CN212151675U - Coal gasification black water heat recovery device - Google Patents
Coal gasification black water heat recovery device Download PDFInfo
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- CN212151675U CN212151675U CN201922319109.2U CN201922319109U CN212151675U CN 212151675 U CN212151675 U CN 212151675U CN 201922319109 U CN201922319109 U CN 201922319109U CN 212151675 U CN212151675 U CN 212151675U
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Abstract
The application discloses a coal gasification black water heat recovery device, wherein coal gasification black water is decompressed by a decompression pipe; carrying out secondary pressure reduction on the coal gasification black water subjected to pressure reduction by using a pressure reduction angle valve, and conveying the coal gasification black water to a first flash tank for flash evaporation to obtain first non-condensable gas and steam; conveying the first uncondensed gas and the steam to a humidifying tower, and carrying out countercurrent contact on the first uncondensed gas and the steam and low-temperature low-pressure circulating water from a second flash evaporator to realize heat exchange between the first uncondensed gas and the steam and the low-temperature low-pressure circulating water; the first uncondensed gas and steam reduced in the humidified tower are delivered to a first flash cooler. In the embodiment of the application, the first uncondensed gas and the steam obtained by the first flash tank directly enter the humidifying tower, and are subjected to countercurrent heat exchange with the once-heated low-temperature low-pressure circulating water in the humidifying tower, and the steam/water is in countercurrent direct contact, so that the heat transfer efficiency is improved; the mode of combining direct heat exchange and indirect heat exchange is adopted, and both the heat exchange efficiency and the equipment quantity are considered.
Description
The present application claims priority from the chinese patent office filed on 27/12/2018, chinese patent application No. 201822228060.5, the entire contents of which are incorporated herein by reference.
Technical Field
The application relates to the field of heat recovery, in particular to a coal gasification black water heat recovery device.
Background
The patent CN102336496A discloses a technical route for recovering flash heat by a method for treating and recycling grey water of a dry coal powder gasification device, wherein the technical route is designed in such a way that gasified black water directly enters a flash tank for primary flash after passing through a pressure reducing valve and a flow limiting element, meanwhile, process water enters the flash tank to wash flash steam, and the washed flash steam passes through a venturi tube, then enters a dehumidifier for heat exchange and cooling, then is further cooled by a cooler, and then is discharged to a torch; and after the liquid subjected to the primary flash evaporation passes through the secondary flash evaporation, the gas is cooled and discharged to a torch, and the liquid is further subjected to flash evaporation and then sent to a clarification tank.
The process technology effectively utilizes the heat coming out of the primary flash evaporation, and improves the recovery efficiency of the flash evaporation heat, but the technical route adopts a mode of reducing the pressure by a direct pressure reducing valve, so that the pressure reducing valve is seriously abraded due to high-pressure-difference operation, and the long-period operation of equipment is restricted; the venturi tube is adopted for gas-liquid mixing, so that scaling in the tube is easily caused; the secondary flash steam is cooled and separated by cooling water and then discharged to a torch, so that the heat of the secondary flash steam is not further utilized, and the consumption of the cooling water is increased.
The patent CN 1214091C-hydrocarbon is the hot recovery method of waste water containing slag in the raw materials gas apparatus for producing, disclose a hot water tower that adopts flash distillation-heat transfer integration, because dry pulverized coal gasification black water handling capacity is big, when leading to using this equipment to gasify black water and carry out the flash distillation and handle, will cause the equipment size huge, processing, the operation difficulty, simultaneously because all concentrate on hot water tower with key parts such as evaporation and heat transfer system in, equipment structure is complicated, in case the trouble, it is very big to overhaul the degree of difficulty.
SUMMERY OF THE UTILITY MODEL
An application aim at of this application provides a coal gasification black water heat reclamation device to it is low to solve heat transfer efficiency among the prior art, overhauls the problem that the degree of difficulty is big.
The application provides a coal gasification black water heat recovery unit, the device includes: the system comprises a pressure reducing pipe, a pressure reducing angle valve, a first flash tank, a humidifying tower, a second flash cooler, a high-temperature circulating water pump, a first flash cooler, a first gas-liquid separation tank, a torch and a settling tank;
the pressure reducing pipe, the pressure reducing angle valve and the first inlet of the first flash tank are sequentially connected;
the first outlet of the first flash tank is connected with the first inlet of the humidifying tower;
the first outlet of the humidifying tower is connected with the first inlet of the first flash cooler;
a first outlet of the first flash cooler is connected with an inlet of the first gas-liquid separation tank;
the first outlet of the first gas-liquid separation tank is connected with the torch;
the second outlet of the first gas-liquid separation tank is connected with the settling tank;
the first outlet of the second flash cooler is connected with the second inlet of the humidifying tower;
and a second outlet of the humidifying tower is connected with the high-temperature circulating water pump.
Further, the apparatus further comprises: the system comprises a first flash angle valve, a second flash tank, a third flash cooler and a second gas-liquid separation tank;
a second outlet of the first flash tank is sequentially connected with a first flash angle valve and an inlet of the second flash tank;
the first outlet of the second flash tank is connected with the second inlet of the second flash cooler;
the second outlet of the second flash cooler is connected to the first inlet of the third flash cooler;
a first outlet of the third flash cooler is connected with an inlet of the second gas-liquid separation tank;
the first outlet of the second gas-liquid separation tank is connected with the torch;
and a second outlet of the second gas-liquid separation tank is connected with the settling tank.
Further, the apparatus further comprises: a second flash angle valve, a third flash tank, a fourth flash cooler, a vacuum pump, a third gas-liquid separation tank and a flash pump;
a second outlet of the second flash tank is connected with an inlet of the third flash tank through a second flash angle valve;
a first outlet of the third flash tank is connected to a first inlet of the fourth flash cooler;
a first outlet of the fourth flash cooler is connected with an inlet of the third gas-liquid separation tank;
the first outlet of the third gas-liquid separation tank is connected with the vacuum pump;
a second outlet of the third gas-liquid separation tank is connected with the settling tank;
and a second outlet of the third flash tank is connected with the settling tank through a flash pump.
Further, a control valve is arranged on the first outlet pipeline of the first gas-liquid separation tank.
Further, a control valve is arranged on the first outlet pipeline of the second gas-liquid separation tank.
According to the technical scheme, the coal gasification black water heat recovery device has the advantages that the coal gasification black water is decompressed by the decompression pipe, and the pressure is reduced to 2.0-3.5 Mpa; carrying out secondary pressure reduction on the coal gasification black water subjected to pressure reduction by using a pressure reduction angle valve, and conveying the coal gasification black water to a first flash tank for flash evaporation to obtain first non-condensable gas and steam, and first black water; conveying the first non-condensable gas and the water vapor to a humidifying tower, and carrying out countercurrent contact with low-temperature low-pressure circulating water from a second flash evaporator to realize heat exchange between the first non-condensable gas and the water vapor and the low-temperature low-pressure circulating water, wherein the temperature of the low-temperature low-pressure circulating water is increased, and the temperature of the first non-condensable gas and the water vapor is reduced; pressurizing the heated low-temperature low-pressure circulating water by a high-temperature circulating water pump to form high-temperature high-pressure circulating water; conveying the first noncondensable water and the steam cooled in the humidifying tower to a first flash cooler, and after the first flash cooler exchanges heat with circulating cooling water and is cooled, allowing the first non-condensable water and the steam to enter a first gas-liquid separation tank for gas-liquid separation to obtain second noncondensable water and the steam and first condensate; conveying the second uncondensed gas and steam separated from the first gas-liquid separation tank to a flare; and conveying the condensate separated by the first gas-liquid separation tank to a settling tank. This application embodiment, the first noncondensable water and the steam that first flash tank obtained directly enter into humidifying tower, with the low temperature low pressure circulating water that has heated once in humidifying tower, carry out countercurrent flow heat transfer, steam/water countercurrent direct contact, improve heat transfer efficiency. The process target is realized by adopting the combination of direct heat exchange and indirect heat exchange, and the number of complex hot water towers is reduced. And the mode of independently performing flash evaporation and heat exchange is adopted, so that the difficulty in maintenance is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a coal gasification black water heat recovery device provided by the present application.
Illustration of the drawings: 1-a pressure reducing pipe, 2-a pressure reducing angle valve, 3-a first flash tank, 4-a humidifying tower, 5-a second flash cooler, 6-a high-temperature circulating water pump, 7-a first flash cooler, 8-a first gas-liquid separation tank, 9-a torch, 10-a settling tank, 11-a first flash angle valve, 12-a second flash tank, 13-a third flash cooler, 14-a second gas-liquid separation tank, 15-a second flash angle valve, 16-a third flash tank, 17-a fourth flash cooler, 18-a vacuum pump, 19-a third gas-liquid separation tank and 20-a flash pump.
Detailed Description
Referring to fig. 1, a coal gasification black water heat recovery device provided by an embodiment of the present application is shown, and the device includes: the system comprises a pressure reducing pipe 1, a pressure reducing angle valve 2, a first flash tank 3, a humidifying tower 4, a second flash cooler 5, a high-temperature circulating water pump 6, a first flash cooler 7, a first gas-liquid separation tank 8, a torch 9 and a settling tank 10;
the pressure reducing pipe 1, the pressure reducing angle valve 2 and a first inlet of the first flash tank 3 are sequentially connected;
the coal gasification black water is decompressed by a decompression pipe 1, and the pressure is reduced to 2.0-3.5 Mpa;
specifically, the coal gas black water is high-temperature and high-pressure solid-containing black water from the bottom of the gasification furnace, the temperature of the coal gas black water is 220 ℃, and the pressure of the coal gas black water is 4.5 MPa. And the pressure of the coal gas black water is reduced by a pressure reducing valve, and the pressure is reduced to 2.0-3.5 Mpa.
Carrying out secondary pressure reduction on the coal gasification black water subjected to pressure reduction by using a pressure reduction angle valve 2, and then conveying the coal gasification black water to a first flash tank 3 for flash evaporation to obtain first non-condensable gas and steam, and first black water;
specifically, the coal gasification black water decompressed in the decompression pipe 1 is decompressed to 0.7Mpa again through the decompression angle valve 2, and then enters the first flash tank 3 for flash evaporation to obtain first non-condensable gas at 170 ℃ and steam.
This application embodiment, before getting into first flash tank 3, will coal gas black water step-down can reduce the preceding back pressure differential of flash valve like this, reduce wear.
A first outlet of the first flash tank 3 is connected with a first inlet of the humidifying tower 4; the first non-condensable gas and the water vapor are conveyed into a humidifying tower 4 and are in countercurrent contact with low-temperature low-pressure circulating water from a second flash cooler 5, so that heat exchange between the first non-condensable gas and the water vapor and the low-temperature low-pressure circulating water is realized, the temperature of the low-temperature low-pressure circulating water is increased, and the temperature of the first non-condensable gas and the water vapor is reduced;
specifically, the first uncondensed gas and the steam are conveyed to a humidifying tower 4, and are in direct countercurrent contact with low-temperature low-pressure circulating water from a second flash cooler 5 in the humidifying tower 4. The first non-condensable gas and the steam exchange heat with the low-temperature low-pressure circulating water. The temperature of the first non-condensable gas and the steam is reduced to below 170 ℃, and the low-temperature and low-pressure circulating water is heated to 140-160 ℃.
This application embodiment, the first noncondensable water and the steam that first flash tank 3 obtained directly enter into humidifying tower 4, and with the low temperature low pressure circulating water that has heated once in humidifying tower 4, carry out countercurrent flow heat transfer, steam/water countercurrent direct contact improves heat transfer efficiency.
According to the embodiment of the application, the process target is jointly realized by adopting a form of combining direct heat exchange and indirect heat exchange, and the number of complex hot water towers is reduced. And the mode of independently performing flash evaporation and heat exchange is adopted, so that the difficulty in maintenance is reduced.
A first outlet of the humidifying tower 4 is connected with a first inlet of the first flash cooler 7;
a first outlet of the first flash cooler 7 is connected with an inlet of the first gas-liquid separation tank 8;
the heated low-temperature low-pressure circulating water is pressurized by a high-temperature circulating water pump 6 to become high-temperature high-pressure circulating water;
the low-temperature and low-pressure circulating water obtained in the humidifying tower 4 after being heated is pressurized by the high-temperature circulating water pump 6 to become high-temperature and high-pressure circulating water, and the high-temperature and high-pressure circulating water is sent to the gasification boundary area to be used as process circulating water of the gasification boundary area. The embodiments of the present application also provide a return line to control or maintain the system water balance.
The first uncondensed gas and the steam which are cooled in the humidifying tower 4 are conveyed to a first flash cooler 7, and after the first flash cooler 7 exchanges heat with circulating cooling water and is cooled, the first flash cooler enters a first gas-liquid separation tank 8 to be subjected to gas-liquid separation, so that second uncondensed gas and the steam as well as first condensed liquid are obtained;
the first outlet of the first gas-liquid separation tank 8 is connected with the torch 9; conveying the second uncondensed gas and steam separated from the first gas-liquid separation tank 8 to a flare 9;
the noncondensable water and the steam that flash distillation goes out in this application embodiment all carry out once circulating cooling water cooling before discharging to torch 9 to further separate noncondensable water and steam through the gas-liquid separation jar, increase and retrieve the condensate liquid volume.
A second outlet of the first gas-liquid separation tank 8 is connected with the settling tank 10; and conveying the condensate separated from the first gas-liquid separation tank 8 to a settling tank 10.
The first condensate separated by the first gas-liquid separation tank 8 is sent to a settling tank 10 for recycling.
A first outlet of the second flash cooler 5 is connected with a second inlet of the humidifying tower 4;
and a second outlet of the humidifying tower 4 is connected with the high-temperature circulating water pump 6.
Further, referring again to fig. 1, the apparatus further includes: a first flash angle valve 11, a second flash tank 12, a third flash cooler 13 and a second gas-liquid separation tank 14;
a second outlet of the first flash tank 3 is sequentially connected with a first flash angle valve 11 and an inlet of a second flash tank 12;
a first outlet of the second flash tank 12 is connected to a second inlet of the second flash cooler 5;
the second outlet of the second flash cooler 5 is connected to the first inlet of the third flash cooler 13;
a first outlet of the third flash cooler 13 is connected with an inlet of the second gas-liquid separation tank 14;
a first outlet of the second gas-liquid separation tank 14 is connected with the flare 9;
a second outlet of the second knockout drum 14 is connected to the settling tank 10. The first black water is decompressed by a first flash angle valve 11, then is conveyed to a second flash tank 12, and is subjected to flash evaporation in the second flash tank 12 to obtain third non-condensed water, steam and second black water;
specifically, the first black water contains more solids than the coal gasification black water. And after the pressure of the first black water is reduced, the first black water enters a second flash tank 12 and is flashed in the second flash tank 12 to obtain 134 ℃ third non-condensable gas and steam and second black water. The second black water contains more solids than the first black water.
Conveying the third uncondensed gas and the steam to a second flash evaporator cooler 5 for heat exchange with low-temperature low-pressure circulating water; the third non-condensable gas and the steam exchange heat with low-temperature low-pressure circulating water outside the battery limits in the second flash cooler 5, and the low-temperature low-pressure circulating water is heated to 106 ℃.
The second flash evaporator cooler 5 heats the low-temperature low-pressure circulating water and then conveys the heated low-temperature low-pressure circulating water to the humidifying tower 4;
specifically, the heated low-temperature low-pressure circulating water is sent to the humidifying tower 4 to exchange heat with the first uncondensed water and the steam.
In the second flash evaporator cooler 5, the second non-condensable gas and the steam are cooled and then are conveyed to a third flash evaporator cooler 13, the second non-condensable gas and the steam are subjected to heat exchange with circulating cooling water and then are conveyed to a third gas-liquid separation tank 19 for gas-liquid separation, and fourth non-condensable gas and the steam and the second condensate are obtained through separation;
the fourth non-condensable gas and steam are conveyed to a flare 9 and the second condensate is conveyed to a settling tank 10.
Specifically, the separated second condensate is sent to the settling tank 10 for recycling.
Further, referring again to fig. 1, the apparatus further includes: a second flash angle valve 15, a third flash tank 16, a fourth flash cooler 17, a vacuum pump 18, a third gas-liquid separation tank 19 and a flash pump 20;
a second outlet of the second flash tank 12 is connected to an inlet of the third flash tank 16 through a second flash angle valve 15;
a first outlet of the third flash tank 16 is connected to a first inlet of the fourth flash cooler 17;
a first outlet of the fourth flash cooler 17 is connected with an inlet of the third gas-liquid separation tank 19;
a first outlet of the third gas-liquid separation tank 19 is connected to the vacuum pump 18;
a second outlet of the third gas-liquid separation tank 19 is connected with the settling tank 10;
a second outlet of the third flash tank 16 is connected to the settling tank 10 by a flash pump 20.
The second black water is decompressed by a second flash angle valve 15, then is conveyed to a third flash tank 16, and is flashed in the third flash tank 16 to obtain flash steam and third black water;
the third flash tank 16 pumps flash steam through a vacuum pump 18 to control the vacuum degree and ensure the pressure to be between-50 and-25 KpaG;
the flash steam is conveyed to a fourth flash cooler 17 to exchange heat with circulating cooling water to obtain cooled flash steam;
conveying the cooled flash steam to a third gas-liquid separation tank 19 for gas-liquid separation to obtain non-condensable gas and third condensate;
conveying the non-condensable gas to a torch 9 or a high-point discharge by using a flash vacuum pump arranged on a gas phase outlet pipeline at the top of the third gas-liquid separation tank 19; the third condensate is conveyed to a third settling tank 10;
the third black water enters the settling tank 10 by using a flash pump 20 or by gravity flow.
Specifically, the third black water separated by the third flash tank 16 contains more solids than the second black water, and the third black water enters the settling tank 10 through the flash pump 20 or by gravity flow, and is clarified in the settling tank 10.
Further, a control valve is arranged on the first outlet pipeline of the first gas-liquid separation tank 8.
The pressure of the first flash tank 3 is controlled by a control valve arranged on an outlet pipeline of the first gas-liquid separation tank 8, and the pressure is controlled at 0.5-0.7 MpaG.
Further, a control valve is provided on the first outlet line of the second gas-liquid separation tank 14.
The pressure of the second flash tank 12 is controlled by a control valve provided in the outlet line of the second knock-out tank 14 at a pressure of 0.15 to 0.35 MpaG.
According to the technical scheme, the coal gasification black water heat recovery device has the advantages that the coal gasification black water is decompressed by the decompression pipe 1, and the pressure is reduced to 2.0-3.5 Mpa; carrying out secondary pressure reduction on the coal gasification black water subjected to pressure reduction by using a pressure reduction angle valve 2, and then conveying the coal gasification black water to a first flash tank 3 for flash evaporation to obtain first non-condensable gas and steam, and first black water; the first non-condensable gas and the water vapor are conveyed into a humidifying tower 4 and are in countercurrent contact with low-temperature low-pressure circulating water from a second flash cooler 5, so that heat exchange between the first non-condensable gas and the water vapor and the low-temperature low-pressure circulating water is realized, the temperature of the low-temperature low-pressure circulating water is increased, and the temperature of the first non-condensable gas and the water vapor is reduced; the heated low-temperature low-pressure circulating water is pressurized by a high-temperature circulating water pump 6 to become high-temperature high-pressure circulating water; the first uncondensed gas and the steam which are cooled in the humidifying tower 4 are conveyed to a first flash cooler 7, and after the first flash cooler 7 exchanges heat with circulating cooling water and is cooled, the first flash cooler enters a first gas-liquid separation tank 8 to be subjected to gas-liquid separation, so that second uncondensed gas and the steam as well as first condensed liquid are obtained; conveying the second uncondensed gas and steam separated from the first gas-liquid separation tank 8 to a flare 9; and conveying the condensate separated from the first gas-liquid separation tank 8 to a settling tank 10. This application embodiment, the first noncondensable water and the steam that first flash tank 3 obtained directly enter into humidifying tower 4, and with the low temperature low pressure circulating water that has heated once in humidifying tower 4, carry out countercurrent flow heat transfer, steam/water countercurrent direct contact improves heat transfer efficiency. The process target is realized by adopting the combination of direct heat exchange and indirect heat exchange, and the number of complex hot water towers is reduced. And the mode of independently performing flash evaporation and heat exchange is adopted, so that the difficulty in maintenance is reduced.
Other embodiments of the present application will be apparent to those skilled in the art from consideration of the specification and practice of the application disclosed herein. This application is intended to cover any variations, uses, or adaptations of the invention following, in general, the principles of the application and including such departures from the present disclosure as come within known or customary practice within the art to which the invention pertains. It is intended that the specification and examples be considered as exemplary only, with a true scope and spirit of the application being indicated by the following claims.
It will be understood that the present application is not limited to the precise arrangements described above and shown in the drawings and that various modifications and changes may be made without departing from the scope thereof. The scope of the application is limited only by the appended claims.
Claims (5)
1. A coal gasification black water heat recovery device, characterized in that the device comprises: the system comprises a pressure reducing pipe (1), a pressure reducing angle valve (2), a first flash tank (3), a humidifying tower (4), a second flash cooler (5), a high-temperature circulating water pump (6), a first flash cooler (7), a first gas-liquid separation tank (8), a torch (9) and a settling tank (10);
the pressure reducing pipe (1), the pressure reducing angle valve (2) and a first inlet of the first flash tank (3) are connected in sequence;
a first outlet of the first flash tank (3) is connected with a first inlet of the humidifying tower (4);
the first outlet of the humidifying tower (4) is connected with the first inlet of the first flash cooler (7);
a first outlet of the first flash cooler (7) is connected with an inlet of the first gas-liquid separation tank (8);
the first outlet of the first gas-liquid separation tank (8) is connected with the torch (9);
a second outlet of the first gas-liquid separation tank (8) is connected with the settling tank (10);
the first outlet of the second flash cooler (5) is connected with the second inlet of the humidifying tower (4);
and a second outlet of the humidifying tower (4) is connected with the high-temperature circulating water pump (6).
2. The coal gasification black water heat recovery apparatus of claim 1, further comprising: a first flash angle valve (11), a second flash tank (12), a third flash cooler (13) and a second gas-liquid separation tank (14);
a second outlet of the first flash tank (3) is sequentially connected with a first flash angle valve (11) and an inlet of a second flash tank (12);
a first outlet of the second flash tank (12) is connected to a second inlet of the second flash cooler (5);
the second outlet of the second flash cooler (5) is connected to the first inlet of the third flash cooler (13);
a first outlet of the third flash cooler (13) is connected with an inlet of the second gas-liquid separation tank (14);
the first outlet of the second gas-liquid separation tank (14) is connected with the torch (9);
and a second outlet of the second gas-liquid separation tank (14) is connected with the settling tank (10).
3. The coal gasification black water heat recovery apparatus of claim 2, further comprising: a second flash angle valve (15), a third flash tank (16), a fourth flash cooler (17), a vacuum pump (18), a third gas-liquid separation tank (19) and a flash pump (20);
a second outlet of the second flash tank (12) is connected with an inlet of the third flash tank (16) through a second flash angle valve (15);
a first outlet of the third flash tank (16) is connected to a first inlet of the fourth flash cooler (17);
a first outlet of the fourth flash cooler (17) is connected with an inlet of the third gas-liquid separation tank (19);
the first outlet of the third gas-liquid separation tank (19) is connected with the vacuum pump (18);
a second outlet of the third gas-liquid separation tank (19) is connected with the settling tank (10);
the second outlet of the third flash tank (16) is connected to the settling tank (10) by a flash pump (20).
4. The coal gasification black water heat recovery device according to claim 1, wherein a control valve is arranged on the first outlet pipeline of the first gas-liquid separation tank (8).
5. The coal gasification black water heat recovery device according to claim 2, wherein a control valve is provided on the first outlet line of the second gas-liquid separation tank (14).
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| CN201822228060 | 2018-12-27 | ||
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110877919A (en) * | 2018-12-27 | 2020-03-13 | 宁夏神耀科技有限责任公司 | Coal gasification black water heat recovery method and device |
| CN112939125A (en) * | 2021-01-25 | 2021-06-11 | 内蒙古伊姆克系统科技有限公司 | Coal gasification black water flash evaporation gas spraying heat exchange system and method |
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2019
- 2019-12-20 CN CN201922319109.2U patent/CN212151675U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110877919A (en) * | 2018-12-27 | 2020-03-13 | 宁夏神耀科技有限责任公司 | Coal gasification black water heat recovery method and device |
| CN110877919B (en) * | 2018-12-27 | 2024-05-03 | 宁夏神耀科技有限责任公司 | Coal gasification black water heat recovery method and device |
| CN112939125A (en) * | 2021-01-25 | 2021-06-11 | 内蒙古伊姆克系统科技有限公司 | Coal gasification black water flash evaporation gas spraying heat exchange system and method |
| CN112939125B (en) * | 2021-01-25 | 2023-01-03 | 内蒙古伊姆克系统科技有限公司 | Coal gasification black water flash evaporation gas spray heat exchange system and method |
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