CN103803668A - System for recovering residual heat of ammonia vapor on top of surplus ammonia water ammonia still - Google Patents
System for recovering residual heat of ammonia vapor on top of surplus ammonia water ammonia still Download PDFInfo
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- CN103803668A CN103803668A CN201410070540.7A CN201410070540A CN103803668A CN 103803668 A CN103803668 A CN 103803668A CN 201410070540 A CN201410070540 A CN 201410070540A CN 103803668 A CN103803668 A CN 103803668A
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Abstract
The invention discloses a system for recovering residual heat of ammonia vapor on the top of a surplus ammonia water ammonia still. The system comprises an ammonia still, a heat pump unit, a circulating hot water pump, a reboiler, a waste water pump and a gas-liquid separator, wherein the heat pump unit is an absorptive heat pump unit which comprises an evaporator end, an absorber end, a generator end and a condenser end. The heat pump unit is placed on the top of the ammonia still and is used for recycling latent heat of ammonia vapor on the top of the still to heat circulating hot water, the heated circulating hot water is used for heating ammonia distilling waste water at the bottom of the still through the reboiler to produce saturated vapor, and the saturated steam returns into the ammonia still to supply distillation energy and realize recycling of energy, so that the consumption of coal gas or vapor is lowered, and the utilization ratio of recovered residual heat is increased. The ammonia vapor is subjected to gas-liquid separation after recovery of the latent heat, and liquid-phase ammonia water returns into the ammonia still for serving as reflux liquid.
Description
Technical field
The present invention relates to residual coking ammonia water processing technology field, specifically a kind of remained ammonia ammonia still process tower top ammonia steam heat recovery system.
Background technology
Coal produces all higher remained ammonias of a certain amount of ammonia nitrogen, prussiate, sulfide, phenol and COD concentration in coking.Remained ammonia generally will pass through the treatment process such as oil removing, dephenolize, ammonia still process, phenol-cyanogen sewage.Ammonia still process is to remove ammonia, prussiate and the sulfide in remained ammonia by distillation, improves waste water quality, meets the requirement of phenol-cyanogen sewage treatment process, reclaims ammonia for desulfurization simultaneously or produces sulphur ammonium.Remained ammonia ammonia distillation process is divided into water vapor ammonia still process, thermal oil ammonia still process and tube furnace ammonia still process by type of heating; Can be divided into again normal pressure ammonia still process and negative pressure ammonia still process by working pressure, no matter which kind of remained ammonia ammonia distillation process tower top ammonia vapour is taken away the approximately 80-90% that distills thermal losses, and ammonia vapour need to be in ammonia still process dephlegmator with in warm water, condensing cooling is liq ammonia, middle warm water recycles after cooling rack is cooling, at the bottom of tower, provides distillation heat again take coal gas or steam as heat source.The ammonia steam thermal energy that ammonia still tower top is generated fails to carry out effective recycling, causes waste, has reduced energy utilization rate, and has increased process water consumption.
Summary of the invention
The object of the present invention is to provide a kind of remained ammonia ammonia still process tower top ammonia steam heat recovery system, be applied in ammonia steaming system by heat pump techniques, by replace former ammonia vapour dephlegmator by heat pump set, realize the abundant recovery of the ammonia steam latent heat that ammonia still tower top is generated, improve energy recovery utilization ratio, reduce the object of water consumption.
The present invention solves the technical scheme that its technical problem takes: a kind of remained ammonia ammonia still process tower top ammonia steam heat recovery system, comprises ammonia still, waste water pump and heat pump set; The distilled ammonia wastewater delivery port of ammonia still bottom is communicated with the input aperture of waste water pump, also comprises reboiler, circulating hot-water pump and gas-liquid separator;
The delivery port of described waste water pump is communicated with the distilled ammonia wastewater input aperture of reboiler bottom; Described heat pump set is absorption type heat pumping set, comprises evaporator end, resorber end, condenser end and producer end; The delivery port of described evaporator end is communicated with the input aperture I of described resorber end, and the delivery port of described resorber end is communicated with the input aperture of described producer end, and is serially connected with solution heat exchanger on this connecting path;
The delivery port I of described producer end is communicated with the input aperture of described condenser end; The delivery port of described condenser end is communicated with the input aperture of described evaporator end and is serially connected with cryogenic fluid pump on this connecting path; The delivery port II of described producer end is communicated with the input aperture II of described resorber end and is serially connected with solution heat exchanger on this connecting path; Described condenser end is communicated with cooling water source; The ammonia steam outlet at described ammonia still top is communicated with the ammonia vapor inlet port of described evaporator end by the first branch road, be communicated with the ammonia vapor inlet port of described producer end by the second branch road; The gas-liquid mixture delivery port of the gas-liquid mixture delivery port of described evaporator end and described producer end is communicated with respectively the input aperture of described gas-liquid separator; The liquid phase delivery port of described gas-liquid separator is communicated to ammonia still; The saturation steam delivery port at described reboiler top is communicated to ammonia still; After the heat exchange of described reboiler, circulating hot water delivery port is communicated with the input aperture of described circulating hot-water pump; The delivery port of described circulating hot-water pump is communicated with the hot water input aperture of described resorber end; The hot water output port of described resorber end is communicated with the front circulating hot water of the heat exchange input aperture of described reboiler.
Further, the gas phase delivery port on described gas-liquid separator is communicated with sulphur ammonium operation saturex or coal gas negative pressure end.
The present invention replaces now widely used ammonia still process dephlegmator by absorption heat pump set, heat pump set is positioned over ammonia still top, recycle tower top ammonia vapour latent heat for heating cycle hot water by heat pump set, circulating hot water after heating produces saturation steam by distilled ammonia wastewater at the bottom of reboiler heating tower again, saturation steam returns distillation heat is provided in ammonia still, realize the recycle of energy, thereby reduce coal gas or steam consumption, improve the utilization ratio of waste heat recovery, ammonia steam is recovered after latent heat through gas-liquid separation, liquid phase ammoniacal liquor returns in ammonia still as phegma, exhaust steam can be sent into sulphur ammonium operation saturex or enter coal gas system by negative pressure, there is following characteristics:
(I) carrys out heating cycle hot water by recycling ammonia still tower top ammonia steam latent heat, and heated circulating hot water heats the distilled ammonia wastewater at the bottom of ammonia still by reboiler, makes to become low-pressure saturated steam and returns and in ammonia still, continue to provide distillation heat; Then circulating hot water returns to heat pump set circulating-heating through pump pressurization, has realized the recirculation utilization of multi-faceted, the multi-stage type to ammonia still process tower top ammonia steam latent heat, improves the utilization ratio to ammonia steam latent heat;
(II) replaces former dephlegmator by heat pump set, by heat pump set, the part heat of ammonia steam passed to circulating hot water, reduced middle warm water consumption, thereby reduced water consumption;
(III) heat pump set is take heat recirculated water as carrier, and the distilled ammonia wastewater of vaporizing at the bottom of ammonia still by reboiler generates saturation steam and returns in ammonia still and continue to provide distillation thermal losses, does not increase waste water total amount;
(IV) ammonia steam latent heat is after being reclaimed by heat pump set, and through gas-liquid separator, liquid phase directly refluxes in ammonia still;
(V) this technique only replaces former dephlegmator at the very useful heat pump of ammonia still, increase gas-liquid separator, at the bottom of tower, increase reboiler and circulating hot-water pump, at the bottom of tower, waste water pump can utilize former ammonia steaming system waste water pump, only part waste water is caused to newly-increased reboiler, do not affect former ammonia still process main equipment, quantities is little, invests low;
(VI) this technique can be suitable for steam ammonia still process, thermal oil ammonia still process and tube furnace ammonia still process, and the extent of spreading amd application is wide.This system reform simultaneously, based on existing equipment, does not affect main equipment, and improvement expenses is low, has good economic benefit and social benefit.
Accompanying drawing explanation
Fig. 1 is syndeton schematic diagram of the present invention;
Fig. 2 is the syndeton schematic diagram of heat pump components in the present invention;
In figure: 1 ammonia still, 2 heat pump components, 21 evaporator end, 22 resorber ends, 23 producer ends, 24 condenser end, 25 cryogenic fluid pumps, 26 solution heat exchangers, 27 first branch roads, 28 second branch roads, 3 circulating hot-water pumps, 4 reboilers, 5 waste water pumps, 6 gas-liquid separators, 7 cooling water sources.
Embodiment
For ease of understanding technology contents of the present invention, below in conjunction with accompanying drawing, its technical scheme is described further.
As depicted in figs. 1 and 2, a kind of remained ammonia ammonia still process tower top ammonia steam heat recovery system, comprises ammonia still 1, heat pump set 2, circulating hot-water pump 3, reboiler 4, waste water pump 5 and gas-liquid separator 6.Described heat pump set 2 is (two classes) absorption type heat pumping set, comprises evaporator end 21, resorber end 22, producer end 23 and condenser end 24.
On ammonia still 1, there is remained ammonia input aperture and ammonia steam outlet, the bottom of ammonia still 1 has heating unit, by this heating unit, the remained ammonia of sending in ammonia still 1 is effectively evaporated, produce ammonia gas vapor and at the bottom of the tower of ammonia still 1, produce distilled ammonia wastewater simultaneously.Heat pump set 2 is common heat-energy recovering apparatus, conventionally utilize cryogen evaporation of water and condensation that the energy of its inner evaporator end 21 and condenser end 24 is carried, evaporator end 21 connects the weary gas of steam, middle temperature used heat and producer end 23 form driving heat source system, middle temperature used heat also forms heat source system with evaporator end 21, the above-mentioned explanation about ammonia still 1 and heat pump set 2 operation logics is prior art, repeats no more herein.
The distilled ammonia wastewater delivery port of ammonia still 1 bottom is communicated with the input aperture of waste water pump 5, and the delivery port of waste water pump 5 is communicated with the input aperture of reboiler 4 bottoms., and send in reboiler 4 the distilled ammonia wastewater sucking-off of ammonia still 1 bottom by waste water pump 5.The delivery port at reboiler 4 tops is communicated with ammonia still 1.The distilled ammonia wastewater of sending in reboiler 4 carries out energy exchange with the circulating hot water (superheated water) of being sent into by heat pump components 2, be saturation steam by distilled ammonia wastewater gasification, the saturation steam producing is admitted in ammonia still 1 by the delivery port at reboiler 4 tops, and distillation heat is provided.Described circulating hot-water pump 3, reboiler 4, waste water pump 5 threes have formed the core of waste heat recovery.
Concrete annexation between ammonia still 1, gas-liquid separator 6 and heat pump set 2 threes, and the concrete annexation of circulating hot-water pump 3 and reboiler 4 and heat pump set 2 is as follows.
The delivery port of the evaporator end 21 in heat pump set 2 is communicated with the input aperture I of resorber end 22, the delivery port of resorber end 22 is communicated with the input aperture of producer end 23, the delivery port I of producer end 23 is communicated with the input aperture of condenser end 24, the delivery port of condenser end 24 is communicated with the input aperture of evaporator end 21 and on connecting path, is serially connected with cryogenic fluid pump 25, and the delivery port II of producer end 23 is communicated with the input aperture II of resorber end 22 and on connecting path, is serially connected with solution heat exchanger 26.
Condenser end 24 in heat pump set 2 is communicated with cooling water source (being the heat pipe entrance and outlet communication loop water source of condenser end).
The ammonia steam outlet at ammonia still 1 top is communicated with the ammonia vapor inlet port of the evaporator end 21 in heat pump set 2 by the first branch road 27, be communicated with the ammonia vapor inlet port of the producer end 23 in heat pump set 2 by the second branch road 28.The gas-liquid mixture delivery port of evaporator end 21 and the gas-liquid mixture delivery port of producer end 23 are communicated with respectively the input aperture of gas-liquid separator 6.It should be noted that the ammonia vapor inlet port of described evaporator end 21 and entrance and the outlet of corresponding evaporator end heat transfer tube respectively of gas-liquid mixture delivery port; The ammonia vapor inlet port of described producer end 23 and entrance and the outlet of corresponding producer end heat transfer tube respectively of gas-liquid mixture delivery port.
The gas phase delivery port of described gas-liquid separator 6 is communicated with sulphur ammonium operation saturex or coal gas negative pressure end, and the liquid phase delivery port of gas-liquid separator 6 is communicated with ammonia still 1, liquid return is continued to participate in the process of ammonia still process generating steam to ammonia still 1.
The input aperture of circulating hot water delivery port communication loop hot water pump 3 after the heat exchange of described reboiler 4.The delivery port of circulating hot-water pump 3 is communicated with the hot water input aperture of the resorber end 22 in heat pump set 2.The hot water output port of resorber end 22 is communicated with the front circulating hot water of the heat exchange input aperture of reboiler 4.It should be noted that the hot water input aperture of described resorber end 22 and hot water output port's entrance and outlet of corresponding resorber end heat transfer tube respectively; Circulating hot water input aperture and entrance and the outlet of corresponding reboiler heat transfer tube respectively of circulating hot water delivery port after heat exchange before the heat exchange of described reboiler 4.
On each transfer line, be not so provided with the accessories such as various by-pass valve controls, power-driven pump and conventionally test element; as one of ordinary skilled in the art; completely can be as the case may be; the above-mentioned accessory that needs are used specifically arranges; for ease of explanation and understand improvement feature of the present invention; it the related content of this part is no longer elaborated, so can not form restriction to protection scope of the present invention.
Principle of work:
In the evaporator end 21 of described heat pump set 2, carry the cryogen of coming to be admitted to band evaporator end 21 by described cryogenic fluid pump 25 from the condenser end 24 of heat pump set 2, after cryogen is sent into by the input aperture of evaporator end 21, cryogen absorbs the heat of low-pressure steam in evaporator end 21 heat-transfer pipes and evaporates generation refrigerant vapour, makes low-pressure steam part condense into liquid and discharge unit simultaneously.The input aperture I that the refrigerant vapour generating is delivered to resorber end 22 by the delivery port of evaporator end 21 enters resorber end 22 inside.Low-pressure steam is the ammonia steam from ammonia still 1 top, ammonia steam is sent into the heat-transfer pipe of evaporator end 21 by the ammonia vapor inlet port of evaporator end 21, the most of gas-liquid mixture generating after heat exchange is outputed in gas-liquid separator 6 by the gas-liquid mixture delivery port of evaporator end 21 heat-transfer pipes.
At the resorber end 22 of described heat pump set 2, sprayed to the absorbent solution on the heat pipe of resorber end 22 by the input aperture II of resorber end 22, absorb the heat of the refrigerant vapour being generated by evaporator end 21.The absorption heat generating while absorbing refrigerant vapour heats up the hot water in resorber end 22 heat pipes, becomes superheated water.Absorbent solution absorbs after refrigerant vapour, and the absorbent solution of density loss becomes dilute solution, and dilute solution is sent into producer end 23 inside after heat exchange through the input aperture of producer end 23 by solution pump.The input aperture of circulating hot-water pump 3 receives by the hot water that after the heat exchange of reboiler 4, circulating hot water delivery port end is sent here (this part hot water has passed through heat release in reboiler 4 is interior, is the hot water after cooling, therefore hereinafter referred to as by cooling hot water).The corresponding hot water input aperture (instant heating tube inlet) that is communicated with described resorber end 22 of delivery port of circulating hot-water pump 3, thereby will be sent in the heat pipe of resorber end 22 by cooling hot water, the absorbent solution of spray absorb the absorption heat generating when refrigerant vapour be just used for heating this place by cooling hot water.Described is sent back to the front circulating hot water input aperture of heat exchange of reboiler 4 and is entered in reboiler 4 by hot water output port's (being heat pipe outlet) of described resorber end 22 by cooling hot water heated rear (becoming superheated water), generate saturation steam with the heat exchange of ammonia still process waste gas, and the saturation steam of generation is sent into ammonia still 1 inside.
At the producer end 23 of described heat pump set 2, by resorber end 22 that export and through heating after dilute solution, sprayed on the heat pipe of producer end 23, dilute solution is heated by the low-pressure steam in heat pipe, heated dilute solution produces refrigerant vapour, dilute solution becomes the absorbent solution that concentration is higher (being strong solution) simultaneously, the absorbent solution generating is sent back to resorber end 22 by the delivery port ii of producer end 23, and be to send into its inside through the input aperture II of resorber end 22, absorbent solution has been passed through the heating of solution heat exchanger 26 in the process of being carried to resorber end 22 by producer end 23.Low-pressure steam is the ammonia steam from ammonia still 1 top, ammonia steam is sent into the heat-transfer pipe of producer end 23 by the ammonia vapor inlet port of producer end 23, the gas-liquid mixture generating after heat exchange is outputed in gas-liquid separator 6 by the gas-liquid mixture delivery port of producer end 23 heat-transfer pipes.The refrigerant vapour that producer end 23 generates is delivered to condenser end 24 by the delivery port i of producer end 23, and enters its inside through the input aperture of condenser end 24.
In the condenser end 24 of described heat pump set 2, the refrigerant vapour of being sent into by the input aperture of condenser end 24 sprays on the heat transfer tube of condenser end 24, refrigerant vapour becomes cryogen liquid after being lowered the temperature, the input aperture place that cryogen liquid is transported to evaporator end 21 by the delivery port of condenser end 24 through cryogenic fluid pump 25 enters evaporator end 21 inside.
The ammonia steam reclaiming after latent heat has become gas-liquid mixture, and flows in gas-liquid separator 6, and the gas phase separating in gas-liquid separator 6 is connected with sulphur ammonium operation saturex or coal gas negative pressure, and the liquid phase separating is returned to distillation tower 1.
In a word, waste water pump 5 is sent into distilled ammonia wastewater and the heat pump set 2 of reboiler 4 inside and is sent into the superheated water heat exchange in reboiler 4, generates saturation steam and sends in ammonia still 1.Superheated water after heat exchange becomes the hot water that temperature is lower and is admitted to circulating hot-water pump 3, and sends back to heat pump set 2 and carry out heat exchange intensification through circulating hot-water pump 3, is sending back to reboiler 4, so cycle heat exchange after becoming superheated water.
Except the technical characterictic described in specification sheets, be the known technology of those skilled in the art.
Claims (2)
1. a remained ammonia ammonia still process tower top ammonia steam heat recovery system, comprises ammonia still, waste water pump and heat pump set; The distilled ammonia wastewater delivery port of ammonia still bottom is communicated with the input aperture of waste water pump, it is characterized in that:
Also comprise reboiler, circulating hot-water pump and gas-liquid separator; The delivery port of described waste water pump is communicated with the distilled ammonia wastewater input aperture of reboiler bottom;
Described heat pump set is absorption type heat pumping set, comprises evaporator end, resorber end, condenser end and producer end; Described condenser end is communicated with cooling water source;
The delivery port of described evaporator end is communicated with the input aperture I of described resorber end;
The delivery port of described resorber end is communicated with the input aperture of described producer end, and is serially connected with solution heat exchanger on this connecting path;
The delivery port I of described producer end is communicated with the input aperture of described condenser end;
The delivery port of described condenser end is communicated with the input aperture of described evaporator end and is serially connected with cryogenic fluid pump on this connecting path;
The delivery port II of described producer end is communicated with the input aperture II of described resorber end and is serially connected with solution heat exchanger on this connecting path;
The ammonia steam outlet at described ammonia still top is communicated with the ammonia vapor inlet port of described evaporator end by the first branch road, be communicated with the ammonia vapor inlet port of described producer end by the second branch road;
The gas-liquid mixture delivery port of the gas-liquid mixture delivery port of described evaporator end and described producer end is communicated with respectively the input aperture of described gas-liquid separator;
The liquid phase delivery port of described gas-liquid separator is communicated to ammonia still; The saturation steam delivery port at described reboiler top is communicated to ammonia still;
After the heat exchange of described reboiler, circulating hot water delivery port is communicated with the input aperture of described circulating hot-water pump;
The delivery port of described circulating hot-water pump is communicated with the hot water input aperture of described resorber end;
The hot water output port of described resorber end is communicated with the front circulating hot water of the heat exchange input aperture of described reboiler.
2. remained ammonia ammonia still process tower top ammonia steam heat recovery system according to claim 1, is characterized in that: the gas phase delivery port on described gas-liquid separator is communicated with sulphur ammonium operation saturex or coal gas negative pressure end.
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| CN201410070540.7A CN103803668A (en) | 2014-02-28 | 2014-02-28 | System for recovering residual heat of ammonia vapor on top of surplus ammonia water ammonia still |
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| CN201410070540.7A CN103803668A (en) | 2014-02-28 | 2014-02-28 | System for recovering residual heat of ammonia vapor on top of surplus ammonia water ammonia still |
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| CN104403700A (en) * | 2014-11-26 | 2015-03-11 | 山东钢铁股份有限公司 | Device and method for coke oven gas cooling and residual heat recycling |
| CN104534741A (en) * | 2014-12-31 | 2015-04-22 | 新疆科宇科技有限公司 | Heat efficient coupling energy-saving system for high-temperature heat pump of distillation equipment and refrigerating machine |
| CN104926012A (en) * | 2015-06-30 | 2015-09-23 | 长沙华时捷环保科技发展有限公司 | Treatment process for high-concentration ammonium-nitrogen waste water |
| CN105836760A (en) * | 2016-03-17 | 2016-08-10 | 山东钢铁股份有限公司 | Method and system for producing ammonia water from salt extracting waste steam of HPF-process desulfurization liquid with ammonia as alkali source |
| CN106766342A (en) * | 2016-12-12 | 2017-05-31 | 松下制冷（大连）有限公司 | Ammonia still process column overhead ammonia vapour residual heat system is reclaimed using lithium bromide absorption type heat pump |
| CN107504548A (en) * | 2017-09-18 | 2017-12-22 | 江苏中圣管道工程技术有限公司 | A kind of steam-water mixing central heating system |
| CN108251144A (en) * | 2018-01-29 | 2018-07-06 | 中冶焦耐(大连)工程技术有限公司 | The technique and system of tar final dewatering are realized using heat pump unit recovery waste heat |
| CN109336133A (en) * | 2018-11-15 | 2019-02-15 | 山东联盛环保科技有限公司 | A kind of device and technique of negative pressure low temperature recycling high concentration ammonium hydroxide |
| CN110440626A (en) * | 2019-09-05 | 2019-11-12 | 荏原冷热系统（中国）有限公司 | Ammonia still process column overhead ammonia steam heat recovery system and coking process system |
| CN110436545A (en) * | 2019-07-16 | 2019-11-12 | 临涣焦化股份有限公司 | A kind of remained ammonia distilling apparatus of heat energy recycling |
| CN114526564A (en) * | 2021-12-31 | 2022-05-24 | 湖南中创化工股份有限公司 | Method and device for recycling latent heat of acetic acid removal tower of isopropyl acetate device based on heat pump system |
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| CN104403700A (en) * | 2014-11-26 | 2015-03-11 | 山东钢铁股份有限公司 | Device and method for coke oven gas cooling and residual heat recycling |
| CN104534741B (en) * | 2014-12-31 | 2018-04-06 | 新疆科宇科技有限公司 | A kind of high temperature heat pump of distillation equipment and refrigeration machine heat coupling energy-saving system |
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| CN104926012A (en) * | 2015-06-30 | 2015-09-23 | 长沙华时捷环保科技发展有限公司 | Treatment process for high-concentration ammonium-nitrogen waste water |
| CN104926012B (en) * | 2015-06-30 | 2017-03-22 | 长沙华时捷环保科技发展股份有限公司 | Treatment process for high-concentration ammonium-nitrogen waste water |
| CN105836760A (en) * | 2016-03-17 | 2016-08-10 | 山东钢铁股份有限公司 | Method and system for producing ammonia water from salt extracting waste steam of HPF-process desulfurization liquid with ammonia as alkali source |
| CN106766342A (en) * | 2016-12-12 | 2017-05-31 | 松下制冷（大连）有限公司 | Ammonia still process column overhead ammonia vapour residual heat system is reclaimed using lithium bromide absorption type heat pump |
| CN107504548A (en) * | 2017-09-18 | 2017-12-22 | 江苏中圣管道工程技术有限公司 | A kind of steam-water mixing central heating system |
| CN108251144A (en) * | 2018-01-29 | 2018-07-06 | 中冶焦耐(大连)工程技术有限公司 | The technique and system of tar final dewatering are realized using heat pump unit recovery waste heat |
| CN108251144B (en) * | 2018-01-29 | 2023-08-01 | 中冶焦耐(大连)工程技术有限公司 | Process and system for realizing final dehydration of tar by recycling waste heat of heat pump unit |
| CN109336133A (en) * | 2018-11-15 | 2019-02-15 | 山东联盛环保科技有限公司 | A kind of device and technique of negative pressure low temperature recycling high concentration ammonium hydroxide |
| CN110436545A (en) * | 2019-07-16 | 2019-11-12 | 临涣焦化股份有限公司 | A kind of remained ammonia distilling apparatus of heat energy recycling |
| CN110440626A (en) * | 2019-09-05 | 2019-11-12 | 荏原冷热系统（中国）有限公司 | Ammonia still process column overhead ammonia steam heat recovery system and coking process system |
| CN114526564A (en) * | 2021-12-31 | 2022-05-24 | 湖南中创化工股份有限公司 | Method and device for recycling latent heat of acetic acid removal tower of isopropyl acetate device based on heat pump system |
| CN114526564B (en) * | 2021-12-31 | 2023-09-29 | 湖南中创化工股份有限公司 | Method and device for recycling latent heat of acetic acid removal tower of isopropyl acetate device based on heat pump system |
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Application publication date: 20140521 |