CN106403496A - Method for strengthening liquefying separation of synthetic product through waste heat and waste pressure refrigerating - Google Patents
Method for strengthening liquefying separation of synthetic product through waste heat and waste pressure refrigerating Download PDFInfo
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Abstract
The invention discloses a method for strengthening low-temperature liquefying separation of a reaction product through waste heat and waste pressure refrigerating. The liquefied product obtained through condensation separation under the low temperature and the low pressure serves as a refrigerant so that normal-temperature refrigerating liquid can be cooled to the low-temperature vaporization temperature; the refrigerant then absorbs waste heat to be heated to 135 DEG C to 185 DEG C to become an expansion machine working medium, adiabatic expansion is conducted, and mechanical power is output; and the expansion machine outlet working medium is liquefied under the normal-temperature -air cooling conditions, serves as the product to be output and is also used as the refrigerating liquid to be circulated, the expansion machine outlet working medium is also used as working fluid of an ejector to absorb waste heat and is heated and pressurized to be ejected to absorb refrigerating liquid steam vaporized under the low temperature, the cooling capacity needed for condensation separation of the liquefied product is provided, and therefore the separation effect is strengthened, the product yield is increased, and the refrigerating energy consumption is reduced. Condensate waste heat or low-pressure waste heat steam at the temperature of 185 DEG C is used for refrigerating, the condensate waste heat or low-pressure waste heat steam is used for strengthening liquefying separation of ammonia synthetic tower products, and the yield can be increased by 10% or higher; and the condensate waste heat or low-pressure waste heat steam is used for strengthening liquefying separation of methyl alcohol synthetic tower products, and the yield can be increased by 9.6% or higher.
Description
Technical field
The present invention relates to the use of the field of energy-saving technology of industrial process waste heat overbottom pressure refrigeration, the particularly industrial process such as synthesis ammonia, synthesizing methanol needs the method using low-temperature liquefaction separation chemistry product.
Background technology
The pressure synthesis chemical reaction process systems such as synthesis ammonia, synthesizing methanol, a certain proportion of product and reactant is contained in reactor outlet high pressure gas mixture, the condensing temperature of product is far above reactant at the same pressure, admixture of gas is therefore made to cool to the condensing temperature less than product, you can to make product liquefaction separation, gas reactant be recycled back into reactor.According to the macroscopic property of product, system pressure is higher, temperature is lower, be more conducive to product liquefaction to separate.On the premise of system pressure is certain, idetified separation is mainly by reduction thing system temperature.Temperature is brought down below room temperature cooling water, then need refrigeration to provide low temperature refrigerant.Temperature is lower, energy consumption for cooling is bigger, and this is that restriction prior art liquefaction separation temperature fails to reach the principal element of low temperature needed for preferable product yield.Taking 13.0MPa ammonia synthesis process as a example, existing 0 DEG C of process liquefaction separation temperature, the synthesis ammoniacal liquor separation product yield that reactor generates is brought back reactor less than the 80%, product residue more than 20% in circulating air again, reduces reactor production capacity.The method breaking through this kind of restriction is using chemical reaction process internal system waste heat overbottom pressure refrigeration, so that liquefaction separation temperature reduces limiting from energy consumption for cooling.Particularly with the separating obtained liquefaction products of high pressure low temperature from as cold-producing medium, before blood pressure lowering enters storage tank, play the effect of pressure energy contained by it, absorb adiabatic expansion acting after waste heat raising enthalpy, complete to export mechanical work while pressure reduction, kill two birds with one stone.The inventive method is based on above-mentioned principle and utilizes chemical process system waste heat overbottom pressure refrigeration strengthening product low-temperature liquefaction to separate, and has energy-conservation, reduction of discharging, increases production multiple advantageous effects.
Content of the invention
A kind of open the refrigeration using chemical reaction process system waste heat overbottom pressure of the present invention strengthens the detached method of product low-temperature liquefaction, with reactor outlet process fluid through low temperaturet 4（-20~0℃）High pressurep 4（4.5~24.5MPa）The separating obtained product that liquefies is coolant, makes the cold-producing medium of recycling be down to the required low temperature of refrigeration from room temperature, coolant temperature rise is extremelyt 0（55~65℃）The waste heat of re-absorption process system is warming up to afterwardst 5（135~185℃）Become decompressor working medium, adiabatic expansion is to pressure againp 6（0.01~2.0 MPa）, temperaturet 6（0~60℃）, output mechanical workW 6（Heat-work(conversion ratio 18% ~ 33%）.After expander outlet working medium liquefies under normal temperature air cooling condition, both exported as liquefaction products, and also served as refrigerant cycle, also serve as the working fluid of ejector：During as cold-producing medium, in cryogenic temperaturet 2（-10~10℃）Ort 3（-25 ~ -5℃）Lower heat absorption vaporizes and is forced to suck ejector, boosts to the pressure that can use normal temperature air cooling liquidp 8（0.01~2.0 MPa）；During working fluid as ejector, by its fromp 8It is pressurized top 15（0.3~20 MPa）, recycle process waste so that it is vaporized and be superheated tot 15（135~185℃）Attract thus there is enough energy and entering ejectort 2Ort 3At a temperature of vaporization refrigerant vapour, and be mixed with boosting top 8, liquefy under normal temperature air cooling condition, recycle.
The technology of the present invention route is：Reactor outlet pressurep 0（5~25 MPa）, product assay mole percenty 0（5~20%）Mixed gas, cooled to by preposition heat transmission equipmentT 0（35~45℃）Afterwards, by temperature in recirculation cooler 1t 4（-20~0℃）Cold cycle air cooling be cooled toT 1（15~25℃）, continue quilt in one-level cryogenic heat exchanger 2t 2（-10~10℃）At a temperature of vaporization cold-producing medium heat absorption cool toT 2（-5~15℃）, continue quilt in two grade low-temp heat exchangers 3t 3（-25 ~ -5℃）At a temperature of the cold-producing medium heat absorption of vaporization cooling and separate required low temperature to product liquefactionT 3（-20~0℃）, then separate in gas-liquid separator 4, obtain pressurep 4（4.5~24.5MPa）, temperaturet 4（-20~0℃）Liquefaction products and equality of temperature with pressure circulating air, the content of residual product in circulating airy 4Ratio reactor outlet contenty 0Low by more than 85%.Circulating air its temperature after circulation heat exchanger 1 reclaims cold is promoted to higher than 30 DEG C, then is further heated up to higher than 50 DEG C of Returning reactors circulations by preposition heat transmission equipment.
The pressure that gas-liquid separator 4 obtainsp 4（4.5~24.5MPa）, temperaturet 4（-20~0℃）Low-temperature liquefaction product absorb as coolant first and go after the heat of cold-producing medium of one-level cryogenic heat exchanger 2 and two grade low-temp heat exchangers 3 from room temperature storage tank 8 circulation, then the mixed gas heating temperature rise being come by reactor in preposition heat transmission equipment is extremelyt 0（55~65℃）, then be heated to by waste-heat recoverer 5t 5（135~185℃）, become the working medium entrance decompressor 6 adiabatic expansion output mechanical work of decompressor againW 6（Heat-work(conversion ratio 18% ~ 33%）, expander outlet power pressurep 6（0.01~2.0 MPa）, temperaturet 6（0~60℃）, pressure is condensed into by normal temperature air cooler 7p 8（0.01~2.0 MPa）, temperaturet 8（0~60℃）Liquid, enter room temperature storage tank 8 buffer after as liquefaction products output, or as cold-producing medium and ejector working fluid recycle.
Circulating from room temperature storage tank 8 goes the coolant that the cold-producing medium of one-level cryogenic heat exchanger 2 and two grade low-temp heat exchangers 3 is obtained by gas-liquid separator 4 to cool tot 9=t 10（-15~5℃）And reach supercooled state, respectively one-level cryogenic heat exchanger 2 and two grade low-temp heat exchanger 3 heat absorption vaporization refrigeration are entered by air relief valve 9 and 10, become respective vapourizing temperaturet 2（-10~10℃）Witht 3（-25 ~ -5℃）Under saturation refrigerant vapour, be forced to suck the first injector 11 of corresponding suction pressure and second injector 12.With force (forcing) pump 16 by ejector working fluid from the pressure of room temperature storage tank 8p 8It is pressurized top 15（0.3~20 MPa）, pass through waste-heat recoverer 15 heating after the mixed gas waste-heat temperature rise that preposition heat transmission equipment is come by reactor is to 55 ~ 65 DEG C again and vaporize and be superheated tot 15（135~185℃）, then respectively enter first injector 11 and second injector 12 attract the saturation refrigerant vapour of each self-corresponding one-level cryogenic heat exchanger 2 and two grade low-temp heat exchangers 3, and be allowed to boost to the corresponding condensing pressure of normal temperature air cooler 13 and 14 by mixingp 8（0.01~2.0 MPa）, liquefy and enter room temperature storage tank 8.Ejector working fluid mass flow amount with suck refrigerant vapour mass flow ratio 0.8 ~ 1.8.
Pressure value of the present invention refers both to absolute pressure, and the utilization warm area of described process waste is（65℃~200℃）, described atmospheric temperature exists（-20℃~40℃）Scope.
Brief description
Accompanying drawing 1 is the schematic diagram of the utilization chemical reaction process system waste heat overbottom pressure refrigeration strengthening product low-temperature liquefaction separation method that the present invention provides.In figure：1- circulation heat exchanger；2- one-level cryogenic heat exchanger；3- bis- grade low-temp heat exchanger；4- gas-liquid separator；5th, 15- waste-heat recoverer；6- decompressor；7th, 13,14- normal temperature air cooler；8- Normal Atmospheric Temperature Liquid product reservoir；9th, 10- air relief valve；11- first injector；12- second injector；16- force (forcing) pump.
Specific embodiments
Below in conjunction with but be not limited to embodiment illustrate the specific embodiment of the invention
The liquefaction that embodiment 1 produces product ammonia in 1320 tons of ammonia convertor exit gas daily separates
Ammonia convertor exit gas logistics：Total flow 23926.5 kmol/h, containing ammonia 4228.3 kmol/h, remaining is nitrogen, hydrogen
Ammonia convertor exit gas stagnation pressure：13.0 MPa
Ammonia separation Posterior circle gas stagnation pressure：12.2 MPa
Waste heat thermal source 1：Shift conversion step collects 185 DEG C of water vapor condensates, 137120 kg/h
Waste heat thermal source 2：Waste heat boiler produces 185 DEG C, 1.0MPa saturated vapor, 20000 kg/h
1320 tons of ammonia convertor outlet pressures of daily outputp 0（≤13.0MPa）, ammonia content mole percenty 0（≥17.67%）Mixed gas 23926.5 kmol/h, cooled to by preposition heat transmission equipmentT 0（35℃）Afterwards, by temperature in recirculation cooler 1t 4（-10℃）Cold cycle air cooling be cooled toT 1（24℃）, continue quilt in one-level cryogenic heat exchanger 2t 2（0℃）At a temperature of liquid ammonia vaporization heat absorption cool toT 2（10℃）, continue quilt in two grade low-temp heat exchangers 3t 3（-16℃）At a temperature of liquid ammonia vaporization heat absorption cool and separate required low temperature to product ammoniacal liquorization in mixed gasT 3（≤-10℃）, enter in gas-liquid separator 4 and separate, obtain pressurep 4（≤12.2MPa）, temperaturet 4（≤-10℃）Liquefied ammonia 3594 kmol/h and equality of temperature with pressure circulating air, remaining ammonia content in circulating airy 4（≤2.38%）Compare reactor outlety 0Low by more than 86.5%.Circulating air its temperature after circulation heat exchanger 1 reclaims cold is promoted to 31 DEG C, then is further heated up to 55 DEG C of return ammonia convertors circulations by preposition heat transmission equipment.
Low-temperature liquid ammonia 61098 kg/h that gas-liquid separator 4 obtains absorbs as coolant first and goes after one-level cryogenic heat exchanger 2 and two grade low-temp heat exchangers 3 heat as the liquefied ammonia of cold-producing medium from room temperature storage tank 8 circulation, continues in preposition heat transmission equipment by the next mixed gas waste-heat temperature rise of ammonia convertor extremelyt 0（≥60℃）, then pass through waste-heat recoverer 5 137120 kg/h water vapor condensates（185℃）Waste-heat is extremelyt 5（180℃）, enter decompressor 6 adiabatic expansion output mechanical work as decompressor working mediumW 6（14076.6 MJ/h, heat-work(conversion ratio >=20.6%）, expander outlet power pressurep 6（2.0 MPa）, temperaturet 6（50℃）Pressure is condensed into by normal temperature air cooler 7p 8（≤2.0 MPa）, temperaturet 8（≤50℃）Liquefied ammonia, enter room temperature storage tank 8 buffer after as liquefied ammonia output of products 61098 kg/h.
Circulating from room temperature storage tank 8 as cold-producing medium goes the low-temperature liquid ammonia that liquefied ammonia 34860 kg/h of one-level cryogenic heat exchanger 2 and two grade low-temp heat exchangers 3 is obtained by gas-liquid separator 4 first to cool tot 9=t 10（-5℃）And reach supercooled state, then respectively one-level cryogenic heat exchanger 2 is entered by air relief valve 9 and 10（15810 kg/h）With two grade low-temp heat exchangers 3（19050 kg/h）Heat absorption vaporization refrigeration, becomes respective vapourizing temperaturet 2（0℃）Witht 3（-16℃）Under saturated ammonia steam, and be forced to suck each self-corresponding first injector 11 and second injector 12.With force (forcing) pump 16 using as ejector working fluid 41000 kg/h liquefied ammonia from the pressure of room temperature storage tank 8p 8It is pressurized top 15（≤8.0 MPa）, pass through waste-heat recoverer 15 waste heat boiler after the mixed gas waste-heat temperature rise that preposition heat transmission equipment is come by ammonia convertor is to 60 DEG C again and produce saturated vapor 20000 kg/h（185℃）Heating vaporizes and is superheated tot 15（180℃）, then respectively enter first injector 11（15800 kg/h）With second injector 12（25200 kg/h）Attract the saturated ammonia steam of each self-corresponding one-level cryogenic heat exchanger 2 and two grade low-temp heat exchangers 3, and make ejector export by mixing to reach the corresponding condensing pressure of normal temperature air cooler 13 and 14p 8（2.0 MPa）, liquefaction return room temperature storage tank 8.
The present embodiment utilizes ammonia synthesis process system waste heat（137120 kg/h and 185 DEG C of waste hot steam 20000 kg/h of 185 DEG C of water vapor condensates）Refrigeration, strengthening synthetic tower outlet mixed gas condensation at low temperature liquefaction separates and synthesizes ammonolysis product, and compared with prior art, the beneficial effect of acquisition is：
Make daily output 1320 tons of ammonia convertor output increased to 1460 tons, production capacity increases by 10.6%；
Save mechanical compression refrigeration energy consumption 11274 MJ/h and export mechanical work 14076 MJ/h, total energy-conservation 25350MJ/h；
2000 tons of cooling water of saving/per hour.
The liquefaction that embodiment 2 produces product methanol in 300 tons of methyl alcohol synthetic reactor exhaust gas daily separates
Methyl alcohol synthetic reactor exhaust gas：Total flow 6080.9 kmol/h, containing methanol 433 kmol/h, aqueous 38.3 kmol/h, remaining is incoagulability synthesis gas
Methyl alcohol synthetic reactor exhaust gas stagnation pressure：≤5.0 MPa
Methyl alcohol synthetic reactor circulating air stagnation pressure：≤4.88 MPa
Waste heat thermal source 1：Shift conversion step collects 185 DEG C of water vapor condensates, 10500 kg/h
Waste heat thermal source 2：Waste heat boiler produces 185 DEG C, 1.0MPa saturated vapor, 1560 kg/h
300 tons of methyl alcohol synthetic reactors of daily output go out pressure towerp 0（≤5.0MPa）, methanol content mole percenty 0（≤7.12%）Mixed gas 6080.9 kmol/h, cooled to by preposition heat transmission equipmentT 0（40℃）Afterwards, by temperature in recirculation cooler 1t 4（0℃）Cold cycle air cooling be cooled toT 1（15℃）, continue quilt in one-level cryogenic heat exchanger 2t 2（-10℃）At a temperature of cold-producing medium methyl alcohol vaporizing heat absorption cool toT 2（≤0℃）, enter in gas-liquid separator 4 and separate, obtain pressurep 4（≤4.88MPa）, temperaturet 4（≤0℃）Methanol solution 428.4 kmol/h（13708.7 kg/h）With equality of temperature with the cold cycle gas pressed, residual methanol content in cold cycle gasy 4（≤0.082%）Than methyl alcohol synthetic reactor outlety 0Low by 98.8%.Cold cycle gas its temperature after circulation heat exchanger 1 reclaims cold is promoted to 35 DEG C, returns methyl alcohol synthetic reactor by preposition heat transmission equipment.
Low-temp methanol liquid 13708.7 kg/h that gas-liquid separator 4 obtains absorbs from room temperature as coolant first（65℃）After the heat as the methanol solution of cold-producing medium for the one-level cryogenic heat exchanger 2 is removed in storage tank 8 circulation, in preposition heat transmission equipment by the next mixed gas waste-heat temperature rise of methyl alcohol synthetic reactor extremelyt 0（65℃）, then pass through waste-heat recoverer 5 10500 kg/h water vapor condensates（185℃）Waste-heat is extremelyt 5（180℃）, enter decompressor 6 adiabatic expansion output mechanical work as decompressor working mediumW 6（1091.8 MJ/h, heat-work(conversion ratio >=22%）, expander outlet power pressurep 6（0.105 MPa）, temperaturet 6（65℃）Pressure is condensed into by normal temperature air cooler 7p 8（0.105MPa）, temperaturet 8（≤65℃）Methanol solution, enter room temperature storage tank 8 buffer after as product methanol export 13708.7 kg/h.
The low-temp methanol liquid that 65 DEG C of methanol solution 1778.6 kg/h of one-level cryogenic heat exchanger 2 are obtained by gas-liquid separator 4 first is gone to cool to as cold-producing medium from room temperature storage tank 8 circulationt 9（3℃）Reach supercooled state, then one-level cryogenic heat exchanger 2 heat absorption vaporization refrigeration is entered by air relief valve 9, become vapourizing temperaturet 2（≤-10℃）Under saturation methanol steam, and be forced suck first injector 11.With force (forcing) pump 16 using as ejector working fluid 2976.8 kg/h methanol solutions from the pressure of room temperature storage tank 8p 8It is pressurized top 15（≤0.9 MPa）, produced with waste heat boiler in waste-heat recoverer 15（185℃）Saturated vapor 1560 kg/h heating vaporizes and is superheated tot 15（180℃）, attract the next saturation methanol steam of one-level cryogenic heat exchanger 2 vaporization subsequently into first injector 11, and make ejector export by mixing to reach the corresponding condensing pressure of normal temperature air cooler 13p 8（≥0.105 MPa）, liquefaction return room temperature storage tank 8.
The present embodiment utilizes methanol technics system waste heat（10500 kg/h and 185 DEG C of waste hot steam 1560 kg/h of 185 DEG C of water vapor condensates）Refrigeration, strengthening methyl alcohol synthetic reactor outlet mixed gas condensation at low temperature liquefaction separates, and compared with prior art, the beneficial effect of acquisition is：
Make daily output 300 tons of methyl alcohol synthetic reactor output increased to 329 tons, production capacity increases by 9.67%；
Make that circulating air is aqueous to be down to less than 0.005%；
Output mechanical work 1091.8 MJ/h；
500 tons of cooling water of saving/per hour.
The invention is not restricted to above-described embodiment, its technical scheme is explained in Summary.
Claims (3)
1. a kind of refrigeration using waste heat overbottom pressure strengthens the detached method of product low-temperature liquefaction, it is characterized in that being coolant with reactor outlet process fluid in the separating obtained liquefaction products of -20 ~ 0 DEG C of low temperature, 4.5 ~ 24.5MPa liquefied at high pressure, the cold-producing medium of recycling is down to -15 ~ 5 DEG C required of low temperature of refrigeration from room temperature；The waste heat of coolant absorption technique system is warming up to 135 ~ 185 DEG C, becomes the working medium adiabatic expansion output mechanical work of decompressor, heat-work(conversion ratio 18 ~ 33% again；0 ~ 60 DEG C of expander outlet power pressure 0.01 ~ 2.0 MPa, temperature, liquefies under normal temperature air cooling condition, enters room temperature storage tank buffer, both exported as liquefaction products, and also served as refrigerant cycle, also serve as the working fluid of ejector；Working medium as cold-producing medium, -10 ~ 10 DEG C of one-level cryogenic heat exchanger or two grade low-temp heat exchangers -25 ~
Vaporization refrigeration at a temperature of -5 DEG C, the saturated vapor of vaporization is inhaled into the ejector of corresponding suction pressure；Working medium as ejector working fluid, it is pressurized to the pressure of 0.3 ~ 20 MPa, it is allowed to vaporize and be superheated to 135 ~ 185 DEG C using waste heat, respectively enter the first injector refrigerant vapour that attract one-level cryogenic heat exchanger and two grade low-temp heat exchangers vaporization corresponding with second injector, and boost to 0.01 ~ 2.0 MPa, be allowed to liquefy with normal temperature air cooler by mixing；Ejector working fluid mass flow amount is 0.8 ~ 1.8 with the ratio of the refrigerant vapour mass flow sucking.
2. utilize the waste heat overbottom pressure refrigeration strengthening detached method of product low-temperature liquefaction according to claim 1, it is characterized in that the ammonia convertor exit gas of pressure≤13.0MPa, ammonia content mole percent >=17%, cool≤- 10 DEG C by one-level cryogenic heat exchanger and two grade low-temp heat exchangers, remaining ammonia content mole percent≤2.38% in gas-liquid separation Posterior circle gas；Using gas-liquid separation gained low-temperature liquid ammonia first as the heat of coolant absorption refrigeration agent -5 DEG C of temperatures above of liquefied ammonia, then absorb ammonia convertor exit gas waste heat and be warming up to >=60 DEG C, the waste-heat of the 185 DEG C of water vapor condensates collected with shift conversion step again is not less than 20% to 180 DEG C as decompressor working medium adiabatic expansion output mechanical work, heat-work(conversion ratio, and expander outlet working medium is condensed into the saturation liquefied ammonia of temperature≤50 DEG C by normal temperature air cooler；Liquefied ammonia as ejector working fluid is pressurized to≤8.0 MPa, absorb ammonia convertor outlet mixed gas waste heat temperature rise to be vaporized and be superheated to 180 DEG C with 185 DEG C of saturated vapor heating again to after >=60 DEG C, enter the cold-producing medium saturated vapor at a temperature of ejector attracts -16 ~ 0 DEG C, working fluid mass flow amount and the ratio 0.8 ~ 1.8 of refrigerant vapour mass flow, make refrigerant vapour boost to normal temperature air cooler corresponding condensing pressure≤2.0 MPa by ejector.
3. utilize the waste heat overbottom pressure refrigeration strengthening detached method of product low-temperature liquefaction according to claim 1, it is characterized in that the methyl alcohol synthetic reactor exhaust gas body of pressure≤5.0MPa, methanol content mole percent≤7%, cool≤0 DEG C by one-level cryogenic heat exchanger, by residual methanol content mole percent≤0.082% in gas-liquid separation Posterior circle gas；Using gas-liquid separation gained low-temp methanol liquid first as the heat of coolant absorption refrigeration more than 3 DEG C warm areas of agent methanol solution, then absorb methyl alcohol synthetic reactor exhaust gas body waste heat and be warming up to >=60 DEG C, the waste-heat of the 185 DEG C of water vapor condensates collected with shift conversion step again is not less than 22% to 180 DEG C as decompressor working medium adiabatic expansion output mechanical work, heat-work(conversion ratio, and expander outlet working medium is condensed into the saturation methanol solution of temperature≤65 DEG C by normal temperature air cooler；Room temperature methanol solution is pressurized to≤0.9 MPa, vaporized and be superheated to 180 DEG C with 185 DEG C of saturated vapor heating, as ejector working fluid attract≤- 10 DEG C at a temperature of cold-producing medium methanol saturated vapor, working fluid mass flow amount and the ratio 0.8 ~ 1.8 of refrigerant vapour mass flow, make cold-producing medium methanol steam boost to the corresponding condensing pressure >=0.105MPa of normal temperature air cooler by ejector.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106679243A (en) * | 2017-02-17 | 2017-05-17 | 查都（上海）科技有限公司 | Refrigerating system for lowering liquid ammonia consumption |
| CN112004589A (en) * | 2018-04-20 | 2020-11-27 | 西门子股份公司 | Method for operating a reactor plant |
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2015
- 2015-08-02 CN CN201510463151.5A patent/CN106403496A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106679243A (en) * | 2017-02-17 | 2017-05-17 | 查都（上海）科技有限公司 | Refrigerating system for lowering liquid ammonia consumption |
| CN106679243B (en) * | 2017-02-17 | 2022-05-20 | 查都(海南)科技有限公司 | Refrigerating system capable of reducing liquid ammonia consumption |
| CN112004589A (en) * | 2018-04-20 | 2020-11-27 | 西门子股份公司 | Method for operating a reactor plant |
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