CN112125365A - Coal gasification black water treatment system - Google Patents
Coal gasification black water treatment system Download PDFInfo
- Publication number
- CN112125365A CN112125365A CN202011008460.0A CN202011008460A CN112125365A CN 112125365 A CN112125365 A CN 112125365A CN 202011008460 A CN202011008460 A CN 202011008460A CN 112125365 A CN112125365 A CN 112125365A
- Authority
- CN
- China
- Prior art keywords
- tower
- tank
- separator
- stage
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000010866 blackwater Substances 0.000 title claims abstract description 69
- 238000002309 gasification Methods 0.000 title claims abstract description 53
- 239000003245 coal Substances 0.000 title claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 130
- 239000007789 gas Substances 0.000 claims abstract description 54
- 238000001704 evaporation Methods 0.000 claims abstract description 40
- 230000008020 evaporation Effects 0.000 claims abstract description 40
- 239000007791 liquid phase Substances 0.000 claims description 46
- 239000012071 phase Substances 0.000 claims description 30
- 239000002699 waste material Substances 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- 239000006232 furnace black Substances 0.000 claims description 2
- 239000007792 gaseous phase Substances 0.000 claims 2
- 239000002253 acid Substances 0.000 abstract description 10
- 239000002918 waste heat Substances 0.000 abstract description 10
- 238000011084 recovery Methods 0.000 abstract description 9
- 230000007774 longterm Effects 0.000 abstract description 3
- 239000010797 grey water Substances 0.000 description 21
- 239000006227 byproduct Substances 0.000 description 11
- 230000008901 benefit Effects 0.000 description 9
- 239000007788 liquid Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 230000005484 gravity Effects 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 101100298225 Caenorhabditis elegans pot-2 gene Proteins 0.000 description 3
- 230000001174 ascending effect Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Abstract
The invention provides a coal gasification black water treatment system, which comprises a high-temperature hot water tower and a secondary flash tank which are sequentially connected, wherein a gas phase outlet of the high-temperature hot water tower is sequentially connected with a stripping tower after passing through a primary cooler and a primary separator, and a gas phase outlet of the secondary flash tank is sequentially connected with the stripping tower after passing through a secondary cooler and a secondary separator. The coal gasification black water treatment system provided by the invention fully flashes the gasification black water, further strips the primary and secondary flash evaporation steam condensate with high content of acid gas components, reduces the acid components in the gasification water system, prevents scaling of the whole system, prevents blockage of pipeline valves, ensures long-term stable operation of the device, fully recovers heat of each stage, effectively improves waste heat recovery efficiency, and reduces heat loss.
Description
Technical Field
The invention belongs to the technical field of coal gasification, and particularly relates to a coal gasification black water treatment system.
Background
The traditional coal gasification black water flash evaporation process generally adopts three-stage flash evaporation treatment, flash evaporation steam at all stages is directly cooled by circulating water, and non-condensable gas is sent out of a boundary region for treatment.
The traditional three-stage flash evaporation treatment system for the gasified black water comprises the following steps:
black water from a gasification furnace and a washing tower is decompressed by a black water angle valve and enters a high-pressure flash tank, and high-flash steam at the top of the tank is cooled by circulating water and then is directly sent to a boundary region for incineration or recovery treatment; black water at the bottom of the high-pressure flash tank enters a low-pressure flash tank for further flash evaporation, and low flash gas at the top of the low-pressure flash tank is sent to a gasification deaerator to heat low-pressure grey water from a grey water tank and low-temperature conversion condensate from a conversion section; and (3) feeding the black water at the bottom of the low-pressure flash tank to a vacuum flash tank for flash evaporation, cooling the flash gas at the top by circulating water, then emptying, and feeding the black water at the bottom to a clarifying tank for settlement treatment.
The traditional three-stage flash evaporation treatment system for the gasified black water generally has the following problems that (1) the circulating water consumption is large and the energy consumption is high; (2) scale is easy to form in the deaerator, and the blockage problem is serious; (3) the gasification system has high acid gas content, which causes the easy scaling of the whole system, blocks the pipeline valve and influences the stable operation of the gasification system
Disclosure of Invention
In view of the above, the invention aims to provide a coal gasification black water treatment system, which carries out full flash evaporation on gasification black water, further carries out steam stripping on primary and secondary flash evaporation steam condensate with high content of acid gas components, reduces the acid components in a gasification water system, ensures that the whole system is not easy to scale, blocks a pipeline valve, ensures that a device stably operates for a long time, fully recovers heat of each stage, effectively improves waste heat recovery efficiency, and reduces heat loss.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
the coal gasification black water treatment system comprises a high-temperature hot water tower and a secondary flash tank which are sequentially connected, wherein a gas phase outlet of the high-temperature hot water tower is sequentially connected with a stripping tower after passing through a primary cooler and a primary separator, and a gas phase outlet of the secondary flash tank is sequentially connected with the stripping tower after passing through a secondary cooler and a secondary separator.
Further, the gas phase outlets of the first-stage separator and the second-stage separator are connected with the gas phase inlet of the stripping tower, and the liquid phase outlets of the first-stage separator and the second-stage separator are connected with the liquid phase inlet of the stripping tower.
Furthermore, the primary cooler and the secondary cooler are both connected with a hot water supply inlet of the thermal power station and a hot water return outlet of the thermal power station.
Further, a liquid phase outlet of the stripping tower is connected with the upper part of the high-temperature hot water tower, the top of the stripping tower is sequentially connected with a tower top cooler and a tower top separator, a liquid phase outlet of the tower top separator is connected with the upper part of the stripping tower, and a gas phase outlet of the tower top separator is connected with a stripping gas outlet.
Furthermore, the lower part of the high-temperature hot water tower is connected with a black water inlet of the gasification furnace and a black water inlet of the washing tower, a liquid phase outlet of the high-temperature hot water tower is connected with a hot water outlet, and the upper part of the high-temperature hot water tower is connected with a transformation condensate inlet.
Further, still include tertiary flash system, tertiary flash system includes the first tertiary flash tank of series connection, the tertiary flash tank of second, first tertiary flash tank with the liquid phase exit linkage of second grade flash tank, the liquid phase export of first tertiary flash tank is connected with the tertiary flash tank of second, and the liquid phase export and the black water exit linkage of the tertiary flash tank of second.
Further, the vacuum degrees of the first three-stage flash tank and the second three-stage flash tank are different.
Further, the gas phase outlet of the first tertiary flash tank is connected with the first tertiary cooler and the first tertiary separator in sequence, the gas phase outlet of the second tertiary flash tank is connected with the second tertiary cooler and the second tertiary separator in sequence, the gas phase outlet of the first tertiary separator and the gas phase outlet of the second tertiary separator are both connected with the vent, and the liquid phase outlet of the first tertiary separator and the liquid phase outlet of the second tertiary separator are both connected with the condensate tank.
Furthermore, cold water inlets of the first and second tertiary coolers are connected with a desalted water inlet, cold water outlets of the first and second tertiary coolers are connected with a deaerator, a liquid phase outlet of the deaerator is connected with a waste pot, a steam outlet of the waste pot is connected with the deaerator and a stripping tower, and the waste pot is further connected with a high-temperature hot water tower and a primary cooler.
Furthermore, the condensate tank is connected with the grey water tank, the grey water tank is also connected with the clarifying tank, a liquid phase outlet of the grey water tank is connected with the grey water outlet and the upper part of the high-temperature hot water tower, the clarifying tank is connected with a black water inlet, the black water inlet is connected with the black water outlet, and the bottom of the clarifying tank is connected with a black water outlet of a black water filtering plant.
Further, the high-temperature hot water tower adopts a tower plate type internal part, flash steam at the lower section enters the upper section through the ascending pipe to directly exchange heat with water, and the operating pressure of the high-temperature hot water tower is 0.7-1.0 MPa.
Furthermore, the waste boiler shell side by-product is 0.4-0.6MPa steam.
Furthermore, the primary cooler adopts a shell-and-tube heat exchanger, and the outlet temperature of the low-temperature hot water is 60-95 ℃.
Furthermore, the first-stage separator adopts a gravity type gas-liquid separator with a demister, and the operating pressure is 0.65-0.85 MPa.
Further, the operating pressure of the secondary flash tank is 0.3-0.5MPa, and the tower top temperature is 115-145 ℃.
Furthermore, the secondary cooler adopts a shell-and-tube heat exchanger, and the outlet temperature of the low-temperature hot water is 60-95 ℃.
Furthermore, the second-stage separator adopts a gravity type gas-liquid separator with a demister, and the operating pressure is 0.27-0.47 MPa;
furthermore, the three-stage flash evaporation system adopts a first three-stage flash evaporation tank and a second three-stage flash evaporation tank which are connected in series and arranged up and down, and the operating pressure is 0.07-0.09 MPa.
Further, the first three-stage flash tank and the second three-stage flash tank which are connected in series share one set of vacuum pumping system.
Further, the three-stage cooler adopts a shell-and-tube heat exchanger, and desalted water can be heated to 60-70 ℃.
Furthermore, the three-stage separator adopts a gravity type gas-liquid separator with a demister, outlet pipelines at the top of the separator are respectively provided with pressure control, and the operating pressure is 0.07-0.09 MPa.
Furthermore, the stripping tower adopts plate-type tower internals, and the operating pressure is 0.2-0.3 MPa.
Further, the tower top cooler adopts a shell-and-tube heat exchanger, and the outlet temperature of the low-temperature hot water is 60-95 ℃.
Further, the liquid-phase feeding material of the deaerator is desalted water, and the operating pressure is 0.12-0.4 MPa.
Compared with the prior art, the coal gasification black water treatment system has the following advantages:
(1) sufficient flash evaporation is carried out on the gasified black water, the primary flash evaporation steam condensate and the secondary flash evaporation steam condensate with high content of acid gas components are further stripped, the acid components in a gasified water system are reduced, the whole system is not easy to scale, pipeline valves are not easy to block, the long-term stable operation of the device is ensured, and all levels of heat are sufficiently recovered, so that the waste heat recovery efficiency is effectively improved, and the heat loss is reduced.
(2) The gasified grey water is directly heated in the high-temperature hot water tower, low-level heat of flash steam at each stage is used for heating low-temperature hot water, heat at each stage is fully recovered, and waste heat recovery efficiency is improved. And the gasified grey water and the conversion condensate are directly heated in the high-temperature hot water tower, so that the heat exchange is more sufficient.
(3) Utilize multistage waste heat recovery, fully retrieve the heat, improve gasification water system quality of water, guarantee the steady operation of system, improve the economic benefits of mill.
(4) The deaerator only processes desalted water, and the device stop caused by the scale blockage of the deaerator is avoided.
(5) The waste boiler is arranged, and the byproduct steam of the waste boiler is used as a heat source of the deaerator and the stripping tower, so that the energy is fully saved, and the economic benefit of a factory is improved. The waste boiler is arranged for producing the steam as the byproduct, and the steam as the byproduct is used by the stripping tower and the deaerator, so that the steam consumption of the device is reduced, and the economic benefit is improved.
(6) The cooling medium of each stage of flash evaporation cooler uses the low-temperature hot water of the whole plant to replace circulating cooling water, thereby reducing the consumption of the circulating water, recovering the heat and improving the economic benefit.
(7) The three-stage flash evaporation system is provided with two three-stage flash evaporation tanks connected in series, and is more suitable for the current large-scale coal gasification project.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and, together with the description, serve to explain the invention without limitation. In the drawings:
FIG. 1 is a schematic view of a coal gasification black water treatment system according to an embodiment of the present invention.
Description of reference numerals:
1-high temperature hot water tower; 2-waste pot; 3-a first-stage cooler; 4-a secondary flash tank; 5-a three-stage flash system; 51-a first three-stage flash tank; 52-a second three-stage flash tank; 6-a secondary separator; 7-a secondary cooler; 8-a first-stage separator; 9-a deaerator; 10-overhead cooler; 11-overhead separator; 12-a stripping column; 13-a first tertiary cooler; 14-a first tertiary separator; 15-a second tertiary cooler; 16-a second three-stage separator; 17-a condensate tank; 18-a clarifying tank; 19-ash water tank;
a-grey water outlet; b-a shift condensate inlet; c-a hot water outlet; d-a black water inlet of the gasification furnace; e-black water inlet of the water washing tower; f-a low-pressure steam outlet; g-black water outlet; h-air release port; i-a stripping gas outlet; j-low pressure steam inlet; k-black water is discharged from a filtering workshop outlet; an L-black water inlet; an M-desalted water inlet; HWS-hot water feed water inlet of thermal power station; HWR-hot water return outlet of the thermal power station.
Detailed Description
It should be noted that the embodiments and features of the embodiments of the present invention may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings, which are merely for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be construed as limiting the invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the invention, the meaning of "a plurality" is two or more unless otherwise specified.
In the description of the invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted", "connected" and "connected" are to be construed broadly, e.g. as being fixed or detachable or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. Unless otherwise specifically stated or limited, the term "fixedly connected" may be a commonly used fixedly connected manner such as a plug, a weld, a threaded connection, a bolt connection, etc. The specific meaning of the above terms in the creation of the present invention can be understood by those of ordinary skill in the art through specific situations.
The invention will be described in detail with reference to the following embodiments with reference to the attached drawings.
The coal gasification black water treatment system comprises a high-temperature hot water tower 1 and a secondary flash tank 4 which are sequentially connected, wherein a gas phase outlet of the high-temperature hot water tower 1 is sequentially connected with a stripping tower 12 after passing through a primary cooler 3 and a primary separator 8, and a gas phase outlet of the secondary flash tank 4 is sequentially connected with the stripping tower 12 after passing through a secondary cooler 7 and a secondary separator 6.
The coal gasification black water treatment system carries out full flash evaporation on the gasification black water, and further carries out steam stripping on the primary flash evaporation steam condensate and the secondary flash evaporation steam condensate with high content of acid gas components, so that the acid components in the gasification water system are reduced, the whole system is not easy to scale, a pipeline valve is not easy to block, the long-term stable operation of the device is ensured, and all levels of heat are fully recovered, the waste heat recovery efficiency is effectively improved, and the heat loss is reduced.
Utilize multistage waste heat recovery, fully retrieve the heat, improve gasification water system quality of water, guarantee the steady operation of system, improve the economic benefits of mill.
And gas phase outlets of the first-stage separator 8 and the second-stage separator 6 are connected with a gas phase inlet of the stripping tower 12, and liquid phase outlets of the first-stage separator 8 and the second-stage separator 6 are connected with a liquid phase inlet of the stripping tower 12.
And the primary cooler 3 and the secondary cooler 7 are both connected with a hot water supply inlet HWS and a hot water return outlet HWR of the thermal power station.
The cooling medium of each stage of flash evaporation cooler uses factory low-temperature hot water to replace circulating cooling water, thereby reducing the consumption of the circulating water, recovering heat and improving economic benefits
A liquid phase outlet of the stripping tower 12 is connected with the upper part of the high-temperature hot water tower 1, the top of the stripping tower 12 is sequentially connected with an overhead cooler 10 and an overhead separator 11, a liquid phase outlet of the overhead separator 11 is connected with the upper part of the stripping tower 12, and a gas phase outlet of the overhead separator 11 is connected with a stripping gas outlet I.
The lower part of the high-temperature hot water tower 1 is connected with a gasification furnace black water inlet D and a washing tower black water inlet E, a liquid phase outlet of the high-temperature hot water tower 1 is connected with a hot water outlet C, and the upper part of the high-temperature hot water tower 1 is connected with a transformation condensate inlet B.
The gasified grey water is directly heated in the high-temperature hot water tower 1, low-level heat of flash steam at each stage is used for heating low-temperature hot water, heat at each stage is fully recovered, and waste heat recovery efficiency is improved. And the gasified grey water and the conversion condensate are directly heated in the high-temperature hot water tower 1, so that the heat exchange is more sufficient.
Still include tertiary flash system 5, tertiary flash system 5 is including the first tertiary flash tank 51 of series connection, the tertiary flash tank 52 of second, first tertiary flash tank 51 with the liquid phase exit linkage of second grade flash tank 4, the liquid phase export of first tertiary flash tank 51 is connected with the tertiary flash tank 52 of second, and the liquid phase export of the tertiary flash tank 52 of second is connected with black water outlet G.
The first three-stage flash tank 51 and the second three-stage flash tank 52 have different vacuum degrees.
The three-stage flash evaporation system 5 is provided with two three-stage flash evaporation tanks connected in series, and is more suitable for the current large-scale coal gasification project.
The gas phase outlet of the first three-level flash tank 51 is sequentially connected with the first three-level cooler 13 and the first three-level separator 14, the gas phase outlet of the second three-level flash tank 52 is sequentially connected with the second three-level cooler 15 and the second three-level separator 16, the gas phase outlet of the first three-level separator 14 and the gas phase outlet of the second three-level separator 16 are both connected with the vent gas port H, and the liquid phase outlet of the first three-level separator 14 and the liquid phase outlet of the second three-level separator 16 are both connected with the condensate tank 17.
The cold water inlets of the first three-stage cooler 13 and the second three-stage cooler 15 are connected with a desalted water inlet M, the cold water outlets of the first three-stage cooler 13 and the second three-stage cooler 15 are connected with a deaerator 9, the liquid phase outlet of the deaerator 9 is connected with a waste pot 2, the steam outlet of the waste pot 2 is connected with the deaerator 9 and a stripping tower 12, and the waste pot 2 is further connected with a high-temperature hot water tower 1 and a primary cooler 3.
The waste boiler 2 is arranged, and the byproduct steam of the waste boiler 2 is used as a heat source of the deaerator 9 and the stripping tower 12, so that the energy is fully saved, and the economic benefit of a factory is improved. The waste boiler 2 is arranged for producing steam as a byproduct, and the steam as the byproduct is used by the stripping tower 12 and the deaerator 9, so that the steam consumption of the device is reduced, and the economic benefit is improved.
The deaerator 9 only treats desalted water, and the device stop caused by scaling and blockage of the deaerator 9 is avoided.
The condensate tank 17 is connected with the grey water tank 19, the grey water tank 19 is further connected with the clarifying tank 18, a liquid phase outlet of the grey water tank 19 is connected with the grey water outlet A and the upper part of the high-temperature hot water tower 1, the clarifying tank 18 is connected with a black water inlet L, the black water inlet L is connected with the black water outlet G, and the bottom of the clarifying tank 18 is connected with a black water outlet K of a filtering plant.
The high-temperature hot water tower 1 adopts a tower plate type internal part, flash steam at the lower section enters the upper section through an ascending pipe to directly exchange heat with water, and the operating pressure of the high-temperature hot water tower 1 is 0.7-1.0 MPa.
And a byproduct of 0.4-0.6MPa steam is produced in the shell pass of the waste boiler 2.
The primary cooler 3 adopts a shell-and-tube heat exchanger, and the temperature of a low-temperature hot water outlet C is 60-95 ℃.
The first-stage separator 8 adopts a gravity type gas-liquid separator with a demister, and the operating pressure is 0.65-0.85 MPa.
The operation pressure of the secondary flash tank 4 is 0.3-0.5MPa, and the tower top temperature is 115-145 ℃.
The secondary cooler 7 adopts a shell-and-tube heat exchanger, and the temperature of a low-temperature hot water outlet C is 60-95 ℃.
The second-stage separator 6 adopts a gravity type gas-liquid separator with a demister, and the operating pressure is 0.27-0.47 MPa;
the three-stage flash evaporation system 5 adopts a first three-stage flash evaporation tank 51 and a second three-stage flash evaporation tank 52 which are connected in series and are arranged up and down, and the operating pressure is 0.07-0.09 MPa.
The first three-stage flash tank 51 and the second three-stage flash tank 52 connected in series share a set of vacuum pumping system.
The three-stage cooler adopts a shell-and-tube heat exchanger and can heat desalted water to 60-70 ℃.
The three-stage separator adopts a gravity type gas-liquid separator with a demister, pressure control is respectively arranged on outlet pipelines at the top of the separator, and the operating pressure is 0.07-0.09 MPa.
The stripping tower 12 adopts a plate-type tower internal part, and the operating pressure is 0.2-0.3 MPa.
The tower top cooler 10 adopts a shell-and-tube heat exchanger, and the temperature of a low-temperature hot water outlet C is 60-95 ℃.
The liquid-phase feeding of the deaerator 9 is desalted water, and the operating pressure is 0.12-0.4 MPa.
The specific operation process comprises the following steps:
high-pressure black water from a black water inlet D of the gasification furnace and a black water inlet E of the washing tower is decompressed by an angle valve and enters the lower section of the high-temperature hot water tower 1 to be flashed, the flash steam directly exchanges heat with grey water, low-temperature conversion condensate and tower bottom liquid of the stripping tower 12 at the upper section of the high-temperature hot water tower 1, and hot water flows out from a hot water outlet C after being pressurized and returns to the washing tower to be used for removing dust of synthesis gas.
The flash steam at the top of the upper section of the high-temperature hot water tower 1 passes through the waste boiler 2 (waste heat boiler) to form a byproduct of low-pressure steam which is used as a heat source of the deaerator 9 and the stripping tower 12.
The non-condensable gas/condensate from the waste boiler 2 enters a primary cooler 3 to heat low-temperature hot water from a boundary area, and low-level heat is further recovered. The non-condensable gas/condensate from the primary cooler 3 enters a primary separator 8, the gas phase separated by the primary separator 8 enters the bottom of a stripping tower 12, and the liquid phase enters the top of the stripping tower 12.
The black water at the lower section of the high-temperature hot water tower 1 enters a secondary flash tank 4, the flash steam at the top of the secondary flash tank 4 heats the low-temperature hot water from the boundary region through a secondary cooler 7, and the low-level heat is recovered. The non-condensable gas/condensate from the secondary cooler 7 enters the secondary separator 6, the gas phase separated by the secondary separator 6 enters the bottom of the stripping tower 12, and the liquid phase enters the top of the stripping tower 12.
The condensate of the first-stage separator 8 and the condensate of the second-stage separator 6 enter the top of a stripping tower 12, the flash steam of the first-stage separator 8 and the flash steam of the second-stage separator 6 enter the bottom of the stripping tower 12, and the low-pressure steam by-product of the waste boiler 2 is used as a stripping heat source.
The liquid phase at the bottom of the stripping tower 12 returns to the high-temperature hot water tower 1 for heating. The stripping gas at the top of the stripping tower 12 enters the tower top separator 11 after being heated by the tower top cooler 10 to recover heat by low-temperature hot water in a boundary region, the separated gas phase is sent out of the boundary region for treatment, and the liquid phase flows back to the stripping tower 12.
The black water from the bottom of the second-level flash tank 4 enters a first third-level flash tank 51, the flash steam at the top of the first third-level flash tank 51 is heated by a first third-level cooler 13 and enters a boundary region for desalinization, and low-level heat is recovered; the non-condensable gas/condensate from the first three-stage cooler 13 enters a first three-stage separator 14, the gas phase separated by the first three-stage separator 14 is discharged to the atmosphere through a liquid ring vacuum pump outlet, and the liquid phase enters a condensate tank 17 and is pressurized by a pump and sent to an ash water tank 19.
The liquid phase at the bottom of the first three-stage flash tank 51 enters a second three-stage flash tank 52, and the liquid phase at the bottom of the second three-stage flash tank is pressurized and sent to the clarifying tank 18 by a pump. The flash steam at the top of the second three-stage flash tank 52 is heated by a second three-stage cooler 15 to enter a boundary region for desalting water, and low-level heat is recovered; the non-condensable gas/condensate from the second three-stage cooler 15 enters a second three-stage separator 16, the gas phase separated by the second three-stage separator 16 is discharged to the atmosphere through a liquid ring vacuum pump outlet, and the liquid phase enters a condensate tank 17 and is pressurized by a pump and sent to an ash water tank 19.
The desalted water heated by the first three-stage cooler 13 and the second three-stage cooler 15 enters the deaerator 9, part of the deaerated water is used as water supplement of the process system, and part of the deaerated water is used for the waste boiler 2 to produce low-pressure steam as a byproduct.
Clear water on the upper part of the clarifying tank 18 enters an ash water tank 19 through overflow, and black water containing solids on the lower part is pressurized and sent to a filtering plant through a pump.
One part of the grey water in the grey water tank 19 returns to the high-temperature hot water tower 1 for heating and recycling by the system, and the other part of the grey water is used as discharged wastewater and is sent to sewage treatment;
example 1
6.5MPa of coal water slurry is gasified in a certain factory, the daily coal input amount of a single furnace of the gasification furnace is 3000t, and the gasification furnace is the maximum coal water slurry furnace type in the current operation. The amount of gasified black water discharged to the flash evaporation system is 380t/h, and the amount of grey water returned to the system is 380t/h by using the traditional coal gasification black water flash evaporation process.
When the flash system is optimized to be the coal gasification black water treatment system, the steam used in the stripping tower 12 can be self-sufficient in the system, and the surplus of 3.0t/h is sent to the deaerator 9 in the device.
The temperature of desalted water entering the device can be heated to 70 ℃, and then the desalted water is sent to the deaerator 9, and steam consumption is saved by 60% compared with the condition that the desalted water at 30 ℃ directly enters the deaerator 9 to be deaerated.
The desalted water of the thermoelectric device is heated by the waste heat of the flash steam, so that the consumption of the steam of the thermoelectric device and the circulating water of a flash evaporation system is saved, and the running cost of the device can be saved by 1350 ten thousand yuan per year.
Example 2
6.5MPa of coal water slurry is gasified in a certain factory, the daily coal input amount of a single furnace of the gasification furnace is 3000t, and the gasification furnace is the maximum coal water slurry furnace type in the current operation. By using the traditional coal gasification black water flash evaporation process, high flash steam is directly sent to a conversion device stripping tower 12 to be used as a stripping heat source, low flash steam, grey water and low-temperature conversion condensate are deoxidized in a deaerator 9, and the system mainly has the following problems:
(1) the shift unit stripping tower 12 is often operated in an overload state, the acid gas component at the tower top is too high, the corrosion is serious, the stripping effect is poor, the content of the condensed liquid ammonia in the process of returning to gasification is high, the scale of a gasification process water pipeline and a valve is easy to scale, and the device needs to be stopped for descaling when the content is serious;
(2) the deaerator 9 has poor operation condition, the deaerator head is easy to scale, and in severe cases, the deaerator head internal part and the water outlet are all blocked, and the deaerator head needs to be stopped and descaled periodically.
After the treatment process is replaced by the coal gasification black water treatment system, the deaerator 9 has no blockage, the stripping tower 12 has stable operation, the gasification water quality is obviously improved, the overhaul period is prolonged, and the descaling workload is greatly reduced.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and should not be taken as limiting the invention, so that any modifications, equivalents, improvements and the like, which are within the spirit and principle of the present invention, should be included in the scope of the present invention.
Claims (10)
1. A coal gasification black water treatment system is characterized in that: including high temperature hot water tower (1), second grade flash tank (4) that connect gradually, the gaseous phase export of high temperature hot water tower (1) is connected with strip tower (12) after passing through first order cooler (3), first order separator (8) in proper order, the gaseous phase export of second grade flash tank (4) pass through second order cooler (7), second grade separator (6) in proper order after with strip tower (12) are connected.
2. The coal gasification black water treatment system according to claim 1, wherein: the gas phase outlets of the first-stage separator (8) and the second-stage separator (6) are connected with the gas phase inlet of the stripping tower (12), and the liquid phase outlets of the first-stage separator (8) and the second-stage separator (6) are connected with the liquid phase inlet of the stripping tower (12).
3. The coal gasification black water treatment system according to claim 1, wherein: and the primary cooler (3) and the secondary cooler (7) are connected with a hot water supply inlet (HWS) and a hot water return outlet (HWR) of the thermal power station.
4. The coal gasification black water treatment system according to claim 1, wherein: the liquid phase outlet of the stripping tower (12) is connected with the upper part of the high-temperature hot water tower (1), the top of the stripping tower (12) is sequentially connected with a tower top cooler (10) and a tower top separator (11), the liquid phase outlet of the tower top separator (11) is connected with the upper part of the stripping tower (12), and the gas phase outlet of the tower top separator (11) is connected with a stripping gas outlet (I).
5. The coal gasification black water treatment system according to claim 1, wherein: the lower part of the high-temperature hot water tower (1) is connected with a gasification furnace black water inlet (D) and a washing tower black water inlet (E), a liquid phase outlet of the high-temperature hot water tower (1) is connected with a hot water outlet (C), and the upper part of the high-temperature hot water tower (1) is connected with a conversion condensate inlet (B).
6. The coal gasification black water treatment system according to claim 1, wherein: the three-stage flash evaporation system (5) comprises a first three-stage flash evaporation tank (51) and a second three-stage flash evaporation tank (52) which are connected in series, the first three-stage flash evaporation tank (51) is connected with a liquid phase outlet of the second-stage flash evaporation tank (4), a liquid phase outlet of the first three-stage flash evaporation tank (51) is connected with the second three-stage flash evaporation tank (52), and a liquid phase outlet of the second three-stage flash evaporation tank (52) is connected with a black water outlet (G).
7. The coal gasification black water treatment system according to claim 6, wherein: the vacuum degrees of the first three-stage flash tank (51) and the second three-stage flash tank (52) are different.
8. The coal gasification black water treatment system according to claim 6, wherein: the gas phase outlet of the first three-level flash tank (51) is sequentially connected with a first three-level cooler (13) and a first three-level separator (14), the gas phase outlet of the second three-level flash tank (52) is sequentially connected with a second three-level cooler (15) and a second three-level separator (16), the gas phase outlet of the first three-level separator (14) and the gas phase outlet of the second three-level separator (16) are both connected with a vent gas port (H), and the liquid phase outlet of the first three-level separator (14) and the liquid phase outlet of the second three-level separator (16) are both connected with a condensate tank (17).
9. The coal gasification black water treatment system according to claim 6, wherein: the cold water inlets of the first three-stage cooler (13) and the second three-stage cooler (15) are connected with a desalted water inlet (M), the cold water outlets of the first three-stage cooler (13) and the second three-stage cooler (15) are connected with a deaerator (9), the liquid phase outlet of the deaerator (9) is connected with a waste boiler (2), the steam outlet of the waste boiler (2) is connected with the deaerator (9) and a stripping tower (12), and the waste boiler (2) is further connected with a high-temperature hot water tower (1) and a primary cooler (3).
10. The coal gasification black water processing system according to claim 8, wherein: the condensate tank (17) is connected with the ash water tank (19), the ash water tank (19) is further connected with the clarifying tank (18), a liquid phase outlet of the ash water tank (19) is connected with the ash water outlet (A) and the upper part of the high-temperature hot water tower (1), the clarifying tank (18) is connected with the black water inlet (L), the black water inlet (L) is connected with the black water outlet (G), and the bottom of the clarifying tank (18) is connected with the black water filtering plant outlet (K).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011008460.0A CN112125365A (en) | 2020-09-23 | 2020-09-23 | Coal gasification black water treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011008460.0A CN112125365A (en) | 2020-09-23 | 2020-09-23 | Coal gasification black water treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112125365A true CN112125365A (en) | 2020-12-25 |
Family
ID=73841203
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011008460.0A Pending CN112125365A (en) | 2020-09-23 | 2020-09-23 | Coal gasification black water treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112125365A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113060785A (en) * | 2021-03-17 | 2021-07-02 | 宁夏神耀科技有限责任公司 | Coal gasification flash distillation device and coal gasification flash distillation process |
| CN113387501A (en) * | 2021-07-08 | 2021-09-14 | 宁夏神耀科技有限责任公司 | Solid-black-containing water treatment and recycling device and method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201309840Y (en) * | 2008-12-05 | 2009-09-16 | 上海九元石油化工有限公司 | Improved stripping tower bottom purified water heat-exchange system of sewage stripping device |
| US20110209407A1 (en) * | 2010-02-26 | 2011-09-01 | General Electric Company | Heat recovery in black water flash systems |
| CN105561616A (en) * | 2016-02-04 | 2016-05-11 | 河南心连心化肥有限公司 | Gasification ash water low-pressure flash heat energy utilizing device and heat energy utilizing method thereof |
| CN107158891A (en) * | 2017-05-22 | 2017-09-15 | 中国成达工程有限公司 | A kind of coal gasified black water flashed vapour utilizes technique |
| CN207627955U (en) * | 2017-11-22 | 2018-07-20 | 科林未来能源技术(北京)有限公司 | A kind of gasification black water flash system |
| CN208121048U (en) * | 2018-02-28 | 2018-11-20 | 国家能源投资集团有限责任公司 | A kind of gasification system |
-
2020
- 2020-09-23 CN CN202011008460.0A patent/CN112125365A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201309840Y (en) * | 2008-12-05 | 2009-09-16 | 上海九元石油化工有限公司 | Improved stripping tower bottom purified water heat-exchange system of sewage stripping device |
| US20110209407A1 (en) * | 2010-02-26 | 2011-09-01 | General Electric Company | Heat recovery in black water flash systems |
| CN105561616A (en) * | 2016-02-04 | 2016-05-11 | 河南心连心化肥有限公司 | Gasification ash water low-pressure flash heat energy utilizing device and heat energy utilizing method thereof |
| CN107158891A (en) * | 2017-05-22 | 2017-09-15 | 中国成达工程有限公司 | A kind of coal gasified black water flashed vapour utilizes technique |
| CN207627955U (en) * | 2017-11-22 | 2018-07-20 | 科林未来能源技术(北京)有限公司 | A kind of gasification black water flash system |
| CN208121048U (en) * | 2018-02-28 | 2018-11-20 | 国家能源投资集团有限责任公司 | A kind of gasification system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113060785A (en) * | 2021-03-17 | 2021-07-02 | 宁夏神耀科技有限责任公司 | Coal gasification flash distillation device and coal gasification flash distillation process |
| CN113387501A (en) * | 2021-07-08 | 2021-09-14 | 宁夏神耀科技有限责任公司 | Solid-black-containing water treatment and recycling device and method |
| CN113387501B (en) * | 2021-07-08 | 2022-11-15 | 宁夏神耀科技有限责任公司 | Solid-black-containing water treatment and recycling device and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP2264287B1 (en) | Energy generating method using thermal cycles with high-pressure and moderate-temperature steam | |
| CN101157442B (en) | Waste heat reclaiming process for CO transformation | |
| CN107399870B (en) | Texaco gasifier black water heat recovery processing system | |
| CN112125365A (en) | Coal gasification black water treatment system | |
| CN110877919A (en) | Coal gasification black water heat recovery method and device | |
| CN106587233A (en) | Comprehensive utilization method for coal chemical industry gasified black water high-temperature flashing steam | |
| CN214114973U (en) | CO conversion condensate refining process system | |
| US7827792B2 (en) | Refrigerant cooled main steam condenser binary cycle | |
| CN105481646A (en) | Refrigeration method for methanol synthesis and separation | |
| CN102107119B (en) | Multiple-effect membrane distillation device and method | |
| CN102502703B (en) | Ammonia distillation method for waste heat of coke-oven flue gas | |
| CN204917951U (en) | Get rid of CO's in raw gas isothermal conversion systems | |
| CN102199453A (en) | Improved Lurgi gasification furnace waste heat recovering method and device | |
| CN112107875B (en) | Flash evaporation steam stripping cooling system and black water treatment process using same | |
| CN212151675U (en) | Coal gasification black water heat recovery device | |
| CN102587884A (en) | Utilizing process for underground gasified gas condensate | |
| CN201545718U (en) | Urea process condensed fluid treatment device | |
| CN108868932B (en) | Low-temperature waste heat power generation device | |
| CN217808778U (en) | Energy-saving cold hydrogenation product purification system in production of polycrystalline silicon by GCL method | |
| US3436911A (en) | Apparatus for combined gas-steam-ammonia cycle | |
| CN213823486U (en) | Flash evaporation stripping cooling system | |
| CN106362428A (en) | Steam stripping method of low temperature shift process condensate | |
| CN201545757U (en) | Residual ammonia water treatment device in coking process | |
| CN2415821Y (en) | Eddy degassing liquid | |
| CN220552300U (en) | Steam condensate heat energy recovery system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Yang Lijian Inventor after: Gao Zhihui Inventor after: Liu Shengkai Inventor after: Shi Haochun Inventor after: Wang Yishu Inventor after: Xu Jun Inventor before: Yang Lijian Inventor before: Gao Zhihui Inventor before: Liu Shengkai Inventor before: Shi Haochun Inventor before: Wang Yishu Inventor before: Xu Jun |
|
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20201225 |