatilizing moisture in biomass.
The invention is a biomass oxidation process in an oxidation furnace, and the products are high-temperature hot air and ash slag which does not participate in the reaction; the reaction result in the gasification furnace is reduction, gasification cracking, preheating and drying from bottom to top.
With reference to fig. 1, the working principle of a biomass gasification thermal carbon co-production system with an independent oxidation furnace is briefly described:
after the biomass is oxidized and combusted in the oxidizing furnace 1, a large amount of heat and carbon dioxide are generated in the form of flue gas, the flue gas enters the gasification furnace 6 through the flue gas pipe 2 and is used for the subsequent reaction, and substances which cannot participate in the reaction of the biomass form slag to be discharged;
the heat and the carbon dioxide quantity entering the gasification furnace 6 can be regulated by regulating the air inflow, the feeding quantity and the deslagging speed of the oxidation furnace 1 and the readings on the oxygen detection device 3, the temperature sensor 4 and the flowmeter 5 on the flue gas pipe 2, so that the intensity and the reaction degree of the later-stage gasification in the gasification furnace 6 are regulated;
when the temperature of the flue gas does not reach the temperature of the post-stage reaction, the flue gas circulation valve 111 and the flue gas circulation fan 110 can be started, so that part of the flue gas flows back to the oxidation furnace 1 through the flue gas circulation pipe 109 to be heated again and then used for the post-stage reaction.
Specifically, the working method of the biomass gasification combined heat and carbon production system provided with the independent oxidation furnace comprises the following steps:
a: adding an oxidation material into the oxidation chamber 101 through an oxidation material feeding port, starting a small amount of air inlet in the oxidation furnace 1, maintaining the lowest combustion state, monitoring the flue gas to keep the temperature lower than the cracking temperature of the biomass in the gasification furnace 6 through a temperature sensor 4, accumulating the flow of the flue gas through a flowmeter 5 until the flue gas can replace air in the gasification furnace 6, and gradually increasing the air inlet of the oxidation furnace 1;
b: during normal operation, the air inflow of the oxidation furnace 1 is maintained to be lower than the air inflow required by full combustion of the fuel in the oxidation furnace 1, the oxygen detection device 3 is used for monitoring that the flue gas does not contain or contains trace oxygen, and the air inflow of the oxidation furnace 1 is regulated to adjust the temperature and flow of the flue gas so that the heat of the flue gas meets the requirement of the subsequent biomass gasification process;
c: when the combustion process reaches the maximum set value and the heat required by the gasification of the biomass at the later stage cannot be met, the combustion process is regulated by any one or more of the following modes:
a, biomass with higher heat value is used as oxidized fuel;
b, in the range of the allowable air inflow of the gasification furnace 6, the air inflow of the oxidation furnace 1 is increased, so that the biomass at the bottom in the gasification furnace 6 can be partially oxidized, namely, the gasification furnace 6 also has an oxidation heat release process, and the biomass combustible gas yield of the whole device is further improved;
c, opening the flue gas circulation pipe 109 so that part of the flue gas is recycled and heated and is used for the subsequent reaction again;
d, under the condition that the temperature of the flue gas exceeds a certain temperature, a certain amount of water can be sprayed into the flue gas, and after the water is gasified in the flue gas pipe 2, the water enters the gasification furnace 6 to participate in reduction reaction in gasification, so that the heat value of the combustible gas is improved;
d: when the gasification furnace 6 requires extremely low load, such as maintaining a hot standby state, the opening of the flue gas pipe valve 17 can be closed, and simultaneously the flue gas circulation valve 111 is opened and the flue gas circulation fan 110 is started, so that the oxidation furnace 1 is in a basic maintenance state, and when the gasification output needs to be increased, the gasification furnace is not required to be re-ignited, and only the flue gas circulation fan 110, the flue gas circulation valve 111 and the large flue gas pipe valve 17 need to be closed or closed;
e: opening an electric flashboard 12 of a gasification material feed inlet 11, enabling gasification material to enter the gasification furnace 6 through the gasification material feed inlet 11, enabling a level gauge 14 to measure the level height at any time, starting a rotary electric scraping plate 13 when the level height reaches a set value range until the level is stable and within an allowable range, closing the electric flashboard 12, introducing flue gas of the oxidation furnace 1, starting a draught fan 19 on a combustible gas extraction air pipe 15, and starting a gasification process; the flue gas of the oxidation furnace 1 fully permeates into the gasification material layer through two-stage gas distribution of the flue gas distribution device 7, reduction and cracking reactions occur, and generated combustible gas is sucked away from the suction air pipe 15 under the action of the induced draft fan 19;
f: the biomass gasification is finished from bottom to top, and whether the biomass at the bottom is sufficiently carbonized can be judged by observing the temperature changes of different heights and parts in the gasification furnace 6 through the inserted temperature sensor 16; when the carbonization is judged, the electric gear 802 is started to drive the first grate 8 to move, and the carbon material is discharged to the discharge hopper 9; the discharge valve 902 and the screw conveyor 10 are opened, and the char is discharged to the outside through the char outlet 10-1.
After discharging a certain amount of char, the gasification material level measured by the ultrasonic level gauge 14 is lowered, and when the value is lowered by a certain amount, the feeding operation is started.
And D-F are continuously or intermittently repeated, so that the continuous external production of combustible gas and the continuous or intermittent external production of biomass charcoal can be realized.
In the whole production process, the cold water intake is kept constant, and the excessive high temperature of carbon output can be prevented.
When the pressure in the oxidation furnace 1 is monitored to be too high by the oxidation furnace pressure gauge 112, the output power of the air inlet fan 103 is reduced, and the operation of the air inlet fan 103 is stopped when the output power exceeds the upper limit of the allowed set value.
When the pressure of the gasifier chamber is too low and other parameters are normal, the gasifier pressure gauge 18 can be regulated in a mode of reducing the output power of the induced draft fan 19, reducing the suction of combustible gas or increasing the output power of the air inlet fan 103 of the oxidation furnace; when the pressure of the gasifier is too high and other parameters are normal, the gasifier pressure gauge 18 can be regulated by increasing the output power of the induced draft fan 19, increasing the suction of combustible gas or reducing the output power of the air inlet machine 103 of the oxidation furnace.
The whole set of system adopts full-automatic control operation and is provided with a manual emergency shutdown function; meanwhile, when key parameters such as the pressure of the oxidation furnace and the pressure of the gasification furnace are too high, the pressure of the gasification furnace is too low, a protection value is set, the protection value exceeds the set value, and the adjustment ranges of the air inlet machine 103 and the induced draft fan 19 reach the boundary, the system automatically stops in an emergency.
When an emergency stop is needed, the feeding of the oxidation furnace 1 and the gasification furnace 6 is stopped, the flue pipe valve 17 is closed, the flue gas circulation valve 111 and the flue gas circulation fan 110 are opened, the oxidation furnace air inlet fan 103 is closed, the combustible gas extraction induced draft fan 19 is closed, the discharge valve 902 and the screw conveyor 10 are closed, and the cooling water is kept normally open.
Claims (7)
1. The biomass gasification thermal carbon co-production system with the independent oxidation chamber is characterized by comprising an oxidation furnace (1) and a gasification furnace (6) which are independently arranged, wherein the oxidation furnace (1) and the gasification furnace (6) are connected through a flue gas pipe (2), a flue gas pipe valve (17) is arranged on the flue gas pipe (2), the flue gas pipe (2) is also connected with one end of a flue gas circulation pipe (109), the other end of the flue gas circulation pipe (109) is communicated with an oxidation chamber (101) of the oxidation furnace (1), a flue gas circulation valve (111) and a flue gas circulation fan (110) are respectively arranged on the flue gas circulation pipe (109), and an oxygen detection device (3), a temperature sensor (4) and a flowmeter (5) are respectively arranged on a pipeline between the flue gas pipe valve (17) and the oxidation furnace (1); the gasification furnace (6) is provided with a first furnace row (8) at the bottom, the first furnace row (8) divides the gasification furnace into an upper cavity and a lower cavity, a gas distribution device (7) is fixed in the upper cavity, a flue gas pipe (2) passes through the furnace wall of the gasification furnace (6) and is led into the gas distribution device (7), a gas distribution plate (702) is arranged at the outlet of the flue gas pipe (2), the first furnace row (8) is a circumferential grate, a circle of holes (801) consistent with the thickness degree of gasification materials are arranged at the periphery of the first furnace row (8), the first furnace row (8) rotates under the drive of an electric gear (802), a discharge hopper (9) is arranged at the bottom of the first furnace row (8), a space between the first furnace row (8) and the discharge hopper (9) forms the lower cavity, a hollow water cooling wall (901) is arranged on the outer wall of the discharge hopper (9), a water inlet (901-1) and a water outlet (2) are respectively arranged at the hollow water cooling wall (901-1), the water outlet (901-2) is connected with a first branch pipe (108) and a second pipe (108-2) which are connected with the first furnace (108-2) through a second branch pipe (1-108), the first branch pipe (108-1) and the second branch pipe (108-2) are respectively provided with a water pipe valve (108-3).
2. The biomass gasification combined cycle system provided with an independent oxidation chamber according to claim 1, wherein the gasification furnace (6) is an updraft fixed bed gasification furnace.
3. The biomass gasification combined cycle system with the independent oxidation chamber according to claim 2, wherein the gas distribution device (7) is in a multi-layer pagoda shape, each layer is provided with a plurality of gas distribution holes (701), the bottom of the gas distribution device (7) is of a closed structure, and the gas distribution device (7) is fixed on the inner wall of the gasification furnace (6) through reinforcing steel bars (703).
4. The biomass gasification combined cycle system with the independent oxidation chamber according to claim 3, wherein a discharge valve (902) is arranged at the bottom of the discharge hopper (9), a screw conveyor (10) is arranged below the discharge valve (902), a gasification material feeding hopper (11) is arranged at the upper part of the gasification furnace (6), an ultrasonic material level gauge (14), a rotary electric scraper (13) and an extraction air pipe (15) are respectively arranged on a cover plate at the top of the gasification furnace, and an induced draft fan (19) is arranged on the extraction air pipe (15).
5. The biomass gasification combined cycle system with the independent oxidation chamber according to claim 4, wherein the oxidation furnace (1) comprises an oxidation chamber (101), an oxidation material inlet (102) and a flue gas outlet (106) are arranged on the side wall of the upper portion of the oxidation chamber (101), the flue gas outlet (106) is connected with the flue gas pipe (2), a second fire grate (104) is arranged below the inner portion of the oxidation chamber (101), the second fire grate (104) is connected with a slag discharge port (105), a blower (103) is arranged on the outer wall of the bottom of the oxidation chamber (101), and a pressure gauge (112) is further arranged on the oxidation chamber (101).
6. The method of operating a biomass gasification combined cycle system with independent oxidation chambers according to any one of claims 1 to 5, comprising the steps of:
after the biomass is oxidized and combusted in the oxidizing furnace (1), a large amount of heat and carbon dioxide are generated in the form of flue gas, and the flue gas enters the gasification furnace (6) through the flue gas pipe (2);
the heat and the carbon dioxide quantity entering the gasification furnace (6) can be regulated by regulating the air inflow, the feeding quantity and the deslagging speed of the oxidation furnace (1) and the readings on the oxygen detection device (3), the temperature sensor (4) and the flowmeter (5) on the flue gas pipe (2), so that the intensity and the reaction degree of the rear-stage gasification in the gasification furnace (6) are regulated;
when the temperature of the flue gas does not reach the temperature of the post-stage reaction, a flue gas circulation valve (111) and a flue gas circulation fan (110) are started, so that part of the flue gas flows back to the oxidation furnace (1) through the flue gas circulation pipe (109) to be heated again and then is used for the post-stage reaction.
7. The method for operating a biomass gasification combined cycle system with independent oxidation chambers according to claim 6, comprising the steps of:
a: when the device is started, a small amount of air is introduced into the oxidation furnace (1), the lowest combustion state is maintained, the temperature of the flue gas is monitored by the temperature sensor (4) to be lower than the cracking temperature of the biomass in the gasification furnace (6), the flue gas flow is accumulated by the flowmeter (5), and the air inflow of the oxidation furnace (1) is gradually increased until the flue gas replaces all air in the gasification furnace (6);
b: during normal operation, the air inflow of the oxidation furnace (1) is maintained to be lower than the air inflow required by full combustion of fuel in the oxidation furnace (1), the flue gas is monitored by an oxygen detection device (3) to contain no or trace oxygen, and the air inflow of the oxidation furnace (1) is regulated to adjust the temperature and flow of the flue gas so that the heat of the flue gas meets the requirement of a subsequent biomass gasification process;
in the use process, when the combustion process reaches the maximum set value and the heat required by the gasification of the biomass at the later stage cannot be met, the biomass is regulated by any one or more of the following modes:
(a) Biomass with higher heat value is used as oxidized fuel;
(b) The air inflow of the oxidizing furnace (1) is increased within the range of the air inflow permitted by the gasification furnace (6), so that the biomass at the bottom in the gasification furnace (6) can be partially oxidized, namely, the oxidation exothermic process also occurs in the gasification furnace (6), and the biomass combustible gas yield of the whole device is further improved;
(c) Opening a flue gas recirculation pipe (109) so that part of the flue gas recirculation is heated for the subsequent reaction;
(d) Under the condition that the temperature of the flue gas exceeds a certain temperature, a certain amount of water can be sprayed into the flue gas, and after the water is gasified in the flue gas pipe (2), the water enters the gasification furnace (6) to participate in reduction reaction in gasification, so that the heat value of the combustible gas is improved;
when the gasification furnace (6) requires extremely low load, the opening of the flue gas pipe valve (17) can be closed, the flue gas circulation valve (111) is opened, and the flue gas circulation fan (110) is started, so that the oxidation furnace (1) is in a basic maintenance state, and when gasification output needs to be increased, the gasification furnace does not need to be re-ignited, and only the flue gas circulation fan (110), the flue gas circulation valve (111) and the large flue gas pipe valve (17) need to be closed or closed.
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