CN113862041A - Biomass gasification coupling coal-fired power generation system - Google Patents
Biomass gasification coupling coal-fired power generation system Download PDFInfo
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- CN113862041A CN113862041A CN202111358622.8A CN202111358622A CN113862041A CN 113862041 A CN113862041 A CN 113862041A CN 202111358622 A CN202111358622 A CN 202111358622A CN 113862041 A CN113862041 A CN 113862041A
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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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
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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
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D17/00—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces
- F25D17/02—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces for circulating liquids, e.g. brine
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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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- Oil, Petroleum & Natural Gas (AREA)
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Abstract
The invention provides a biomass gasification coupling coal-fired power generation system which comprises a biomass raw material module, a fly ash circulation module, a waste heat recovery module and a coal burner group module, wherein the biomass raw material module, the fly ash circulation module, the waste heat recovery module and the coal burner group module are sequentially connected through a pipeline, the fly ash circulation module adopts a fluidized bed gasification furnace, a primary fly ash circulation device and a secondary fly ash circulation device, and the biomass gasification coupling coal-fired power generation system has the beneficial effects that: the two-stage cyclone separator is arranged to send all the particles which are separated and not completely reacted back to the gasification furnace for continuous gasification, so that the dust content of the fuel gas is reduced, the gasification efficiency is effectively improved, and the clean and efficient utilization of the biomass is realized; the waste heat recovery device adopts a high-pressure water closed circulation loop, and the heat is recovered while the heat exchanger is prevented from being polluted and blocked due to tar condensation in the biomass gas.
Description
Technical Field
The invention relates to the technical field of biomass power generation, in particular to a biomass gasification coupling coal-fired power generation system.
Background
The biomass power generation is power generation by using biomass energy of biomass, is one of renewable energy power generation, and comprises direct combustion power generation of agricultural and forestry waste, gasification power generation of agricultural and forestry waste, waste incineration power generation, landfill gas power generation and methane power generation. World biomass power generation originated in the 70 th 20 th century, and when global oil crisis had broken out, danish began to actively develop clean renewable energy and vigorously pursue biomass power generation such as straw. Since 1990, biomass power generation has begun to grow vigorously in many countries in europe and america.
The biomass is used as renewable resource and has the characteristics of rich resource yield, wide regional distribution and stable energy storage. The biomass is mainly utilized by direct combustion, pyrolysis and other modes at home and abroad, but due to the characteristics of relatively low biomass energy density, high moisture, high volatile content, high alkali metal content and the like, the direct combustion is easy to slag and coke. The release of the volatile components in the biomass pyrolysis process is mainly in the form of tar, and can be used for oil product preparation through tar deep processing, but the biomass pyrolysis residue still has higher heat value and is insufficient in energy utilization.
The biomass and coal co-combustion power generation is adopted, but due to the characteristics of biomass slagging and coking, the working condition of local coking of a boiler occurs, the output and normal operation of a coal-fired unit are influenced, tar generated by biomass gasification is changed into liquid from gas at the temperature of lower than 300 ℃, the viscosity of the liquid tar is high, the tar is attached to a heating surface, the heat exchange surface is rapidly polluted and coked, and the normal operation of a gas cooler is influenced. Due to the limitation of the use temperature of the heat conduction oil, the temperature of the heating surface is difficult to control to be higher than 300 ℃ all the time, so that the built biomass gasification coupling coal-fired unit has the problems of serious contamination, coking and the like of a heat exchanger caused by tar condensation of a high-temperature gas cooler. In addition, the gasification temperature of the biomass fluidized bed is low, so that the carbon content of fly ash carried in fuel gas is high, and the gasification efficiency of the system is low.
Disclosure of Invention
In order to overcome the problems in the prior art, the invention provides a biomass gasification coupling coal-fired power generation system.
The invention discloses a biomass gasification coupling coal-fired power generation system, which comprises a biomass raw material module, a fly ash circulation module, a waste heat recovery module and a coal-fired unit module, wherein the biomass raw material module, the fly ash circulation module, the waste heat recovery module and the coal-fired unit module are sequentially connected through a pipeline, the fly ash circulation module adopts a fluidized bed gasification furnace, a first-stage fly ash circulation device and a second-stage fly ash circulation device, the fluidized bed gasification furnace is provided with a first material return port and a second material return port, the first-stage fly ash circulation device adopts a first-stage cyclone separator and a material return device, the second-stage fly ash circulation device adopts a second-stage cyclone separator, an ash cooling machine and a fly ash circulation device, a two-stage cyclone separator is arranged, the particles which are separated and not completely reacted are completely returned into the gasification furnace for continuous gasification, the dust content of fuel gas is reduced, and the gasification efficiency is effectively improved, the biomass is utilized cleanly and efficiently, the waste heat recovery module adopts the high-temperature gas cooler, the circulating device and the pressure stabilizing tank, the temperature of low-pressure feed water is kept at 270-320 ℃ all the time after the low-pressure feed water enters the circulating device through the circulating device and the pressure stabilizing tank, the problems of contamination and coking caused by separation of tar in the biomass gas on the heat exchange surface of the high-temperature gas cooler can be effectively prevented, and the stable and reliable operation of the high-temperature gas cooler is ensured.
On the basis, the biomass raw material module adopts a biomass raw material bin for storing biomass raw materials, an outlet below the biomass raw material bin is connected with an inlet above the feeder, an outlet below the feeder is connected with a feed inlet of the fluidized bed gasification furnace, and the biomass raw materials are sent into the fluidized bed gasification furnace for gasification.
On the basis, the top outlet of the fluidized bed gasification furnace is connected with the primary cyclone separator, the primary cyclone separator is connected with a material returning device, the material returning device is connected with the first material returning port, the particulate matters separated by the primary cyclone separator return to the fluidized bed gasification furnace in a high-temperature thermal state under the action of return air for re-gasification, as the fuel gas of the primary cyclone separator still contains a large amount of fly ash which contains a large amount of incompletely gasified carbon, the top outlet of the primary cyclone separator is connected with the secondary cyclone separator, the bottom outlet of the secondary cyclone separator is connected with an ash cooling machine, the ash cooling machine is connected with the second material returning port through a fly ash circulating device, the particulate matters separated by the secondary cyclone separator are cooled to 120-160 ℃ by the ash cooling machine and then return to the fluidized gasification furnace in a pneumatic conveying manner through a fly ash circulating device, the two-stage cyclone separator is arranged to separate the fly ash and return the fly ash to the fluidized bed gasification furnace for continuous gasification, on one hand, the whole carbon conversion rate can be improved, on the other hand, the dust content of fuel gas can be reduced, the risk of ash deposition of a subsequent fuel gas cooler is reduced, the generated ash enters the slag cooler from the outlet at the bottom of the fluidized bed gasification furnace, and the ash in the slag cooler is cooled by water.
On the basis, an outlet at the top of the secondary cyclone separator is connected with a gas inlet of the high-temperature gas cooler to cool gas, a gas outlet below the high-temperature gas cooler is connected with a coal-fired unit, and cooled gas is conveyed to the coal-fired unit to be combusted.
On the basis, the circulating device comprises a circulating pump and a heat transfer heat exchanger, the high-temperature gas cooler, the circulating pump and the heat transfer heat exchanger form closed circulation, and the temperature is maintained through the closed circulation, so that the problems of contamination and coking caused by separation of tar in the biomass gas on the heat exchange surface of the high-temperature gas cooler can be effectively prevented, and the stable and reliable operation of the high-temperature gas cooler is ensured.
On the basis, the pressure stabilizing tank is connected to a pipeline between the high-temperature gas cooler and the heat transfer heat exchanger, and the pressure of closed cycle is adjusted through the pressure stabilizing tank.
On this basis, set up the surge tank import on the surge tank, high-pressure gas gets into the pressure of adjusting the surge tank from the surge tank import, and the liquid level is adjusted to the moisturizing branch pipe, moisturizing branch pipe one end is passed through the moisturizing pump and is connected the surge tank, and the moisturizing house steward is connected to the other end, in order to maintain the high pressure water circulation volume in the closed circulation circuit, through moisturizing pump toward the moisturizing in the surge tank.
On the basis, the outlet below the fluidized bed gasification furnace is connected with a slag cooler, a water inlet of the slag cooler adopts low-pressure boiler to supply water, a water outlet of the slag cooler is connected with a water inlet of the ash cooler, a water outlet of the ash cooler is connected with a water replenishing header pipe, the water supply of the low-pressure boiler is adopted as a gas cooling cold source, and sensible heat of the gas is recovered while the gas is cooled so as to be indirectly used for power generation.
On the basis, the heat transfer heat exchanger adopts one of an evaporator or a water/water heat exchanger.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the biomass gasification coupling coal-fired power generation system, the two-stage cyclone separator is arranged, and the particles which are separated and not completely reacted are completely sent back to the gasification furnace for continuous gasification, so that the dust content of fuel gas is reduced, the gasification efficiency is effectively improved, and clean and efficient utilization of biomass is realized.
(2) According to the biomass gasification coupling coal-fired power generation system, low-pressure boiler feed water is used as a fuel gas cooling cold source, and sensible heat of the fuel gas is recovered while the fuel gas is cooled for indirect power generation; through the closed-loop circulation and pressure stabilization system, the temperature of low-pressure feed water is kept higher than 300 ℃ all the time after the low-pressure feed water enters the closed-loop circulation system, so that the problems of contamination and coking caused by separation of tar in the biomass gas on the heat exchange surface of the high-temperature gas cooler can be effectively prevented, and the stable and reliable operation of the high-temperature gas cooler is ensured; compared with the method adopting heat conduction oil as a cooling medium, the cooling medium adopted by the invention is more economical and safer, and the problems of heat conduction oil degradation, equipment corrosion and the like do not exist.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a second embodiment of the present invention.
In the figure: 1. biomass raw material, 2, biomass storage bin, 3, feeder, 4, fluidized bed gasifier, 5, primary cyclone separator, 6, secondary cyclone separator, 7, ash cooler, 8, fly ash circulating device, 9, slag cooler, 10, slag hopper, 11, slag cooler water inlet, 12, slag cooler water outlet, 13, ash cooler water inlet, 14, ash cooler water outlet, 16, fluidized fan, 17, material returning device, 19, gas cooler cold side water inlet, 20, gas cooler cold side water outlet, 21, heat transfer heat exchanger, 22, surge tank, 23, gas burner, 24, water wall, 25, gas flowmeter, 26, high temperature gas cooler, 27, coal-fired unit, 28, flue gas, 29, coal-fired boiler bottom slag, 31, surge tank inlet, 32, circulating pump, 33, water replenishing pump, 34, heat transfer heat exchanger cold side water inlet, 35, water replenishing header pipe, 36. the heat transfer heat exchanger comprises a cooling outlet 37, a water replenishing branch pipe 38, a gas booster fan 39, a first return port 40 and a second return port.
Detailed Description
The present invention will be described in further detail with reference to the following drawings and examples. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
The invention discloses a biomass gasification coupling coal-fired power generation system, which comprises a biomass raw material module, a fly ash circulation module, a waste heat recovery module and a coal burner group module, wherein the biomass raw material module, the fly ash circulation module, the waste heat recovery module and the coal burner group module are sequentially connected through pipelines, the fly ash circulation module adopts a fluidized bed gasification furnace 4, a primary fly ash circulation device and a secondary fly ash circulation device, two stages of cyclone separators are arranged, all particles which are separated and not completely reacted are sent back into the gasification furnace for continuous gasification, the dust content of fuel gas is reduced, the gasification efficiency is effectively improved, the clean and efficient utilization of biomass is realized, a first material return port 39 and a second material return port 40 are arranged on the fluidized bed gasification furnace 4, the primary fly ash circulation device adopts a primary cyclone separator 5 and a material return device 17, and the secondary fly ash circulation device adopts a secondary cyclone separator 6, The waste heat recovery module adopts a high-temperature gas cooler 26, a circulating device and a pressure stabilizing tank 22, and the circulating device and the pressure stabilizing tank 22 ensure that the temperature is always maintained at 270-320 ℃ after low-pressure feed water enters the circulating device, so that the problems of contamination and coking caused by separation of tar in biomass gas on the heat exchange surface of the high-temperature gas cooler can be effectively prevented, and the stable and reliable operation of the high-temperature gas cooler is ensured.
As a preferred embodiment of the present invention, in this embodiment, the top outlet of the fluidized bed gasification furnace 4 is connected to the primary cyclone separator 5, the primary cyclone separator 5 is connected to the material returning device 17, the material returning device 17 is connected to the first material returning port 39, the particulate matters separated by the primary cyclone separator 5 are returned to the fluidized bed gasification furnace 4 in a high-temperature thermal state by the material returning device 17 under the action of the return air for regasification, since the fuel gas of the primary cyclone separator 5 still contains a large amount of fly ash containing a large amount of incompletely gasified carbon, the top outlet of the primary cyclone separator 5 is connected to the secondary cyclone separator 6, the bottom outlet of the secondary cyclone separator 6 is connected to the ash cooling machine 7, the ash cooling machine 7 is connected to the second material returning port 40 by the fly ash circulating device 8, and the particles separated by the secondary cyclone separator 6 are cooled to 120-160 ℃ by the ash cooling machine 7 and then returned by the fly ash circulating device 8 in a pneumatic conveying manner The fluidized gasification furnace 4 is gasified again, the secondary cyclone separator 6 is arranged to separate the fly ash and return the fly ash to the fluidized bed gasification furnace 4 for continuous gasification, on one hand, the overall carbon conversion rate can be improved, on the other hand, the dust content of fuel gas can be reduced, the risk of ash deposition of a subsequent fuel gas cooler is reduced, the generated ash enters the slag cooler 9 from an outlet at the bottom of the fluidized bed gasification furnace 4, and the ash in the slag cooler 9 is cooled by water.
In the present embodiment, a biomass raw material bin 2 is used as the biomass raw material module for storing the biomass raw material 1, an outlet below the biomass raw material bin 2 is connected to an inlet above a feeder 3, an outlet below the feeder 3 is connected to a feed port of the fluidized bed gasification furnace 4, and the biomass raw material 1 is fed into the fluidized bed gasification furnace 4 for gasification.
In this embodiment, as a preferred embodiment of the present invention, the outlet at the top of the secondary cyclone separator 6 is connected to the gas inlet of the high-temperature gas cooler 26 to cool the high-temperature gas, and the gas outlet below the high-temperature gas cooler 26 is connected to the coal-fired unit to deliver the cooled gas to the coal-fired unit for combustion.
In the present embodiment, the circulating device includes a circulating pump 32 and a heat transfer heat exchanger 21, the high-temperature gas cooler 26, the circulating pump 32 and the heat transfer heat exchanger 21 form a closed cycle, and the temperature is maintained through the closed cycle, so that the problems of contamination and coking caused by the separation of tar in the biomass gas on the heat exchange surface of the high-temperature gas cooler 26 can be effectively prevented, and the stable and reliable operation of the high-temperature gas cooler 26 is ensured.
In the present embodiment, the surge tank 22 is connected to the pipe between the high-temperature gas cooler 26 and the heat transfer heat exchanger 21, and the pressure of the closed cycle is adjusted by the surge tank.
In the preferred embodiment of the present invention, the surge tank 22 is provided with a surge tank inlet 31, the high pressure water enters the regulated pressure through the surge tank inlet 31, the water supply branch pipe 37 regulates the liquid level, one end of the water supply branch pipe 37 is connected to the surge tank 22 through the water supply pump 33, the other end is connected to the water supply main pipe 35, and water is supplied into the surge tank 22 through the water supply pump 33 in order to maintain the circulation amount of the high pressure water in the closed circulation loop.
As a preferred embodiment of the present invention, in this embodiment, the outlet at the lower part of the fluidized bed gasification furnace 4 is connected to the slag cooler 9, the water inlet 11 of the slag cooler adopts low-pressure boiler water supply, the water outlet 12 of the slag cooler is connected to the water inlet 13 of the ash cooler, the water outlet 14 of the ash cooler is connected to the water supply header pipe 35, the low-pressure boiler water supply is adopted as a gas cooling cold source, and sensible heat of the gas is recovered while the gas is cooled for indirect power generation.
In the present embodiment, one of an evaporator and a water/water heat exchanger is used as the heat transfer heat exchanger 21.
Example 1
The biomass raw material 1 is stored in a biomass raw material bin 2, the biomass generally refers to granular biomass particles, the biomass storage bin 2 can store the biomass consumption of the bin gasification furnace for about 6-8 hours, a discharge port of the biomass raw material bin 2 is arranged below the biomass raw material bin 2 and enters a feed port of a feeder 3 through the discharge port of the biomass raw material bin 2, the discharge port of the feeder 3 is connected with a feed port below a fluidized bed gasification furnace 4, the biomass raw material 1 enters the fluidized bed gasification furnace 4, the fluidized bed gasification furnace 4 can be provided with a plurality of feed ports according to the scale of the gasification system, the plurality of feed ports disperse and feed the raw material into the gasification furnace, the uniformity of feeding is improved, the gasification reaction in the furnace is facilitated, meanwhile, the availability of the fluidized bed gasification furnace 4 is increased by the plurality of feed ports, one feed port is arranged in the embodiment, and 1 feeder 3 is correspondingly arranged at each feed port, in this embodiment, a variable frequency screw feeder is adopted, in order to improve the gasification effect, a gasification agent enters the fluidized bed gasification furnace 4 from the bottom through the fluidized fan 16, the gasification agent can be made of air or oxygen-enriched air or pure oxygen, in this embodiment, air is adopted, the biomass raw material 1 and the air fed by the fluidized fan 16 are gasified under the conditions of the gasification pressure of 0-30 kPag and the temperature of 740-760 ℃ to generate low-calorific-value fuel gas, the fuel gas is mixed with particles and enters the primary cyclone separator 5 from an outlet arranged above the fluidized bed gasification furnace 4, the fluidized bed gasification furnace 4 is provided with a first feed back port 39 and a second feed back port 40, the particles enter the feed back device 17 from an outlet below the primary cyclone separator 5 and enter the first feed back port 39 of the fluidized bed gasification furnace 4 through the feed back device 17, and the fuel gas of the primary cyclone separator 5 still contains a large amount of fly ash, the fly ash contains a large amount of incompletely gasified carbon, and the secondary cyclone separator 6 is arranged to separate the fly ash and return the fly ash to the gasification furnace for continuous gasification, so that on one hand, the overall carbon conversion rate can be improved, on the other hand, the dust content of fuel gas can be reduced, and the risk of dust deposition of a subsequent fuel gas cooler is relieved. An outlet above the primary cyclone separator 5 is connected with an inlet above the secondary cyclone separator 6, after secondary separation, particles enter the ash cooler 7 from an outlet below the secondary cyclone separator 6, and because the pressure difference between the primary fly ash and the hearth is small, the material returning device 17 can return the particles to the fluidized bed gasification furnace 4; the pressure difference between the secondary fly ash and the hearth is large, and the secondary fly ash cannot be sent in through a material returning device 17, so that the secondary fly ash needs to be sent back in a pneumatic conveying mode; the flying ash is required to be cooled by pneumatic conveying equipment, therefore, an ash cooler 7 is arranged, the outlet at the bottom of a secondary cyclone separator 6 enters the ash cooler 7, the outlet of the ash cooler 7 is connected with a flying ash circulating device 8, the flying ash circulating device 8 is connected with a second feed back port 40, ash enters an ash cooler 9 from the outlet at the bottom of a fluidized bed gasification furnace 4, the ash in the ash cooler 9 is cooled by water, the cooled ash enters a slag hopper 10, particulate matters separated by the primary cyclone separator 5 return to the fluidized bed gasification furnace 4 in a high-temperature thermal state under the action of feed back air 18 through a feed back device 17 for regasification, the particulate matters separated by the secondary cyclone separator 6 return to the fluidized bed gasification furnace 4 in a pneumatic conveying manner through the flying ash circulating device 8 after being cooled to 120-160 ℃ by the ash cooler 7, the fluidized bed 4, the primary cyclone separator 5, the secondary cyclone separator 6, The material returning device 17 and the pipelines connected between the material returning device and the material returning device are made of fireproof and anti-abrasion lining materials, so that the problems of abrasion and corrosion can be effectively avoided, and high-temperature fuel gas enters the high-temperature fuel gas cooler 26 from the outlet above the secondary cyclone separator 6 for cooling after particles are separated under the action of the primary cyclone separator 5 and the secondary cyclone separator 6.
The high-temperature gas cooler 26, the circulating pump 32 and the heat transfer heat exchanger 21 form a closed circulation loop, the surface temperature of the heat exchange tube behind the high-temperature gas cooler 26 is ensured to be higher than 300 ℃ through the closed circulation loop, the problems of contamination and coking caused by separation of tar in the biomass gas on the heat exchange surface of the high-temperature gas cooler 26 can be effectively prevented, and the stable and reliable operation of the high-temperature gas cooler 26 is ensured.
The closed circulation loop is used for reducing the temperature of the fuel gas, the circulation medium of the closed circulation loop is high-pressure water, the temperature range of the high-pressure water entering the high-temperature fuel gas cooler 26 is 260-320 ℃, usually 270-300 ℃, the high-pressure water enters the closed circulation loop, the high-pressure water absorbs the heat of the high-temperature fuel gas in the fuel gas cooler 26 so as to increase the temperature of the high-pressure water, the high-pressure water brings the heat of the high-temperature fuel gas to the heat transfer heat exchanger 21, the high-pressure water releases heat in the heat transfer heat exchanger 21 and transfers the heat to the low-pressure boiler feed water, and finally the heat is brought to a low-pressure boiler feed water system of the coal-fired unit by the low-pressure boiler feed water; the high-pressure water having a lowered temperature cools the high-temperature gas cooler 26 again by the circulation pump 32, and absorbs heat of the high-temperature gas. The temperature of the cooling medium rises after absorbing the heat of the fuel gas, and the temperature of the cooling medium must be reduced after rising because of the closed loop circulation, otherwise the temperature of the cooling medium can rise continuously to damage the equipment, so the heat transfer heat exchanger 21 is necessary. The cooling medium absorbing the heat of the fuel gas is cooled, and the heat is transferred to the cooling medium of the heat transfer heat exchanger 21.
In this embodiment, the heat transfer heat exchanger 21 is an evaporator, and the saturated steam from the heat transfer heat exchanger cooling outlet 36 may be depressurized and then sent to the return air as return air or sent to the coal-fired unit low-pressure steam pipe network. The steam is used as a gasifying agent, the quality of fuel gas can be adjusted, the self-produced steam is used as return air, the quality of the fuel gas of the gasification furnace can be improved, the system is simplified, a return air system does not need to be specially arranged, and the investment is saved; redundant steam is merged into the steam pipe network, promotes the low pressure steam heat supply ability of whole coal fired unit. When the coal-fired unit is a heat supply unit and steam is sold as a heat supply medium, the method has higher economy.
The pressure of the closed circulation loop is adjusted through a pressure stabilizing tank 22, the pressure stabilizing tank 22 is connected to a pipeline between the high-temperature gas cooler 26 and the heat transfer heat exchanger 21, and when the pressure is too high, partial gas in the pressure stabilizing tank 22 is discharged to reduce the system pressure; when the pressure is too low, a surge tank inlet 31 is arranged on the surge tank 22, high-pressure gas enters the pressure regulation part through the surge tank inlet 31, the high-pressure gas is high-pressure inert gas or high-pressure steam, in the embodiment, the high-pressure steam is adopted, the water replenishing branch pipe 37 is used for regulating the liquid level, in order to maintain the high-pressure water circulation quantity in the closed circulation loop, water is replenished into the surge tank through a water replenishing pump 35, one end of the water replenishing branch pipe 37 is connected with the surge tank 22 through a water replenishing pump 33, and the other end of the water replenishing branch pipe is connected with a water replenishing main pipe 35.
A small amount of water vapor is brought out when the pressure stabilizing tank 22 exhausts, in order to maintain the circulation amount of high-pressure water in a closed circulation loop, water is supplemented into the pressure stabilizing tank 22 through a water supplementing pump 33, the liquid level of the pressure stabilizing tank 22 is kept stable, the pressure is kept at 6-18 MPa, in the embodiment, the pressure is kept at 7-14 MPa, the high-pressure water enters the gas cooler 26 from a cold-side water inlet 19 of the gas cooler through a circulating pump 32, the high-pressure water flows out of a cold-side water outlet 20 of the gas cooler under the action of the circulating pump 32 and then enters the hot side of the heat transfer heat exchanger 21, and the water is fed into a cold side 34 of the heat transfer heat exchanger as low-pressure boiler water. The cold side 34 of the heat transfer heat exchanger enters the surge tank 22 through the water replenishing pump 33, the temperature of high-pressure water in the closed circulation loop is 270-300 ℃, the pressure is 7-14 MPa, and the pressure is far higher than the boiling point of the high-pressure water at the temperature, so that the vaporization of the high-pressure water in the closed circulation loop can be avoided. The gas cooler 26 is designed in a water pipe mode, namely, gas passes through a shell pass, high-pressure water passes through a pipe pass, the gas cooler 26 is integrally designed in a vertical mode, when high-pressure water at 270-300 ℃ passes through a heat exchange pipe of the gas cooler 26, the temperature of the outer surface of the heat exchange pipe is about 300-330 ℃, and condensation of gaseous tar of high-temperature gas which is in contact with the gas cooler and exchanges heat with the gas cooler due to too low temperature can be effectively avoided.
The lower outlet of the fluidized bed gasification furnace 4 is connected with a slag cooler 9, the water outlet 12 of the slag cooler is connected with a water inlet 13 of the slag cooler, the water outlet 14 of the slag cooler is connected with a water supply main pipe 35 of a waste heat recovery system, the water supply main pipe 35 is respectively connected with a cold side inlet water 34 of a heat transfer heat exchanger and an inlet of a water supply pump 33 through branch pipes, a cooling medium is taken from low-pressure boiler water supply of a low-pressure boiler water supply system of a coal-fired unit, the low-pressure boiler water supply generally refers to boiler water between an outlet of a condensate pump of the boiler water supply system and an inlet of a high-pressure boiler water supply pump, the low-pressure boiler water supply recovers heat of ash slag and is used as water supply of the waste heat recovery system, and the insufficient part is continuously supplemented through the main pipe, so that the temperature difference between the water supply temperature and the temperature of a closed circulation loop can be reduced, and equipment damage caused by overlarge temperature difference is avoided.
Through the process, the high-temperature gas at 700-800 ℃ is cooled to 350-450 ℃ by the cooler 26, the cooled gas enters the gas burner 23 through the outlet below the high-temperature gas cooler 26 through the gas booster fan 38 and the gas metering 25 and then enters the coal-fired unit 27 to be combusted together with coal, the water in the water-cooled wall 24 absorbs the heat of the coal and the biomass gas simultaneously and evaporates into water vapor to generate electricity, the generated bottom slag 29 of the coal-fired boiler is discharged from the slag discharge port at the bottom of the coal-fired unit 27, and the generated flue gas 28 is discharged from the tail of the boiler.
Example 2
Referring to fig. 2, in the present embodiment, the heat transfer heat exchanger 21 is a water/water heat exchanger, and the heated low-pressure boiler feed water is sent out from the cooling outlet 36 of the heat transfer heat exchanger and can be sent to a deaerator of the coal-fired unit. When the coal-fired unit is a generator set and abundant low-pressure steam in a plant area can be used by the coal-fired unit, the design of the water/water heat exchanger is simple and the investment is low.
In the description of the present invention, it is to be understood that the terms "coaxial", "bottom", "one end", "top", "middle", "other end", "upper", "one side", "top", "inner", "front", "center", "both ends", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention.
In the present invention, unless otherwise specifically stated or limited, the terms "mounted," "disposed," "connected," "fixed," "screwed," "padded," and the like are to be construed broadly, e.g., as being fixedly connected, detachably connected, or integrated; can be mechanically or electrically connected; the terms may be directly connected or indirectly connected through an intermediate, and may be communication between two elements or interaction relationship between two elements, unless otherwise specifically limited, and the specific meaning of the terms in the present invention will be understood by those skilled in the art according to specific situations.
While the foregoing description shows and describes the preferred embodiments of the present invention, it is to be understood that the invention is not limited to the forms disclosed herein, but is not to be construed as excluding other embodiments and is capable of use in various other combinations, modifications, and environments and is capable of changes within the scope of the inventive concept as described herein, commensurate with the above teachings, or the skill or knowledge of the relevant art. And that modifications and variations may be effected by those skilled in the art without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (9)
1. The utility model provides a biomass gasification coupling coal-fired power generation system, includes biomass raw materials module, flying dust circulation module, waste heat recovery module and coal burner group module, its characterized in that: the biomass raw material module, the fly ash circulation module, the waste heat recovery module and the coal burner unit module are sequentially connected through pipelines,
the fly ash circulating module adopts a fluidized bed gasification furnace (4), a first-stage fly ash circulating device and a second-stage fly ash circulating device, the fluidized bed gasification furnace (4) is provided with a first feed back port (39) and a second feed back port (40), the first-stage fly ash circulating device adopts a first-stage cyclone separator (5) and a feed back device (17), the second-stage fly ash circulating device adopts a second-stage cyclone separator (6), an ash cooling machine (7) and a fly ash circulating device (8),
the waste heat recovery module adopts a high-temperature fuel gas cooler (26), a circulating device and a pressure stabilizing tank (22).
2. The biomass gasification coupled coal-fired power generation system of claim 1, wherein: the top exit linkage of fluidized bed gasifier (4) one-level cyclone (5), feed back ware (17) is connected in one-level cyclone (5), feed back ware (17) are connected first feed back mouth (39), top exit linkage second grade cyclone (6) of one-level cyclone (5), export linkage cold ash machine (7) in second grade cyclone (6) bottom, cold ash machine (7) are connected through fly ash circulating device (8) second feed back mouth (40).
3. The biomass gasification coupled coal-fired power generation system of claim 1, wherein: the biomass raw material module adopts a biomass raw material bin (2) for storing biomass raw materials (1), an outlet below the biomass raw material bin (2) is connected with an inlet above the feeder (3), and an outlet below the feeder (3) is connected with a feed inlet of the fluidized bed gasification furnace (4).
4. The biomass gasification coupled coal-fired power generation system of claim 1, wherein: and an outlet at the top of the secondary cyclone separator (6) is connected with a fuel gas inlet of the high-temperature fuel gas cooler (26), and a fuel gas outlet below the high-temperature fuel gas cooler (26) is connected with a coal-fired unit.
5. The biomass gasification coupled coal-fired power generation system of claim 1, wherein: the circulating device comprises a circulating pump (32) and a heat transfer heat exchanger (21), and the high-temperature fuel gas cooler (26), the circulating pump (32) and the heat transfer heat exchanger (21) form closed circulation.
6. The biomass gasification coupled coal-fired power generation system of claim 1, wherein: the pressure stabilizing tank (22) is connected to a pipeline between the high-temperature gas cooler (26) and the heat transfer heat exchanger (21).
7. The biomass gasification coupled coal-fired power generation system of claim 6, wherein: set up surge tank import (31) on surge tank (22), high-pressure gas passes through surge tank import (31) department and gets into regulated pressure, and moisturizing branch pipe (37) adjust the liquid level, moisturizing branch pipe (37) one end is passed through moisturizing pump (33) and is connected surge tank (22), and moisturizing house steward (35) is connected to the other end.
8. The biomass gasification coupled coal-fired power generation system of claim 7, wherein: the lower outlet of the fluidized bed gasification furnace (4) is connected with a slag cooler (9), a water inlet (11) of the slag cooler adopts a low-pressure boiler to supply water, a water outlet (12) of the slag cooler is connected with a water inlet (13) of an ash cooler, and a water outlet (14) of the ash cooler is connected with the water replenishing main pipe (35).
9. The biomass gasification coupled coal-fired power generation system of claim 5, wherein: the heat transfer heat exchanger (21) adopts one of an evaporator or a water/water heat exchanger.
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| CN115342595A (en) * | 2022-08-16 | 2022-11-15 | 兰州工业学院 | Cooling device with cooling medium capable of being changed |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115342595A (en) * | 2022-08-16 | 2022-11-15 | 兰州工业学院 | Cooling device with cooling medium capable of being changed |
| CN115342595B (en) * | 2022-08-16 | 2023-03-21 | 兰州工业学院 | Cooling device with cooling medium capable of being changed |
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