CN112239682A - Gasification device slag water flash evaporation gas comprehensive utilization system and method - Google Patents
Gasification device slag water flash evaporation gas comprehensive utilization system and method Download PDFInfo
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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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- 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
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
- F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
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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
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B27/00—Machines, plants or systems, using particular sources of energy
- F25B27/02—Machines, plants or systems, using particular sources of energy using waste heat, e.g. from internal-combustion engines
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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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1612—CO2-separation and sequestration, i.e. long time storage
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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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
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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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
- Y02B30/625—Absorption based systems combined with heat or power generation [CHP], e.g. trigeneration
Abstract
The invention relates to a slag water flash vapor comprehensive utilization system and method for a gasification device. The system has wide application range, and is suitable for a gasification device for producing hydrogen or synthetic ammonia by taking coal, petroleum coke, residual oil, multi-component slurry and the like as raw materials, and an acid gas removal device provided with a circulating gas compressor; the low-level heat energy of the flash evaporation gas is fully utilized to produce the chilled water, so that the problem of overhigh temperature of the discharged grey water is solved; the effective components in the flash evaporation gas can be fully recovered, the hydrogen recovery rate is improved, and the economic benefit is remarkable; the method is based on the supercharging equipment of the existing process, the load and the size of newly-added equipment are greatly reduced, the initial investment is low, and the process flow is simple.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a system and a process for comprehensively utilizing flash evaporation gas generated after flash evaporation treatment of slag water in a device by taking coal, residual oil, multi-component slurry and the like as gasification raw materials.
Background
In a gasification raw material gasification device using coal, residual oil, multi-component slurry and the like, high-temperature crude synthesis gas produced by a gasification furnace is washed by chilled water and cooled, most of ash and fine particles are left in slag water, and the slag water is changed into grey water for recycling through secondary or tertiary flash evaporation and clarification treatment. The high-pressure flash evaporation (or primary flash evaporation) treatment of the slag water can resolve a large amount of acid gas dissolved in the slag water to form flash evaporation gas, and simultaneously the black water is concentrated. Because the flash gas contains a large amount of CO2、H2S and other acidic gases, so in the current treatment method, the most common method is to cool the flash evaporation gas by circulating water and then separate the flash evaporation gas, and recycle part of the flash evaporation gasAnd after the liquid is condensed, sending the acid gas with the residual concentration of 25-35% into a sulfur recovery device or carrying out torch combustion treatment on the acid gas.
The flow of flash gas is relatively large, and about 90 percent of the component is H2O and 1-4% of effective gas (CO + H)2) The balance of a small amount of acid gas (CO)2、H2S) and a trace of NH3、N2And the like; the temperature is usually 150 to 180 ℃ and the pressure is about 0.4 to 0.9 MPaG. Therefore, the flash evaporation gas has more low-level heat energy and effective gas with higher utilization value, and if the whole device can be combined and a reasonable process route is designed to comprehensively utilize the flash evaporation gas, a large amount of energy can be saved, the recovery rate of the effective gas can be improved, and the economic benefit is remarkable.
In order to avoid the corrosion to equipment and pipelines caused by overhigh content of ammonia nitrogen, chlorine radicals and the like in a water system, a gasification unit usually needs to continuously discharge grey water and supplement fresh water into the system. If the temperature of the discharged grey water is over 35 ℃ and is higher than that of the downstream short-cut nitrification and denitrification sewage treatment device, bacteria in the activated sludge are easy to die, and therefore, the sewage treatment capacity is reduced. The temperature of the grey water discharged outside is about 50 ℃, and particularly in southern areas, the grey water is difficult to cool to below 35 ℃ by using circulating water. Therefore, the temperature of the externally discharged grey water can be reduced as much as possible only by increasing the circulating water amount and the design margin of the externally discharged grey water heat exchanger, so as to ensure the safety of downstream devices.
In the low-temperature methanol washing process flow, the gas flashed from the hydrogen sulfide-rich methanol and the pre-washed methanol still contains a part of hydrogen (about 1-3%), methanol condensate is separated by a liquid separation tank at the inlet of a circulating gas compressor to obtain circulating gas (the content of hydrogen is about 40-60%), and the circulating gas is pressurized and circulated to the inlet of a low-temperature methanol washing unit by the circulating gas compressor, so that the recovery rate of hydrogen is improved.
The application number 201710363418.2 entitled "a coal gasification black water flash steam utilization process" discloses a coal gasification black water flash steam utilization process, which comprises the steps of directly feeding flash steam into a flash steam washing tower, washing the flash steam by using clean high-temperature transformation condensate, and stripping the high-temperature transformation condensate while washing the flash steam; recycling part of heat of the washed flash steam through the waste boiler byproduct steam, and recycling the residual heat through a waste heat exchanger; and finally, carrying out liquid separation on flash evaporation gas, pressurizing by a compressor, and sending the flash evaporation gas back to a process gas system to utilize effective components. The method mainly recovers the low-level heat energy by a method of by-producing steam, but the low-level heat energy is only transferred from flash gas to by-produced low-pressure steam, and the coal chemical industry device belongs to a device with excessive low-level heat energy, particularly a great amount of low-pressure steam (< 0.5MPaG) of the by-product of the conversion unit is utilized everywhere, so that the method does not effectively recover and utilize the low-level heat energy; in addition, the newly-added flash vapor compressor has larger power and more investment on equipment, operation and maintenance.
Disclosure of Invention
The first technical problem to be solved by the invention is to provide a comprehensive utilization system of slag water flash steam of a gasification device, which can recycle low-level heat energy and effective gas components in the flash steam and solve the problem of overhigh temperature of discharged grey water, aiming at the current situation of the prior art.
The second technical problem to be solved by the invention is to provide a comprehensive utilization method of slag water flash steam of a gasification device aiming at the current situation of the prior art, the method can recycle low-level heat energy and effective gas components in the flash steam and solve the problems that the temperature of discharged grey water is too high and the conventional method cannot cool.
The technical scheme adopted by the invention for solving the technical problems is as follows: the utility model provides a gasification equipment sediment water flash distillation gas comprehensive utilization system which characterized in that: comprises that
The lithium bromide absorption type refrigerating device takes the slag-containing water flash vapor from the gasification device as a heat source and is used for producing chilled water;
an input port of the externally discharged grey water cooler is connected with a chilled water supply end of the lithium bromide absorption type refrigerating device, an output port of the externally discharged grey water cooler is connected with a chilled water return end of the lithium bromide absorption type refrigerating device, and a pipeline for high-temperature externally discharged grey water penetrates through the externally discharged grey water cooler and is used for cooling the high-temperature externally discharged grey water;
the flash evaporation gas primary separator is arranged at the downstream of the lithium bromide absorption type refrigerating device, is provided with an input port for inputting slag-containing water flash evaporation gas output by the lithium bromide absorption type refrigerating device and is used for separating condensate in the slag-containing water flash evaporation gas; the top of the flash evaporation gas primary separator is provided with a gas output end, and the bottom of the flash evaporation gas primary separator is provided with a primary flash evaporation condensate output end;
the flash evaporation gas secondary separator is arranged at the downstream of the flash evaporation gas primary separator and is connected with a gas output end at the top of the flash evaporation gas primary separator through a first pipeline, the top of the flash evaporation gas secondary separator is provided with a gas output end, and the bottom of the flash evaporation gas secondary separator is provided with a secondary flash evaporation condensate output end;
the flash evaporation gas primary cooler is arranged on the first pipeline and used for cooling the gas phase entering the flash evaporation gas secondary separator;
the static mixer is arranged at the downstream of the flash evaporation gas secondary separator, is provided with an input port for inputting the flash evaporation gas and the circulating gas respectively, and is used for mixing the flash evaporation gas and the circulating gas; and
the acid gas removing device is internally provided with a liquid separating tank and a circulating gas compressor which are sequentially connected in series from upstream to downstream, the output end of the static mixer is connected with the input end of the liquid separating tank and used for gas-liquid separation, the bottom of the static mixer is provided with an output port for outputting process condensate, the top of the static mixer is connected with the input port of the circulating gas compressor, and the output port of the circulating gas compressor is connected with the inlet of a downstream conversion unit.
The slag water flash evaporation gas comprehensive utilization system of the gasification device further comprises:
the flash evaporation gas compressor is arranged at the downstream of the flash evaporation gas secondary separator, is connected with a gas output end at the top of the flash evaporation gas secondary separator and is used for cooling the gas phase output by the flash evaporation gas secondary separator; and
and the output end of the flash evaporation gas compressor is connected with the input end of the static mixer through a second pipeline, and the flash evaporation gas secondary cooler is arranged on the second pipeline and is used for cooling the gas phase output by the flash evaporation gas compressor.
The method for applying the slag water flash evaporation gas comprehensive utilization system of the gasification device is characterized in that:
the slag-containing water flash evaporation gas from the gasification device is firstly used as a heat source of a lithium bromide absorption type refrigerating device to produce chilled water, and the chilled water is used for cooling high-temperature discharged grey water to below 35 ℃ to obtain low-temperature discharged grey water so as to meet the requirement of a sewage treatment device on the temperature of the discharged grey water;
then entering a flash evaporation gas primary separator for gas-liquid separation, and discharging condensate;
the separated gas phase sequentially passes through a flash evaporation gas primary cooler and a flash evaporation gas secondary separator to further cool the flash evaporation gas and separate the condensate;
compressing the gas phase separated by the flash gas secondary separator to the same pressure as the circulating gas in the acid gas removal device, and fully mixing the gas phase and the circulating gas in a static mixer to absorb part of carbon dioxide in the flash gas;
the mixed gas enters a liquid separating tank at the inlet of a circulating gas compressor, a small amount of methanol condensate is separated out, the mixed gas is pressurized by the circulating gas compressor and then conveyed to the inlet of a conversion unit/in front of a conversion furnace, and effective components are recovered;
wherein, the condensate at the bottom of the flash evaporation gas primary separator and the flash evaporation gas secondary separator is sent to a downstream low-pressure system for recycling.
Preferably, when the flash vapor pressure at the outlet of the flash vapor compressor is not lower than the pressure of the circulating gas, the flash vapor compressor and the flash vapor secondary cooler are not arranged; when the pressure of flash gas at the outlet of the flash gas compressor is lower than the pressure of circulating gas, the gas phase separated by the flash gas secondary separator sequentially passes through the flash gas compressor and the flash gas secondary cooler to obtain low-temperature flash gas, and the low-temperature flash gas is conveyed to the static mixer. To reduce energy consumption.
Preferably, the slag-containing water flash evaporation gas is a gas obtained after slag water flash evaporation treatment of the gasification device, the pressure is 0-2.0 MPaG, and the temperature is 50-250 ℃.
Preferably, the temperature of the freezing water is 0-50 ℃, and the temperature of the low-temperature externally-discharged grey water is 0-50 ℃.
Preferably, in the flash gas primary cooler and the flash gas secondary cooler, the cooling medium is selected from process materials, circulating water in a public engineering medium, desalted water, chilled water and boiler feed water.
Preferably, the temperature of flash steam output by the lithium bromide absorption refrigeration device is 0-250 ℃.
Preferably, the volume content of dry hydrogen of the circulating gas is 0-50%, and the pressure is 0-2 MPaG.
Preferably, the operation pressure of the inlet liquid separation tank of the recycle gas compressor is 0.1-2.0 MPaG.
Compared with the prior art, the invention has the advantages that: the system has wide application range, and is suitable for a gasification device for producing hydrogen or synthetic ammonia by taking coal, petroleum coke, residual oil, multi-component slurry and the like as raw materials, and an acid gas removal device provided with a circulating gas compressor; the low-level heat energy of the flash evaporation gas is fully utilized to produce the chilled water, so that the problem of overhigh temperature of the discharged grey water is solved; the effective components in the flash evaporation gas can be fully recovered, the hydrogen recovery rate is improved, and the economic benefit is remarkable; the method relies on the supercharging equipment of the existing process, the process flow is simple, the load and the size of newly-added equipment are greatly reduced, and the initial investment is low.
Drawings
FIG. 1 is a process flow diagram of an embodiment of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1, the system for comprehensively utilizing slag water flash vapor in a gasification apparatus of the present embodiment includes:
the lithium bromide absorption type refrigerating device 7 takes the slag-containing water flash vapor 2 from the gasification device as a heat source and is used for producing chilled water;
an input port of the externally discharged grey water cooler 3 is connected with the end 4 of chilled water supply water of the lithium bromide absorption type refrigerating device 7, an output port of the externally discharged grey water cooler is connected with the end 5 of chilled water return water of the lithium bromide absorption type refrigerating device 7, and a pipeline for high-temperature externally discharged grey water 1 penetrates through the externally discharged grey water cooler for cooling the high-temperature externally discharged grey water 1;
the flash evaporation gas primary separator 8 is arranged at the downstream of the lithium bromide absorption type refrigerating device 7, is provided with an input port for inputting the slag-containing water flash evaporation gas 2 output by the lithium bromide absorption type refrigerating device 7 and is used for separating condensate in the slag-containing water flash evaporation gas 2; the top of the flash evaporation gas primary separator 8 is provided with a gas output end, and the bottom is provided with a primary flash evaporation condensate 19 output end;
the flash evaporation gas secondary separator 10 is arranged at the downstream of the flash evaporation gas primary separator 8 and is connected with a gas output end at the top of the flash evaporation gas primary separator 8 through a first pipeline, the top of the flash evaporation gas secondary separator 10 is provided with a gas output end, and the bottom of the flash evaporation gas secondary separator 10 is provided with a secondary flash evaporation condensate 20 output end;
the flash evaporation gas primary cooler 9 is arranged on the first pipeline and is used for cooling the gas phase entering the flash evaporation gas secondary separator 10;
the static mixer 15 is arranged at the downstream of the flash evaporation gas secondary separator 10, is provided with an input port for inputting flash evaporation gas and circulating gas 14 respectively, and is used for mixing the flash evaporation gas and the circulating gas 14;
the acid gas removal device 100 is internally provided with a liquid separating tank 16 and a circulating gas compressor 17 which are sequentially connected in series from upstream to downstream, the output end of a static mixer 15 is connected with the input end of the liquid separating tank 16 and used for gas-liquid separation, the bottom of the static mixer is provided with an output port for outputting process condensate 21, the top of the static mixer is connected with the input port of the circulating gas compressor 17, and the output port of the circulating gas compressor 17 is connected with the inlet of a downstream conversion unit;
the flash evaporation gas compressor 11 is arranged at the downstream of the flash evaporation gas secondary separator 10, is connected with a gas output end at the top of the flash evaporation gas secondary separator 10, and is used for cooling the gas phase output by the flash evaporation gas secondary separator 10; and
the output end of the flash evaporation gas compressor 11 is connected with the input end of the static mixer 15 through a second pipeline, and the flash evaporation gas secondary cooler 12 is arranged on the second pipeline and used for cooling the gas phase output by the flash evaporation gas compressor 11.
The comprehensive method for slag water flash evaporation gas of the gasification device comprises the following steps:
the slag-containing water flash evaporation gas 2 from the gasification device is firstly used as a heat source of a lithium bromide absorption type refrigerating device 7 to produce chilled water, and is used for cooling the high-temperature externally-discharged grey water 1 to below 35 ℃ to obtain low-temperature externally-discharged grey water 6 so as to meet the requirement of a sewage treatment device on the temperature of the externally-discharged grey water;
then enters a flash evaporation gas primary separator 2 for gas-liquid separation, and condensate is discharged;
the separated gas phase passes through a flash evaporation gas primary cooler 9 and a flash evaporation gas secondary separator 10 in sequence, and the flash evaporation gas is further cooled and subjected to condensate separation;
the gas phase separated by the flash gas secondary separator 10 is compressed to the same pressure as the circulating gas in the acid gas removal device, and enters the static mixer 15 together with the circulating gas for fully mixing so as to absorb part of carbon dioxide in the flash gas;
the mixed gas enters a liquid separating tank 16 at the inlet of a circulating gas compressor 17 to separate a small amount of methanol condensate, and the mixed gas is pressurized by the circulating gas compressor 17 and then conveyed to the inlet of a conversion unit/in front of a conversion furnace to recover effective components;
wherein, the condensate at the bottom of the flash evaporation gas primary separator 8 and the flash evaporation gas secondary separator 10 is sent to a downstream low-pressure system for recycling.
When the pressure of flash steam at the outlet of the flash steam compressor 17 is not lower than the pressure of circulating gas, the arrangement of the flash steam compressor 11 and the flash steam secondary cooler 12 is cancelled; when the pressure of the flash gas at the outlet of the flash gas compressor 11 is lower than the pressure of the circulating gas, the gas phase separated by the flash gas secondary separator 10 passes through the flash gas compressor 11 and the flash gas secondary cooler 12 in sequence to obtain low-temperature flash gas, and the low-temperature flash gas is conveyed to the static mixer 15 to reduce energy consumption.
Taking a certain 70 ten thousand Nm3/h hydrogen production device as an example, flash gas 2 from a high-pressure flash tank of a coal gasification device, the pressure of which is 0.8MPaG, the temperature of which is 176 ℃, the flow rate of which is 15t/h, and the content of effective gas of which is 4% (wet basis), enters a lithium bromide absorption type refrigerating device 7 to produce chilled water supply 4 at 10 ℃, and high-temperature discharged grey water 1 at 45 ℃ from a grey water storage tank and the chilled water supply 4 exchange heat through a discharged grey water cooler 3 to obtain low-temperature discharged grey water 6 at 25 ℃, and the low-temperature discharged grey water is sent to a downstream sewage treatment device. The slag-containing water flash steam 2 from the lithium bromide absorption type refrigerating device 7 passes throughAfter passing through a flash gas primary separator 8, a flash gas primary cooler 9 and a flash gas secondary separator 10, cooling to 45 ℃, entering a flash gas compressor 11, compressing to 1.5MPaG, and entering a flash gas secondary cooler 12 to obtain low-temperature flash gas 13 with the temperature of 45 ℃. The circulating gas 14 (desorbed from hydrogen sulfide-rich methanol) from the low-temperature methanol washing device and the low-temperature flash gas 13 are fully mixed in a static mixer 15, then enter a circulating gas compressor inlet liquid separation tank 16, a process condensate 21 containing methanol is separated, a gas-phase mixed gas 18 enters a circulating gas compressor 17 to be pressurized to 6.3MPaG, and enters a carbon monoxide conversion device conversion furnace inlet, so that CO in the mixed gas is subjected to conversion reaction to generate H2Thereby achieving the purpose of recovering effective components. The primary flash condensate 19 and the secondary flash condensate 20 are sent to a gasification unit ash water tank for recycling, the process condensate 21 is methanol condensate, and the methanol condensate can be sent to a methanol recovery tank with lower pressure of a low-temperature methanol washing device for further treatment. The process can recover about 8t/h of effective gas in flash gas 2.
Claims (10)
1. The utility model provides a gasification equipment sediment water flash distillation gas comprehensive utilization system which characterized in that: comprises that
A lithium bromide absorption refrigerating device (7) which takes the slag-containing water flash steam (2) from the gasification device as a heat source and is used for producing chilled water;
an input port of the external emission grey water cooler (3) is connected with the end of chilled water supply (4) of the lithium bromide absorption type refrigerating device (7), an output port of the external emission grey water cooler is connected with the end of chilled water return (5) of the lithium bromide absorption type refrigerating device (7), and a pipeline for high-temperature external emission grey water (1) penetrates through the external emission grey water cooler and is used for cooling the high-temperature external emission grey water (1);
the flash evaporation gas primary separator (8) is arranged at the downstream of the lithium bromide absorption type refrigerating device (7), is provided with an input port for inputting the slag-containing water flash evaporation gas (2) output by the lithium bromide absorption type refrigerating device (7) and is used for separating condensate in the slag-containing water flash evaporation gas (2); the top of the flash evaporation gas primary separator (8) is provided with a gas output end, and the bottom of the flash evaporation gas primary separator is provided with a primary flash evaporation condensate (19) output end;
the flash evaporation gas secondary separator (10) is arranged at the downstream of the flash evaporation gas primary separator (8) and is connected with a gas output end at the top of the flash evaporation gas primary separator (8) through a first pipeline, the top of the flash evaporation gas secondary separator (10) is provided with a gas output end, and the bottom of the flash evaporation gas secondary separator is provided with a secondary flash evaporation condensate (20) output end;
the flash evaporation gas primary cooler (9) is arranged on the first pipeline and is used for cooling the gas phase entering the flash evaporation gas secondary separator (10);
the static mixer (15) is arranged at the downstream of the flash evaporation gas secondary separator (10), is provided with an input port for inputting flash evaporation gas and circulating gas (14) respectively, and is used for mixing the flash evaporation gas and the circulating gas (14); and
the acid gas removal device (100) is internally provided with a liquid separation tank (16) and a circulating gas compressor (17) which are sequentially connected in series from upstream to downstream, the output end of the static mixer (15) is connected with the input end of the liquid separation tank (16) and used for gas-liquid separation, the bottom of the static mixer is provided with an output port for outputting process condensate (21), the top of the static mixer is connected with the input port of the circulating gas compressor (17), and the output port of the circulating gas compressor (17) is connected with the inlet of a downstream conversion unit.
2. The slag water flash steam comprehensive utilization system of the gasification device according to claim 1, characterized in that: also comprises
The flash evaporation gas compressor (11) is arranged at the downstream of the flash evaporation gas secondary separator (10), is connected with the gas output end at the top of the flash evaporation gas secondary separator (10), and is used for cooling the gas phase output by the flash evaporation gas secondary separator (10); and
the output end of the flash evaporation gas compressor (11) is connected with the input end of the static mixer (15) through a second pipeline, and the flash evaporation gas secondary cooler (12) is arranged on the second pipeline and used for cooling the gas phase output by the flash evaporation gas compressor (11).
3. A method for applying the slag water flash steam comprehensive utilization system of the gasification device as claimed in claim 1 or 2, which is characterized in that:
the slag-containing water flash evaporation gas (2) from the gasification device is firstly used as a heat source of a lithium bromide absorption type refrigerating device (7) to produce chilled water, and is used for cooling the high-temperature externally-discharged grey water (1) to below 35 ℃ to obtain low-temperature externally-discharged grey water (6) so as to meet the requirement of a sewage treatment device on the temperature of the externally-discharged grey water;
then enters a flash evaporation gas primary separator (8) for gas-liquid separation, and condensate is discharged;
the separated gas phase sequentially passes through a flash evaporation gas primary cooler (9) and a flash evaporation gas secondary separator (10) to further cool the flash evaporation gas and separate the condensate;
the gas phase separated by the flash gas secondary separator (10) is compressed to the same pressure as the circulating gas (14) in the acid gas removal device (100), and enters a static mixer (15) together with the circulating gas (14) for fully mixing so as to absorb part of carbon dioxide in the flash gas;
the mixed gas enters a liquid separation tank (16) at the inlet of a circulating gas compressor (17) to separate a small amount of methanol condensate, and the mixed gas is pressurized by the circulating gas compressor (17) and then is conveyed to the inlet of a conversion unit/in front of a conversion furnace to recover effective components;
wherein, the condensate at the bottom of the flash evaporation gas primary separator (8) and the flash evaporation gas secondary separator (9) is recycled in a downstream low-pressure system.
4. The comprehensive utilization method of slag water flash steam of a gasification device according to claim 3, characterized in that: when the pressure of flash gas at the outlet of the flash gas compressor (11) is not lower than the pressure of the circulating gas (14), the arrangement of the flash gas compressor (11) and the flash gas secondary cooler (12) is cancelled; when the pressure of flash gas at the outlet of the flash gas compressor (11) is lower than that of the circulating gas (14), the gas phase separated by the flash gas secondary separator (10) sequentially passes through the flash gas compressor (11) and the flash gas secondary cooler (12) to obtain low-temperature flash gas, and the low-temperature flash gas is conveyed to the static mixer (15).
5. The comprehensive utilization method of slag water flash steam of a gasification device according to claim 3, characterized in that: the slag-containing water flash evaporation gas (2) is gas obtained after slag water flash evaporation treatment of the gasification device, the pressure is 0-2.0 MPaG, and the temperature is 50-250 ℃.
6. The comprehensive utilization method of slag water flash steam of a gasification device according to claim 3, characterized in that: the temperature of the freezing water is 0-50 ℃, and the temperature of the low-temperature ash discharge water (6) is 0-50 ℃.
7. The comprehensive utilization method of slag water flash steam of a gasification device according to claim 3, characterized in that: in the flash gas primary cooler 9 and the flash gas secondary cooler 12, the cooling medium is selected from process materials, desalted water, chilled water and boiler feed water in the public engineering medium.
8. The comprehensive utilization method of slag water flash steam of a gasification device according to claim 3, characterized in that: the temperature of flash steam output by the lithium bromide absorption type refrigerating device (7) is 0-250 ℃.
9. The comprehensive utilization method of slag water flash steam of a gasification device according to claim 3, characterized in that: the volume content of dry hydrogen of the circulating gas (14) is 0-50%, and the pressure is 0-2 MPaG.
10. The comprehensive utilization method of slag water flash steam of a gasification device according to claim 3, characterized in that: the operation pressure of the liquid separation tank (16) at the inlet of the circulating gas compressor (17) is 0.1-2.0 MPaG.
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| CN110564455A (en) * | 2019-09-18 | 2019-12-13 | 华陆工程科技有限责任公司 | Fine slag drying method for coal gas making device |
| CN115721951A (en) * | 2022-10-28 | 2023-03-03 | 新疆心连心能源化工有限公司 | Gasification tail gas treatment device and using method thereof |
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