CN1321729A - Heat recovery method of slag-containing waste water from gas production equipment by using hydrocarbon as raw material - Google Patents
Heat recovery method of slag-containing waste water from gas production equipment by using hydrocarbon as raw material Download PDFInfo
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Abstract
The present invention relates to a heat recovery method of dreggy waste water produced in gas production equipment by using hydrocarbon as raw material through gasification of gas fluidized bed, and is characterized by that it is a multicolumn dreggy waste water treatment system in which the dreggy waste water can be evaporated under the condition of multi-stqage pressure, the steam condensation can be used as heat source to directly heat purified water and the several processes of evaporatio, discharging dregs and directly-heating purified water are integrated into one body so as to effectively overcome the defects of scaling and plugging of heat exchanger for indirectly heating purified water by using steam.
Description
The present invention relates to a kind of heat recovery method, being specifically related to coal, refinery coke, biomass, flammable trade waste etc. is the heat recovery method of slag inclusion waste water in the unstripped gas fluidized bed production course of gas.
With the hydrocarbon-containiproducts in the unstripped gas fluidized bed production course of gas (as the contriver in the disclosed technology of Chinese patent " multi-nozzle opposed type coal water slurry or dry coal dust gasification furnace and application thereof " patent No. ZL98110616.1), the coal gas of producing need purify, coal gas rough purification system will produce a large amount of slag inclusion waste water, solids concn is about 0.1～8.0% (wt) in the water, its temperature is about 180～280 ℃, pressure is about 2.0～10.0MPa, and this water is also referred to as Heisui River.In order to save water resources and to reduce discharging, slag inclusion waste water should recycle.This just need isolate solid particulate from slag inclusion waste water, and removes sour gas and incoagulability gas, thereby guarantees the material balance in the slag inclusion waste water, could satisfy the requirement that recycles.
Because the restriction of water technology (flocculation agent heatproof) after slag inclusion waste water has only cooling, just can be removed lime-ash, realize purifying.Therefore the key of slag inclusion wastewater treatment is recovery of heat, how the energy that discharges in the slag inclusion waste water temperature-fall period is returned to purifying waste water of recycling to greatest extent high-qualityly, the normal operation that this is related to the energy-conservation of gasifying process and comprises the whole production technology of gasifying process.
Texaco Development Corporation applies for a patent (application number 94117093.4, publication number CN1104991A) and discloses a kind of blackwater fever recovery method by two-stage or three grades of flash distillations and flash steam and circulation buck indirect heat exchange in China.Practice shows that this method exists significantly not enough: (1) buck through indirect heat exchanger fouling takes place easily, causes heat exchange efficiency to descend, and causes flashing pressure to be difficult to control; (2) flash steam indirect heating buck, because the restriction of the indirect heat transfer temperature difference, the grey water temp that finally advances washing section and chill zone is not high enough, causes steam to utilize fully, is difficult to satisfy gas to steam ratio in the required coal gas of follow-up workshop section; (3) flash steam easily is with Heisui River, influences ordinary production; (4) the flasher bottom discharge has the hidden danger of obstruction; (5) flasher and interchanger are separated, and equipment is many, the flow process complexity.
Therefore, relevant branch of industry presses for a kind of new succinct slag inclusion waste water heat recovery method of flow process, and to reach circularly purifying water temp level height, slag inclusion waste water heat recovery efficiency height prevents fouling, prolongs the purpose of work period.
The heat recovery method that the purpose of this invention is to provide a kind of new slag inclusion waste water overcomes the defective of prior art, satisfies the needs of relevant department.
Realize the technical scheme of the object of the invention:
Described method comprises the steps:
The slag inclusion waste water decompression back that coal gas rough purification system produces imports hot-water tower, make steam turn to steam, and direct and the required direct contact heat-exchanging of purifying waste water that recycles of coal gas rough purification system, making purifies waste water is farthest heated up, and slag inclusion waste water is lowered the temperature, solid content increases.Direct heat exchange can be carried out in packing tower, tray column or other towers.Directly the contact heat-exchanging mode make purify waste water and steam between the temperature difference reach minimum, therefore the temperature levels of purifying waste water that recycles is improved, and the heat recovery efficiency of slag inclusion waste water is higher.Purifying waste water after temperature raises can be sent to coal gas rough purification systemic circulation and use.The part steam of hot-water tower can import the outer deoxygenator that supplies water, and provides the deoxygenator deoxygenation needed heat; Part steam can be used as the thermal source of deaerated water elevated temperature.The slag inclusion waste water that hot-water tower is sent can import the terminal evaporative cooler, further to concentrate slag inclusion waste water, reduces the slag inclusion wastewater temperature.The steam that the terminal evaporative cooler is produced is sent into separator after condenser condenses, non-condensable gases and acid gas are through the vacuum pump emptying, and phlegma relies on potential energy to drain into the purification tank, has promptly saved condensate pump.Vacuum pump can be a water-ring vacuum pump, also can use vapor jet pump.The power steam of vapor jet pump can be provided by hot-water tower.
The slag inclusion waste water that terminal evaporative cooler bottom is further concentrated relies on potential energy to drain into cleaner, and forms fluid-tight by the liquid level of cleaner, has so just saved the slag inclusion waste water pump.Cleaner is by leaving standstill, and solid particulate and water is settlement separate in the dependence gravity realization slag inclusion waste water, and adds the isolating flocculation agent of promotion, as polyacrylamide.Spissated slag inclusion waste water is sent to filtering system, purifies waste water and is overflowed by the cleaner top, enters the purification tank, adds conventional dispersion agent as containing the multiple copolymer of sulfonic acid group, delaying the sedimentation fouling of purifying waste water, and is recycled toward hot-water tower by pumping.
Because coal gas rough purification system can produce the dissimilar slag inclusion waste water of multiply, preferably it is imported hot-water tower respectively.
According to the present invention, a plurality of hot-water towers can be set, slag inclusion waste water decompression back imports first hot-water tower, directly with the contact heat-exchanging of purifying waste water that comes from second hot-water tower, then slag inclusion waste water more further decompression back import second hot-water tower, further lower the temperature and vaporize, and directly and from the next contact heat-exchanging of purifying waste water of the 3rd hot-water tower, make from next the purifying waste water of the 3rd hot-water tower to obtain heating up, slag inclusion waste water is then by further cooling, solid content further increase.
By that analogy, a plurality of hot-water towers can be set, can be provided with 6 hot-water towers at most.Slag inclusion waste water is successively by a plurality of hot-water towers, and the reversed sequence of purifying waste water is passed through, and makes that slag inclusion waste water progressively reduces pressure, cooling, solid content increase, and circularly purifying water is progressively improved temperature, thereby heat is reclaimed to greatest extent.
Along with the tower number increase of hot-water tower, recovery of heat more becomes fully and is reasonable, but the facility investment increase, there is optimal selection problem in this.
According to the present invention, the cooling extent of slag inclusion waste water between a plurality of hot-water towers is 80～180 ℃.
In the preferred scheme of the present invention:
As adopt a hot-water tower, and its service temperature is 100～220 ℃, hot-water tower part steam can import outer water supply deoxygenator, provides the deoxygenator deoxygenation needed heat.
As adopt two hot-water towers, and then the service temperature of first hot-water tower is 120～220 ℃, the service temperature of second hot-water tower is 100～180 ℃.The first hot-water tower part steam can import the deaerated water interchanger, the heating deaerated water enters first separator then, isolated acid gas and the non-condensable gases torch that reduces internal heat, phlegma is delivered to second hot-water tower, and the deaerated water after the heating can be sent to coal gas rough purification system and use.The part steam of second hot-water tower can import outer water supply deoxygenator, provides the deoxygenator deoxygenation needed heat.
As adopt three hot-water towers, and then the service temperature of first hot-water tower is 140～220 ℃, and the service temperature of second hot-water tower is 120～180 ℃, and the service temperature of the 3rd hot-water tower is 100～160 ℃.
According to the present invention, the slag inclusion waste water that last hot-water tower is sent can import the terminal evaporative cooler, further to concentrate slag inclusion waste water, reduces the slag inclusion wastewater temperature.The steam that the terminal evaporative cooler is produced is sent into second separator after condenser condenses, non-condensable gases and acid gas are through the vacuum pump emptying, and phlegma relies on potential energy to drain into the purification tank.
The slag inclusion waste water that terminal evaporative cooler bottom is further concentrated relies on potential energy to drain into cleaner, purifies waste water and is overflowed by the cleaner top, enters the purification tank.
Can adopt indifferent gas gas to carry slag inclusion waste water, carry, make it cooling, enrichment, to replace terminal transpiration cooling as nitrogen gas.
The bottom of hot-water tower, terminal evaporative cooler adds less water by annular water controller, destroys lime-ash and builds bridge.
The advantage of the inventive method is: adopt hot-water tower, cast out flasher and indirect heat exchanger, flow process is succinct, circularly purifying water temp level height, and the heat recovery efficiency height has been eliminated the fouling of purifying waste water in the indirect heat exchanger and causing.
The present invention is further illustrated below in conjunction with accompanying drawing.
Fig. 1 is the schema with a hot-water tower.
Fig. 2 is the schema with two hot-water towers.
As seen from Figure 1, be that 180～280 ℃, pressure are 2.0～10.0MPa from coal gas preliminary purification system temperature Slag inclusion waste water import first hot-water tower 1 after by inlet line 101 decompression. The operation of first hot-water tower 1 About 100～220 ℃ of temperature range, the about 0.1～2.4MPa of pressure limit, the steam that the tower bottom produces enters on the tower The direct heat exchange of purifying waste water that section and water circulating pump 13 are sent here, the gained steam temperature of temperature than direct heat transfer of purifying waste water Low about 0～8 ℃ of degree. Temperature raises purifies waste water on first hot-water tower, 1 top through the pipeline 102 of purifying waste water by only Go to coal gas preliminary purification system after changing water pump 103 pressurizations.
First hot-water tower, 1 top part steam advances the oxygen-eliminating device 7 of outer water supply through first steam pipe line 104, Make heat source, acid gas and the incoagulable gas torch (not indicating on the figure) that reduces internal heat.
A small amount of water of clarified water pump 103 outlets can be by the first annular water controller 107 of first hot-water tower, 1 bottom Enter first hot-water tower 1, destroy lime-ash and build bridge, stagnant dirty slag is discharged by first hot-water tower, 1 bottom.
Slag inclusion waste water after lowering the temperature, concentrating imports terminal devaporizer 3 by first hot-water tower, 1 bottom. Eventually The steam that end devaporizer 3 produces is sent into second separator 6 after condenser 9 condensations, isolated Condensate liquid relies on potential energy to enter purification water tank 5 through second condensate line 601, and incoagulable gas and acid gas are through true Empty pump 15 is emptying. Vavuum pump 15 can be water-ring vacuum pump, also can use steam jet pump. The steam spray The power steam of penetrating pump can be provided by hot-water tower. A small amount of water of clarified water pump 103 outlets can evaporate by terminal The 3rd annular water controller 307 of cooler 3 bottoms enters terminal devaporizer 3, destroys lime-ash and builds bridge.
About 0.02～the 0.07MPa of terminal devaporizer 3 operating pressures, concentrated slag inclusion wastewater temperature about 60～90 ℃, rely on potential energy to drain into clarifier 4 by terminal devaporizer 3 bottoms, clarifier 4 is by leaving standstill dependence The sedimentation separation of solid particle and water in the gravity realization slag inclusion waste water, and add the flocculant that promotes separation, dense The slag inclusion waste water of contracting is sent to follow-up filtration system, and purifying waste water is spilled over to purification water tank 5 by clarifier 4 tops.
Purifying waste water of purification water tank 5 recycles by water circulating pump 13 after routine is processed.
As seen from Figure 2, be that 180～280 ℃, pressure are 2.0～10.0MPa from coal gas preliminary purification system temperature Slag inclusion waste water import first hot-water tower 1 after by inlet line 101 decompression. The operation of first hot-water tower 1 About 120～220 ℃ of temperature range, the about 0.2～2.4MPa of pressure limit, the steam that the tower bottom produces enters on the tower The circularly purifying water direct heat-exchange of section and second hot-water tower 2 further improves the temperature of this circularly purifying water, Gained is purified waste water temperature than low about 0～8 ℃ of the vapor (steam) temperature of direct heat transfer. What temperature raise purifies waste water first Coal gas preliminary purification system is gone in hot-water tower 1 top after the pipeline 102 of purifying waste water is by clarified water pump 103 pressurizations.
First hot-water tower, 1 top part steam advances deaerated water heat exchanger 8 through first steam pipe line 104, Connect the deaerated water that heat pump 14 is sent here, enter then first separator 10 and separate, isolated acid gas and not The solidifying property gas torch (not indicating on the figure) that reduces internal heat, condensate liquid is sent second hot-water tower 2 back to by first condensate line 105. The deaerated water that the gained temperature raises goes to coal gas preliminary purification system.
A small amount of water of clarified water pump 103 outlets can be by the first annular water controller 107 of first hot-water tower, 1 bottom Enter first hot-water tower 1, destroy lime-ash and build bridge, stagnant dirty slag is discharged by first hot-water tower, 1 bottom.
Cooling, the slag inclusion waste water after concentrating import second hot-water tower 2 after by first hot-water tower, 1 bottom pressure relief. About 100～180 ℃ of the operating temperature range of second hot-water tower 2, the about 0.1～1.0MPa of pressure limit. The tower bottom Produce steam, enter the direct heat exchange of purifying waste water that tower top and water circulating pump 13 are sent here, the gained temperature of purifying waste water Vapor (steam) temperature than direct heat transfer is hanged down about 0～8 ℃. What temperature raise purifies waste water on the top of second hot-water tower 2 By the top that enters first hot-water tower 1 after force (forcing) pump 12 pressurizations. The excess steam of second hot-water tower 2 is through Two steam pipe lines 201 enter the oxygen-eliminating device 7 of outer water supply and do heating steam, acid gas and the incoagulability body gas torch that reduces internal heat (not indicating on the figure). A small amount of water of force (forcing) pump 12 outlets adds second hot water by the second annular water controller 207 The bottom of tower 2 is destroyed lime-ash and is built bridge, and stagnant dirty slag is discharged by second hot-water tower, 2 bottoms.
The slag inclusion waste water of further being lowered the temperature and concentrating is sent into the terminal devaporizer by second hot-water tower, 2 bottoms 3. The steam that terminal devaporizer 3 produces is sent into second separator 6 after condenser 9 condensations, separate The condensate liquid that goes out relies on potential energy to enter purification water tank 5, incoagulable gas and acid gas through second condensate line 601 Emptying through vavuum pump 15. Vavuum pump 15 can be water-ring vacuum pump, also can use steam jet pump. Steam The power steam of vapour jet pump can be provided by hot-water tower. A small amount of water of water circulating pump 13 outlets can steam by terminal The 3rd annular water controller 307 of sending out cooler 3 bottoms adds the bottom of terminal devaporizer 3, destroys ash Slag is built bridge.
About 0.02～the 0.07MPa of terminal devaporizer 3 operating pressures, concentrated slag inclusion wastewater temperature about 60～90 ℃, rely on potential energy to drain into clarifier 4 by terminal devaporizer 3 bottoms, clarifier 4 is by leaving standstill dependence The sedimentation separation of solid particle and water in the gravity realization slag inclusion waste water, and add the flocculant that promotes separation, dense The slag inclusion waste water of contracting is sent to follow-up filtration system, and purifying waste water is spilled over to purification water tank 5 by clarifier 4 tops.
Purifying waste water of purification water tank 5 recycles by water circulating pump 13 after routine is processed.
In the situation that does not break away from design of the present invention and essential characteristic, the present invention can carry out some improve and Change, these also belong to claim scope of the present invention.
One day was handled the coal water slurry gasification device of 1000 tons of coals, and vapor pressure is 6.5MPa, and gasification temperature is 1280 ℃.One slag inclusion wastewater flow that goes out coal gas rough purification system is 120m
3/ h, solids concn 2% (wt) in the slag inclusion waste water, temperature is 245 ℃, is provided with two filler hot-water towers.
The service temperature of first hot-water tower 1 is 170 ℃, and working pressure is 0.79MPa; The service temperature of second hot-water tower 2 is 120 ℃, and working pressure is 0.20MPa; The service temperature of terminal evaporative cooler 3 is 80 ℃, and working pressure is 0.047MPa; The temperature of purifying waste water of advancing second hot-water tower 2 is 79 ℃, and flow is 65m
3/ h; Going out first hot-water tower, to go the temperature of purifying waste water of coal gas rough purification system be 168 ℃.
The about 9t/h of steam that first hot-water tower, 1 top has not utilized advances deaerated water interchanger 8 indirect heating deaerated water, makes its temperature be increased to 160 ℃, is sent to coal gas rough purification system then.
The slag inclusion waste water of first hot-water tower, 1 bottom is 100m
3/ h, solids concn 2.4% (wt) in the slag inclusion waste water, temperature is 170 ℃, is sent to second hot-water tower 2.
The about 4t/h of steam that second hot-water tower 2 has not utilized enters the outer deoxygenator 7 that supplies water, and does heating steam.
The slag inclusion waste water of second hot-water tower, 2 bottoms is 88m
3/ h, solids concn 2.7% (wt) in the slag inclusion waste water, temperature is 120 ℃, is sent to terminal evaporative cooler 3.The temperature of purifying waste water that goes out second hot-water tower 2 is 117 ℃.
The concentrated slag inclusion waste water that goes out the terminal evaporative cooler is 80m
3/ h, temperature is 80 ℃, relies on potential energy to drain into cleaner 4 by terminal evaporative cooler 3 bottoms.
Claims (10)
1. a hydrocarbon polymer is the slag inclusion waste water heat recovery method in the raw material gas producing device, it is characterized in that described method comprises the steps:
Slag inclusion waste water decompression back imports hot-water tower, make steam turn to steam, and with the direct contact heat-exchanging of purifying waste water, coal gas rough purification system is sent in purifying waste water after temperature raises, the slag inclusion waste water that hot-water tower is sent imports terminal evaporative cooler (3), the steam that terminal evaporative cooler (3) is produced is sent into second separator (6) after condenser (9) condensation, non-condensable gases and acid gas are through vacuum pump (15) emptying, phlegma drains into and purifies tank (5), the slag inclusion waste water that terminal evaporative cooler (3) bottom is concentrated drains into cleaner (4), carry out settlement separate, spissated slag inclusion waste water is sent to filtering system, purifying waste water enters purification tank (5) by cleaner (4) top, and is sent to hot-water tower by recycle pump (13).
2. the method for claim 1 is characterized in that, the hot-water tower more than 1 can be set, and by each hot-water tower, pass through successively by the reversed sequence of purifying waste water for slag inclusion waste water.
3. method as claimed in claim 2, it is characterized in that, a hot-water tower is set, slag inclusion waste water imports first hot-water tower (1) by inlet line (101) decompression back, its operating temperature range is 100～220 ℃, the steam that the tower bottom produces enters the direct heat exchange of purifying waste water that tower top and water circulating pump (13) are sent here, and purifying waste water of temperature rising gone to coal gas rough purification system on first hot-water tower (1) top through the pipeline of purifying waste water (102);
First hot-water tower (1) top part steam, the deoxygenator (7) that outside first vapour line (104) advances, supplies water;
Terminal evaporative cooler (3) working pressure is 0.02～0.07MPa.
4. method as claimed in claim 2, it is characterized in that, two hot-water towers are set, slag inclusion waste water imports first hot-water tower (1) by inlet line (101) decompression back, the service temperature of first hot-water tower (1) is 120～220 ℃, the steam that the tower bottom produces enters tower top and the next direct heat exchange of purifying waste water of second hot-water tower (2), and purifying waste water that temperature raises gone to coal gas rough purification system on first hot-water tower (1) top through the pipeline of purifying waste water (102);
First hot-water tower (1) top part steam, advance deaerated water interchanger (8) through first vapour line (104), enter first separator (10) then and separate, isolated acid gas and the non-condensable gases torch that reduces internal heat, phlegma is sent second hot-water tower (2) back to by first condensate line (105);
Cooling, the slag inclusion waste water after concentrating import second hot-water tower (2) after by first hot-water tower (1) bottom pressure relief, its service temperature is 100～180 ℃, the tower bottom produces steam, enter the direct heat exchange of purifying waste water that tower top and water circulating pump (13) are sent here, purifying waste water that temperature raises enters the top of first hot-water tower (1) after being pressurizeed by force (forcing) pump (12) in the top of second hot-water tower (2), the excess steam of second hot-water tower (2), the deoxygenator (7) that outside second vapour line (201) enters, supplies water, acid gas and the non-condensable gases torch that reduces internal heat;
Terminal evaporative cooler (3) working pressure is 0.02～0.07MPa.
5. method as claimed in claim 2 is characterized in that, adopts three hot-water towers, and the service temperature of first hot-water tower is 140～220 ℃, and the service temperature of second hot-water tower is 120～180 ℃, and the service temperature of the 3rd hot-water tower is 100～160 ℃.
6. as the arbitrary described method of claim 1～5, it is characterized in that vacuum pump (15) is water-ring vacuum pump or vapor jet pump, the power steam of vapor jet pump can be provided by hot-water tower.
7. as the arbitrary described method of claim 1～5, it is characterized in that, carry slag inclusion waste water to replace terminal transpiration cooling with indifferent gas gas.
8. as the arbitrary described method of claim 1～5, it is characterized in that the bottom of hot-water tower, terminal evaporative cooler (3) adds by annular water controller destroys the less water that lime-ash is built bridge.
9. as the arbitrary described method of claim 1～5, it is characterized in that multiply slag inclusion waste water imports hot-water tower respectively.
10. method as claimed in claim 2 is characterized in that, the cooling extent of slag inclusion waste water between a plurality of hot-water towers is 80～180 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011127015A CN1214091C (en) | 2001-04-24 | 2001-04-24 | Heat recovery method of slag-containing waste water from gas production equipment by using hydrocarbon as raw material |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011127015A CN1214091C (en) | 2001-04-24 | 2001-04-24 | Heat recovery method of slag-containing waste water from gas production equipment by using hydrocarbon as raw material |
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| Publication Number | Publication Date |
|---|---|
| CN1321729A true CN1321729A (en) | 2001-11-14 |
| CN1214091C CN1214091C (en) | 2005-08-10 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011127015A Expired - Lifetime CN1214091C (en) | 2001-04-24 | 2001-04-24 | Heat recovery method of slag-containing waste water from gas production equipment by using hydrocarbon as raw material |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101298569B (en) * | 2008-06-26 | 2011-05-11 | 华东理工大学 | Gasification method of shock chilling type pulp or powder carbonaceous material |
| CN102336496A (en) * | 2011-08-24 | 2012-02-01 | 中国五环工程有限公司 | Method for treating and recycling ash water in dry coal dust gasification device |
| CN102653689A (en) * | 2011-03-03 | 2012-09-05 | 刘红 | Undecomposed steam recycling process through pressurized moving bed coal gasification |
| CN102730809A (en) * | 2012-06-29 | 2012-10-17 | 江苏申久化纤有限公司 | Coal-combustion boiler ash-water recycling system and method |
| CN108061295A (en) * | 2017-07-14 | 2018-05-22 | 新能能源有限公司 | A kind of buck oxygen-eliminating device |
| US11827535B2 (en) | 2021-08-31 | 2023-11-28 | Air Products And Chemicals, Inc. | Integrated heat exchanger and sour water stripper |
-
2001
- 2001-04-24 CN CNB011127015A patent/CN1214091C/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101298569B (en) * | 2008-06-26 | 2011-05-11 | 华东理工大学 | Gasification method of shock chilling type pulp or powder carbonaceous material |
| CN102653689A (en) * | 2011-03-03 | 2012-09-05 | 刘红 | Undecomposed steam recycling process through pressurized moving bed coal gasification |
| CN102653689B (en) * | 2011-03-03 | 2015-11-25 | 李宁 | The undecomposed steam cycle of pressurization moving-bed gasification utilizes technique |
| CN102336496A (en) * | 2011-08-24 | 2012-02-01 | 中国五环工程有限公司 | Method for treating and recycling ash water in dry coal dust gasification device |
| CN102336496B (en) * | 2011-08-24 | 2013-02-27 | 中国五环工程有限公司 | Method for treating and recycling ash water in dry coal dust gasification device |
| CN102730809A (en) * | 2012-06-29 | 2012-10-17 | 江苏申久化纤有限公司 | Coal-combustion boiler ash-water recycling system and method |
| CN108061295A (en) * | 2017-07-14 | 2018-05-22 | 新能能源有限公司 | A kind of buck oxygen-eliminating device |
| US11827535B2 (en) | 2021-08-31 | 2023-11-28 | Air Products And Chemicals, Inc. | Integrated heat exchanger and sour water stripper |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1214091C (en) | 2005-08-10 |
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