CN204404693U - Reclaim the device that synthetic ammonia tailgas produces LNG - Google Patents
Reclaim the device that synthetic ammonia tailgas produces LNG Download PDFInfo
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- CN204404693U CN204404693U CN201420855200.0U CN201420855200U CN204404693U CN 204404693 U CN204404693 U CN 204404693U CN 201420855200 U CN201420855200 U CN 201420855200U CN 204404693 U CN204404693 U CN 204404693U
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Abstract
The utility model discloses and reclaim the device that synthetic ammonia tailgas produces LNG, precool heat exchanger device, booster expansion turbine, gas-liquid separator, dehydrogenation rectifying column and methane rectifying column that it comprises cyclic nitrogen compressor, the first cooler, the second cooler, the 3rd cooler and is arranged in ice chest, described precool heat exchanger device comprises carbon dioxide precooling device and main heat exchanger.Have the following advantages: utilize cryogenic separation synthetic ammonia tailgas technology; again abundant extraction is carried out to methane while the useful hydrogen of ammonia synthesis production is recycled; and liquefaction is the LNG of high added value; be minimized ammonia cost, synthetic ammonia tailgas resource fully recycle with environmental protection problem on accomplish to kill two birds with one stone.
Description
Technical field
The utility model belongs to the recovery and utilization technology field related to periodic off-gases (tail gas) in ammonia synthesizing industry, particularly carries out to the methane in synthetic ammonia tailgas a kind of device reclaiming synthetic ammonia tailgas production LNG that cryogenic separation is extracted into liquefied natural gas LNG.
Background technology
In chemical fertilizer industry field, can produce in the process of preparing ammonia about containing the periodic off-gases of 25% methane, and in the production process of synthetic ammonia, also can produce about containing the synthesis gas of 35% methane, above gas constitutes synthetic ammonia tailgas.For ensureing normally carrying out of ammonia synthesis reaction, synthetic ammonia tailgas need be discharged, to control the concentration of methane.
Now for the method for disposal of synthetic ammonia tailgas, worst is directly be discharged in air, but the methane in tail gas is a kind of greenhouse gases, and it causes the power of global warming to be 25 times of carbon dioxide, and this causes the waste of environmental pollution and resource; Another kind collects after-combustion, and be converted into the secondary energy sources such as heat energy, electric energy, but the economic benefit of the method is lower, the compositions such as the methane that in tail gas, economic value added is very high, hydrogen cannot be recycled; What have is exactly use to filter purification technique and extract the valuable components such as the methane in tail gas again, and prior art and production technology exist the shortcomings such as high energy consumption, high cost, recovery rate are low.
Utility model content
Technical problem to be solved in the utility model is; there is provided a kind of and reclaim the device that synthetic ammonia tailgas produces LNG; utilize cryogenic separation synthetic ammonia tailgas technology; again abundant extraction is carried out to methane while the useful hydrogen of ammonia synthesis production is recycled; and liquefaction is the LNG of high added value; be minimized ammonia cost, synthetic ammonia tailgas resource fully recycle with environmental protection problem on accomplish to kill two birds with one stone.
For solving the problems of the technologies described above, the recovery synthetic ammonia tailgas that the utility model provides produces the device of LNG, precool heat exchanger device, booster expansion turbine, gas-liquid separator, dehydrogenation rectifying column and methane rectifying column that it comprises cyclic nitrogen compressor, the first cooler, the second cooler, the 3rd cooler and is arranged in ice chest, described precool heat exchanger device comprises carbon dioxide precooling device and main heat exchanger, described precool heat exchanger device is provided with high pressure exhaust gas entrance, low-pressure tail gas entrance, hydrogen rich gas exports, rich nitrogen outlet, the circulating nitrogen gas that backflows exports, high pressure nitrogen entrance, high pressure nitrogen exports, backflow circulating nitrogen gas entrance, rich nitrogen inlet, hydrogen rich gas entrance, low-pressure tail gas outlet and high pressure exhaust gas outlet, described high pressure exhaust gas entrance, low-pressure tail gas entrance, hydrogen rich gas exports, rich nitrogen outlet, the circulating nitrogen gas that backflows outlet is communicated with carbon dioxide precooling device respectively with high pressure nitrogen entrance, described high pressure nitrogen outlet, backflow circulating nitrogen gas entrance, rich nitrogen inlet, hydrogen rich gas entrance, low-pressure tail gas outlet is communicated with main heat exchanger respectively with high pressure exhaust gas outlet, described cyclic nitrogen suction port of compressor is communicated with the rich nitrogen outlet of source nitrogen and precool heat exchanger device, its outlet is communicated with booster expansion turbine pressurized end entrance through the first cooler, the outlet of booster expansion turbine pressurized end is communicated with the high pressure nitrogen entrance of precool heat exchanger device again, the high pressure nitrogen exit of precool heat exchanger device is provided with two branch roads, article one, branch road is communicated with booster expansion turbine expanding end entrance, the outlet of booster expansion turbine expanding end is communicated with the circulating nitrogen gas entrance that backflows of precool heat exchanger device again through subcooler, the circulating nitrogen gas that backflows exports communication loop nitrogen suction port of compressor again, another branch road is communicated with methane rectifier through subcooler, high pressure exhaust gas entrance and the low-pressure tail gas entrance of described precool heat exchanger device are communicated with synthesis source of the gas and periodic off-gases source respectively, the outlet of its low-pressure tail gas is communicated with dehydrogenation rectifying column inlet again through dehydrogenation rectifying column reboiler, and the outlet of its high pressure exhaust gas is successively in the middle part of methane rectifying column reboiler is communicated with dehydrogenation rectifying column again with subcooler, the methane-rich liquid outlet methane rectifying column inlet of dehydrogenation rectifier bottoms methane-rich liquid bottom dehydrogenation rectifying column reboiler, the LNG storage tank outside the liquefied natural gas outlet ice chest of methane rectifier bottoms liquefied natural gas bottom methane rectifying column reboiler, the hydrogen rich gas outlet of described dehydrogenation rectifying column top is communicated with gas-liquid separator entrance again through subcooler, liquid bottom gas-liquid separator is communicated with again dehydrogenation rectifier, the hydrogen rich gas outlet at gas-liquid separator top is communicated with the hydrogen rich gas entrance of precool heat exchanger device again through subcooler, the hydrogen rich gas outlet of precool heat exchanger device is communicated with the pressure-swing absorption apparatus outside ice chest through the second cooler, the rich nitrogen outlet at described methane rectifying column top is communicated with the rich nitrogen inlet of precool heat exchanger device through subcooler, the rich nitrogen outlet of precool heat exchanger device is provided with two branch roads, article one, branch road is communicated with the regenerative dryer outside ice chest, another branch road communication loop nitrogen suction port of compressor, methane rectifier is communicated with the liquid nitrogen storage tank outside ice chest.High pressure exhaust gas and low-pressure tail gas enter into ice chest respectively, effectively can utilize the high pressure energy of high pressure exhaust gas, reduce the effect of cyclic nitrogen compressor, reduce energy consumption.Set up gas-liquid separator, the methane in the hydrogen-rich gas of hydrogeneous, nitrogen, methane, the argon that dehydrogenation rectifying column top can be made to flow out is recycled further, improves the rate of recovery of methane.Because the minimum saturation temperature of liquefied natural gas is-162 DEG C, make it cross to be as cold as-165 DEG C by setting up subcooler, make liquefied natural gas enter into LNG storage tank process not generating gasification phenomenon, ensure that the liquefied natural gas entering into LNG storage tank is all liquid.
As preferably, carbon dioxide gas-liquid separator is also provided with in described ice chest, described carbon dioxide precooling device is also provided with carbon dioxide entrance, carbon dioxide gas-liquid separator bottom liquid stream outlet carbon dioxide precooling device, the entrance of carbon dioxide gas-liquid separator is communicated with the carbon dioxide storage tank outside ice chest, and the top of carbon dioxide gas-liquid separator is all communicated with the carbon dioxide recovering apparatus outside ice chest with the carbon dioxide outlet of carbon dioxide precooling device; Described carbon dioxide gas-liquid separator is also provided with overfall, and overfall is positioned at the top of carbon dioxide gas-liquid separator entrance.When foeign element causes that in carbon dioxide gas-liquid separator, liquid level exceedes suddenly overfall, liquid can be discharged automatically, now in carbon dioxide precooling device, liquid level can not continue to raise, ensure that liquid CO 2 completely to primary heat exchanger warm end, can not avoid the problem that excessive temperature differentials causes the breakage of exchanger heat stress.
As preferably, by pipeline communication between described each device, each segment pipe is provided with valve and instrument control point.
After adopting above structure, recovery synthetic ammonia tailgas of the present utility model produces the device of LNG compared with prior art, has the following advantages:
1) compact conformation, utilizes carbon dioxide precooling and nitrogen through booster expansion turbine swell refrigeration technique separation and recovery methane and hydrogen-rich gas, and produces liquid nitrogen product storage simultaneously.Both reduce cost, again saved the energy, have also obtained the LNG energy of environmental protection.
2) tail gas after can utilizing methane liquefaction carrys out supplementary nitrogen circulation, accomplishes to control oneself self-sustaining, does not need additionally to consume nitrogen cryogen, reduce energy consumption and operating cost.
3) add carbon dioxide precooling device, because this increasing carbon dioxide precooling flow process, the nitrogen expansion phase ratio with traditional, decreases cold damage, reduces nitrogen circulation energy consumption of compressor about about 20%.
4) can not only the production purity methane that is greater than 99.2% when nominal situation, liquid nitrogen product can also be produced simultaneously.As emergency power off, or during dynamic overhaul of the equipments, the liquid nitrogen re-injection ice chest from producing can being used to provide cold, still can normally produce.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Wherein: 1, carbon dioxide precooling device, 2, main heat exchanger, 3, LNG storage tank, 4, pressure-swing absorption apparatus, 5, regenerative dryer, 6, liquid nitrogen storage tank, 7, cyclic nitrogen compressor, 8, first cooler, 9, second cooler, 10, 3rd cooler, 11, precool heat exchanger device, 12, booster expansion turbine pressurized end, 13, booster expansion turbine expanding end, 14, gas-liquid separator, 15, dehydrogenation rectifying column, 16, methane rectifying column, 17, dehydrogenation rectifying column reboiler, 18, methane rectifying column reboiler, 19, carbon dioxide gas-liquid separator, 19.1, overfall, 20, subcooler, CO
2for carbon dioxide conduit, HYL is high pressure exhaust gas pipeline, and LYL is low-pressure tail gas pipeline, and N is nitrogen pipeline, and GN is elevated pressure nitrogen pipeline, and CN is the cyclic nitrogen pipeline that backflows, and FN is rich nitrogen pipeline, and FH is rich hydrogen pipeline.
Detailed description of the invention
Below by embodiment, the utility model will be further described by reference to the accompanying drawings.
As shown in Figure 1, the raw coke over gas riser heat recovering device that the present embodiment provides, precool heat exchanger device 11, booster expansion turbine, gas-liquid separator 14, dehydrogenation rectifying column 15 and methane rectifying column 16 that it comprises cyclic nitrogen compressor 7, first cooler 8, second cooler 9, the 3rd cooler 10 and is arranged in ice chest, described precool heat exchanger device 11 comprises carbon dioxide precooling device 1 and main heat exchanger 2, described precool heat exchanger device 11 is provided with high pressure exhaust gas entrance, low-pressure tail gas entrance, hydrogen rich gas exports, rich nitrogen outlet, the circulating nitrogen gas that backflows exports, high pressure nitrogen entrance, high pressure nitrogen exports, backflow circulating nitrogen gas entrance, rich nitrogen inlet, hydrogen rich gas entrance, low-pressure tail gas outlet and high pressure exhaust gas outlet, described high pressure exhaust gas entrance, low-pressure tail gas entrance, hydrogen rich gas exports, rich nitrogen outlet, the circulating nitrogen gas that backflows outlet is communicated with carbon dioxide precooling device 1 respectively with high pressure nitrogen entrance, described high pressure nitrogen outlet, backflow circulating nitrogen gas entrance, rich nitrogen inlet, hydrogen rich gas entrance, low-pressure tail gas outlet is communicated with main heat exchanger 2 respectively with high pressure exhaust gas outlet, described cyclic nitrogen compressor 7 entrance is communicated with the rich nitrogen outlet of source nitrogen and precool heat exchanger device 11, its outlet is communicated with booster expansion turbine pressurized end 12 entrance through the first cooler 8, the outlet of booster expansion turbine pressurized end is communicated with the high pressure nitrogen entrance of precool heat exchanger device 11 again, the high pressure nitrogen exit of precool heat exchanger device 11 is provided with two branch roads, article one, branch road is communicated with booster expansion turbine expanding end 13 entrance, the outlet of booster expansion turbine expanding end is communicated with the circulating nitrogen gas entrance that backflows of precool heat exchanger device 11 again through subcooler 20, the circulating nitrogen gas that backflows exports communication loop nitrogen compressor 7 entrance again, another branch road is communicated with methane rectifying column 16 top through subcooler 20, high pressure exhaust gas entrance and the low-pressure tail gas entrance of described precool heat exchanger device are communicated with synthesis source of the gas and periodic off-gases source respectively, the outlet of its low-pressure tail gas is communicated with dehydrogenation rectifying column inlet again through dehydrogenation rectifying column reboiler 17, and the outlet of its high pressure exhaust gas is successively in the middle part of methane rectifying column reboiler 18 is communicated with dehydrogenation rectifying column again with subcooler 20, the methane-rich liquid outlet methane rectifying column inlet of dehydrogenation rectifier bottoms methane-rich liquid bottom dehydrogenation rectifying column reboiler 17, the LNG storage tank 3 outside the liquefied natural gas outlet ice chest of methane rectifier bottoms liquefied natural gas bottom methane rectifying column reboiler, the hydrogen rich gas outlet of described dehydrogenation rectifying column top is communicated with gas-liquid separator 14 entrance again through subcooler 20, liquid bottom gas-liquid separator 14 is communicated with again dehydrogenation rectifying column 15 top, the hydrogen rich gas outlet at gas-liquid separator 14 top is communicated with the hydrogen rich gas entrance of precool heat exchanger device again through subcooler 20, the hydrogen rich gas outlet of precool heat exchanger device is communicated with the pressure-swing absorption apparatus 4 outside ice chest through the second cooler 9, the rich nitrogen outlet at described methane rectifying column top is communicated with the rich nitrogen inlet of precool heat exchanger device through subcooler 20, the rich nitrogen outlet of precool heat exchanger device is provided with two branch roads, article one, branch road is communicated with the regenerative dryer 5 outside ice chest, another branch road communication loop nitrogen suction port of compressor, methane rectifier is communicated with the liquid nitrogen storage tank 6 outside ice chest.
Carbon dioxide gas-liquid separator 19 is also provided with in described ice chest, described carbon dioxide precooling device 19 is also provided with carbon dioxide entrance, carbon dioxide gas-liquid separator 19 bottom liquid stream outlet carbon dioxide precooling device 1, the entrance of carbon dioxide gas-liquid separator 19 is communicated with the carbon dioxide storage tank outside ice chest, and the top of carbon dioxide gas-liquid separator is all communicated with the carbon dioxide recovering apparatus outside ice chest with the carbon dioxide outlet of carbon dioxide precooling device; Described carbon dioxide gas-liquid separator 19 is also provided with overfall 19.1, and overfall 19.1 is positioned at the top of carbon dioxide gas-liquid separator entrance.
By pipeline communication between described each device, each segment pipe is provided with valve and instrument control point.
The recovery synthetic ammonia tailgas that the present embodiment provides produces the process of LNG, and concrete steps are:
1) dehydrogenation rectifying column rectifying: pressure feed gas and high pressure feed enter respectively by low-pressure tail gas entrance and high pressure exhaust gas entrance, pressure feed gas enters into dehydrogenation rectifying column carry out rectifying through precool heat exchanger device, dehydrogenation rectifying column reboiler successively, meanwhile high pressure feed enters into dehydrogenation rectifying column carry out rectifying through precool heat exchanger device, methane rectifying column reboiler, subcooler successively, 74% be methane in dehydrogenation rectifier bottoms liquid after rectifying, remainder is nitrogen, argon, hydrogen;
2) methane-rich liquid enters methane rectifying column: the temperature flowed out from dehydrogenation rectifier bottoms enters in the middle part of methane rectifying column for-132.97 DEG C of methane-rich liquids;
3) methane rectifying column rectifying: enter into methane rectifying column methane-rich liquid and carry out rectifying, Han Liang≤99.2% of methane in liquid at the bottom of tower after rectifying, this methane liquid finally flow in the LNG storage tank outside ice chest;
4) step 1) in the source of dehydrogenation rectifying column tower top low-temperature receiver: make above-mentioned steps 1) in dehydrogenation rectifying column top gas enter after subcooler is cooled to-171 DEG C, gas fraction liquefies, enter again in gas-liquid separator, the liquid separated participates in rectifying in tower by liquid level difference automatic back flow to dehydrogenation rectifier, and the composition of described dehydrogenation rectifying column top gas is: hydrogen, nitrogen, methane and argon gas.
5) make above-mentioned steps 4) in gas-liquid separator in the hydrogen-rich gas of hydrogeneous, nitrogen, methane, argon at top discharge from gas-liquid separator top and enter subcooler re-heat to-140 DEG C, through precool heat exchanger device re-heat to 5 DEG C cooling box, then enter into pressure-swing absorption apparatus after the further re-heat to 35 of the second cooler DEG C;
6) step 3) in the source of methane rectifying column tower top low-temperature receiver: the valve opening source nitrogen porch, nitrogen enters cyclic nitrogen compressor by boost in pressure, valve closing, then in the pressurized end supercharging of booster expansion turbine, ice chest is entered through the second cooler cooling, cool through carbon dioxide precooling in precool heat exchanger device, major part gas enters booster expansion turbine expanding end and expands, gas temperature after expansion is reduced to below methane boiling point, nitrogen after expansion is successively through subcooler, again cyclic nitrogen suction port of compressor is back to after the re-heat of precool heat exchanger device, so circulate in device inside and form the circulating nitrogen gas that backflows, continue to enter subcooler cooling from precool heat exchanger device cold junction residual gas out, gas is from subcooler out rear reducing pressure by regulating flow, temperature reduces, produce cryogenic liquid and enter rectifying in methane rectifier participation tower, and together discharge from tower top with the waste gas generated in tower, through subcooler, precool heat exchanger device re-heat cooling box, part with expand after the circulating nitrogen gas that backflows converge after be again recycled nitrogen compressor and suck and compress, redundance enters regenerative dryer as waste gas,
7) from methane rectifying column, the liquid nitrogen of rectifying flow in the liquid nitrogen storage tank outside ice chest.
The adjustment of booster expansion turbine expanding end inlet temperature regulates by extracting one temperature higher temperatures air-flow at precool heat exchanger device cold junction top place.
Claims (3)
1. one kind is reclaimed the device that synthetic ammonia tailgas produces LNG, it is characterized in that: precool heat exchanger device, booster expansion turbine, gas-liquid separator, dehydrogenation rectifying column and methane rectifying column that it comprises cyclic nitrogen compressor, the first cooler, the second cooler, the 3rd cooler and is arranged in ice chest, described precool heat exchanger device comprises carbon dioxide precooling device and main heat exchanger, described precool heat exchanger device is provided with high pressure exhaust gas entrance, low-pressure tail gas entrance, hydrogen rich gas exports, rich nitrogen outlet, the circulating nitrogen gas that backflows exports, high pressure nitrogen entrance, high pressure nitrogen exports, backflow circulating nitrogen gas entrance, rich nitrogen inlet, hydrogen rich gas entrance, low-pressure tail gas outlet and high pressure exhaust gas outlet, described high pressure exhaust gas entrance, low-pressure tail gas entrance, hydrogen rich gas exports, rich nitrogen outlet, the circulating nitrogen gas that backflows outlet is communicated with carbon dioxide precooling device respectively with high pressure nitrogen entrance, described high pressure nitrogen outlet, backflow circulating nitrogen gas entrance, rich nitrogen inlet, hydrogen rich gas entrance, low-pressure tail gas outlet is communicated with main heat exchanger respectively with high pressure exhaust gas outlet, described cyclic nitrogen suction port of compressor is communicated with the rich nitrogen outlet of source nitrogen and precool heat exchanger device, its outlet is communicated with booster expansion turbine pressurized end entrance through the first cooler, the outlet of booster expansion turbine pressurized end is communicated with the high pressure nitrogen entrance of precool heat exchanger device again, the high pressure nitrogen exit of precool heat exchanger device is provided with two branch roads, article one, branch road is communicated with booster expansion turbine expanding end entrance, the outlet of booster expansion turbine expanding end is communicated with the circulating nitrogen gas entrance that backflows of precool heat exchanger device again through subcooler, the circulating nitrogen gas that backflows exports communication loop nitrogen suction port of compressor again, another branch road is communicated with methane rectifier through subcooler, high pressure exhaust gas entrance and the low-pressure tail gas entrance of described precool heat exchanger device are communicated with synthesis source of the gas and periodic off-gases source respectively, the outlet of its low-pressure tail gas is communicated with dehydrogenation rectifying column inlet again through dehydrogenation rectifying column reboiler, and the outlet of its high pressure exhaust gas is successively in the middle part of methane rectifying column reboiler is communicated with dehydrogenation rectifying column again with subcooler, the methane-rich liquid outlet methane rectifying column inlet of dehydrogenation rectifier bottoms methane-rich liquid bottom dehydrogenation rectifying column reboiler, the LNG storage tank outside the liquefied natural gas outlet ice chest of methane rectifier bottoms liquefied natural gas bottom methane rectifying column reboiler, the hydrogen rich gas outlet of described dehydrogenation rectifying column top is communicated with gas-liquid separator entrance again through subcooler, liquid bottom gas-liquid separator is communicated with again dehydrogenation rectifier, the hydrogen rich gas outlet at gas-liquid separator top is communicated with the hydrogen rich gas entrance of precool heat exchanger device again through subcooler, the hydrogen rich gas outlet of precool heat exchanger device is communicated with the pressure-swing absorption apparatus outside ice chest through the second cooler, the rich nitrogen outlet at described methane rectifying column top is communicated with the rich nitrogen inlet of precool heat exchanger device through subcooler, the rich nitrogen outlet of precool heat exchanger device is provided with two branch roads, article one, branch road is communicated with the regenerative dryer outside ice chest, another branch road communication loop nitrogen suction port of compressor, methane rectifier is communicated with the liquid nitrogen storage tank outside ice chest.
2. recovery synthetic ammonia tailgas according to claim 1 produces the device of LNG, it is characterized in that: in described ice chest, be also provided with carbon dioxide gas-liquid separator, described carbon dioxide precooling device is also provided with carbon dioxide entrance, carbon dioxide gas-liquid separator bottom liquid stream outlet carbon dioxide precooling device, the entrance of carbon dioxide gas-liquid separator is communicated with the carbon dioxide storage tank outside ice chest, and the top of carbon dioxide gas-liquid separator is all communicated with the carbon dioxide recovering apparatus outside ice chest with the carbon dioxide outlet of carbon dioxide precooling device; Described carbon dioxide gas-liquid separator is also provided with overfall, and overfall is positioned at the top of carbon dioxide gas-liquid separator entrance.
3. recovery synthetic ammonia tailgas according to claim 1 produces the device of LNG, it is characterized in that: by pipeline communication between described each device, each segment pipe is provided with valve and instrument control point.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201420855200.0U CN204404693U (en) | 2014-12-30 | 2014-12-30 | Reclaim the device that synthetic ammonia tailgas produces LNG |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420855200.0U CN204404693U (en) | 2014-12-30 | 2014-12-30 | Reclaim the device that synthetic ammonia tailgas produces LNG |
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| CN204404693U true CN204404693U (en) | 2015-06-17 |
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| CN201420855200.0U Withdrawn - After Issue CN204404693U (en) | 2014-12-30 | 2014-12-30 | Reclaim the device that synthetic ammonia tailgas produces LNG |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104567276A (en) * | 2014-12-30 | 2015-04-29 | 杭州凯德空分设备有限公司 | Device and technological method for producing LNG (liquefied natural gas) by recycling ammonia tail gas |
| CN106146373A (en) * | 2016-06-06 | 2016-11-23 | 襄阳航力机电技术发展有限公司 | Reclaim cumene oxidation tail gas organic matter, the method for overbottom pressure waste heat and device thereof |
-
2014
- 2014-12-30 CN CN201420855200.0U patent/CN204404693U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104567276A (en) * | 2014-12-30 | 2015-04-29 | 杭州凯德空分设备有限公司 | Device and technological method for producing LNG (liquefied natural gas) by recycling ammonia tail gas |
| CN106146373A (en) * | 2016-06-06 | 2016-11-23 | 襄阳航力机电技术发展有限公司 | Reclaim cumene oxidation tail gas organic matter, the method for overbottom pressure waste heat and device thereof |
| CN106146373B (en) * | 2016-06-06 | 2018-04-03 | 襄阳航力机电技术发展有限公司 | Reclaim cumene oxidation tail gas organic matter, the method and its device of overbottom pressure waste heat |
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Granted publication date: 20150617 Effective date of abandoning: 20160817 |
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