CN2883330Y - Power-less ammonia recovery equipment - Google Patents
Power-less ammonia recovery equipment Download PDFInfo
- Publication number
- CN2883330Y CN2883330Y CNU200620012070XU CN200620012070U CN2883330Y CN 2883330 Y CN2883330 Y CN 2883330Y CN U200620012070X U CNU200620012070X U CN U200620012070XU CN 200620012070 U CN200620012070 U CN 200620012070U CN 2883330 Y CN2883330 Y CN 2883330Y
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- gas
- interchanger
- inlet
- liquid separator
- outlet
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 168
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 82
- 238000011084 recovery Methods 0.000 title claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 90
- 239000007789 gas Substances 0.000 claims description 47
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 18
- 239000001257 hydrogen Substances 0.000 claims description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims description 18
- 238000005262 decarbonization Methods 0.000 claims description 11
- 230000002194 synthesizing effect Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 13
- 235000011114 ammonium hydroxide Nutrition 0.000 description 10
- 238000001816 cooling Methods 0.000 description 6
- 238000005057 refrigeration Methods 0.000 description 5
- 230000006837 decompression Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Sorption Type Refrigeration Machines (AREA)
Abstract
The utility model discloses a high efficiency and energy saving un-powered ammonia recovery device, comprising an inlet/outlet pipe of an ammonia tank, a heat exchanger set, a gas-liquid separator set, an expansion set, a throttle valve set, exhaust pipes and an ammonia recovery tower. Ammonia is recovered from the tail ammonia released from the ammonia tank at a low temperature through the multi-stage heat exchanger and the gas-liquid separator with a throttle valve. The multi-level heat exchanger has cold air at low temperature supplied by the expansion set so as to obtain an even better recovery efficiency. The utility model can recover ammonia completely from the tail gas of ammonia synthesizing system, which not only increases the production output, reduces production cost but also eliminates ammonia pollution in the tail gas.
Description
Technical field
The utility model relates to a kind of tail gas treatment device, particularly a kind of unpowered ammonia recovery system.
Background technology
At present, ammonia content if directly discharge, not only caused waste generally 17～62% during the ammonia jar of synthesis ammonia system speeded to exit, and serious environment pollution.At present, ammonia during ammonia enterprise speeds to exit to the ammonia jar mostly reclaims, method is the ammonia jar to be speeded to exit up making ammoniacal liquor through washing, after steaming ammonia with high-temperature steam again ammonia is wherein reclaimed out, but the efficient that is to use this method recovery ammonia is not high and increased soft consumption and energy consumption again, and the ammoniacal liquor of lower concentration can't utilize especially.
The utility model content
At above-mentioned existing in prior technology problem and shortage, the purpose of this utility model provides a kind of energy-efficient unpowered input ammonia recovery system.The utility model is the operating pressure swell refrigeration that utilizes synthesis ammonia system tail gas itself, system temperature is reduced, thereby the high boiling material ammoniacal liquor in the off-gas is divided from coming out to reach the recovery purpose.Use this equipment under the situation of cold affluence, the high-pressure liquid ammonia that is recovered to directly to be sent to the storage of ammonia groove.Can be with the gas ammonia of lower pressure by behind the heat exchanger under the not rich situation of cold, the recovery part cold be sent native system again.Whole plant need not the extra power input, and the ammonia organic efficiency has good economic benefit up to more than 99%.
The utility model is achieved in that a kind of unpowered ammonia recovery system, comprise ammonia jar off-gas inlet pipe, heat exchanger package, the gas-liquid separator group, the expansion unit, the throttling valve group, vapor pipe and ammonia withdrawing can, wherein said heat exchanger package comprises the interchanger more than two or two, every interchanger is provided with one or more than one hot media channels and one or more than one cold medium channel, described throttling valve group comprises one or more throttling valve, described gas-liquid separator group comprises the gas-liquid separator more than two or two, every gas-liquid separator is provided with pneumatic outlet and liquid exit, the liquid exit of every gas-liquid separator connects a throttling valve, and described expansion unit comprises one or more decompressor;
First step exchanger heat medium channel inlet is connected with the off-gas inlet pipe, the outlet of this hot media channel connects the inlet of first step gas-liquid separator, the liquid exit of first step gas-liquid separator connects the throttling valve inlet by pipeline, the throttling valve outlet is entered the mouth by the cold medium channel that pipeline is connected to first step interchanger, and the outlet of this cold medium channel links to each other with the ammonia withdrawing can;
The pneumatic outlet of first step gas-liquid separator is connected to a hot media channel inlet of second stage interchanger by pipeline, the outlet of this hot media channel connects the inlet of second stage gas-liquid separator, the pneumatic outlet of second stage gas-liquid separator is connected with a hot media channel inlet of next stage (third stage) interchanger again by pipeline, second stage gas-liquid separator liquid exit is connected to the inlet of throttling valve by pipeline, the outlet of throttling valve enters the mouth by the cold medium channel that pipeline is connected to upper level (second stage) interchanger, and the outlet of this cold medium channel is connected to upper level (first step) gas-liquid separator liquid by pipeline and comes out by on the connecting pipeline behind the throttling valve; Being connected by that analogy of the interchanger of its back and gas-liquid separator;
The pneumatic outlet of last step gas-liquid separator is connected thereto the inlet of a cold medium channel of first-class heat exchanger, this cold medium channel can be connected with the inlet of decompressor through one-level or the above exchanger heat exchange back of one-level, the escape pipe of decompressor is connected to the inlet of a cold medium channel of last step interchanger, and this cold medium pipeline is connected with vapor pipe after passing all interchanger in front successively.The liquid exit of last step gas-liquid separator is connected to the inlet of throttling valve by pipeline, the outlet of throttling valve can connect a cold medium channel of upper level interchanger, this cold medium channel outlet comes out to be connected through the pipe connecting behind the throttling valve with upper level gas-liquid separator liquid again, also can directly come out to be connected through the pipe connecting behind the throttling valve with upper level gas-liquid separator liquid by pipeline.
The beneficial effect that the utility model can reach is:
1, utilize ammonia jar speed to exit self pressure swell refrigeration in decompressor, cool off the ammonia jar that just flows in the heat exchanger package and speed to exit and reach the purpose that reclaims ammonia, this equipment need not additionally to import power, greatly reduces energy consumption.
2, the purity of using this equipment recovery ammonia is greater than 99%, and it is different and different that the residual ammonia content during the ammonia jar behind the branch ammonia speeds to exit is located utilizable condition according to the user, generally can be less than 1%.
If 3 tail gas that can utilize high pressure emptying air film to carry hydrogen carry out ammonia as auxiliary cooling gas and reclaim, the total system operation can be more steady, and residual ammonia content can further reduce, or the ammonia that is recovered to can be high-pressure liquid ammonia.
Description of drawings
Fig. 1 is the unpowered ammonia recovery system synoptic diagram of the utility model embodiment 1;
Fig. 2 is the unpowered ammonia recovery system synoptic diagram of the utility model embodiment 2;
Fig. 3 is the unpowered ammonia recovery system synoptic diagram of the utility model embodiment 3;
Fig. 4 is the unpowered ammonia recovery system synoptic diagram of the utility model embodiment 4.
Embodiment
As shown in Figure 1, this is unpowered, and input ammonia recovery system comprises ammonia jar off-gas inlet pipe 1, heat exchanger package, gas-liquid separator group, expansion unit, throttling valve group and ammonia withdrawing can 6, described heat exchanger package comprise interchanger 2, interchanger 2 ' and interchanger 2 "; the gas-liquid separator group comprise gas-liquid separator 3, gas-liquid separator 3 ' and gas-liquid separator 3 ", the throttling valve group comprise throttling valve 5 and throttling valve 5 '.Ammonia jar off-gas inlet pipe 1 is connected with the hot media channel 21 of interchanger 2, the outlet of passage 21 is connected with the inlet of gas-liquid separator 3, the liquid exit 32 of separator 3 is connected with throttling valve 5, the outlet of throttling valve 5 connects the inlet of the cold medium channel 22 of interchanger 2, the outlet of cold medium channel 22 is connected with ammonia withdrawing can 6, the pneumatic outlet 31 of separator 3 and interchanger 2 ' hot media channel 2 ' 1 be connected, the outlet of hot media channel 2 ' 1 connect gas-liquid separator 3 ' inlet, separator 3 ' liquid exit 3 ' 2 and throttling valve 5 ' be connected, throttling valve 5 ' outlet connect interchanger 2 ' cold medium channel 2 ' 2, the outlet of passage 2 ' 2 is connected on the pipeline between throttling valve 5 and the passage 22, separator 3 ' pneumatic outlet 3 ' 1 and interchanger 2 " hot media channel 2 " 1 be connected, the inlet of passage 2 " 1 outlet connects gas-liquid separator 3 ", separator 3 " liquid exit 3 " 2 be connected to separator 3 ' liquid exit 3 ' 2 and throttling valve 5 ' between pipeline on, separator 3 " pneumatic outlet 3 " 1 connects the inlet of interchanger 2 " cold medium channel 2 " 2, passage 2 " 2 outlet connect interchanger 2 ' cold medium channel 2 ' 3; outlet of passage 2 ' 3 connects the inlet of decompressor 4; outlet of decompressor 4 connects the inlet of interchanger 2 " cold medium channel 2 " 3; passage 2 " 3 outlet connect interchanger 2 ' the inlet of cold medium channel 2 ' 4, the outlet of passage 2 ' 4 connects the inlet of the cold medium channel 23 of interchanger 2, and the outlet of passage 23 is connected with vapor pipe 7.
It is as follows that the utility model utilizes equipment shown in Figure 1 to carry out the technical process that ammonia reclaims:
1, the ammonia jar is speeded to exit and is entered the hot media channel 21 of interchanger 2 by inlet pipe 1, after in interchanger 2, cooling off, part ammonia becomes liquid and enters gas-liquid separator 3 by hot media channel 21, through separation the back ammonia liquor by the liquid exit 32 of separator 3 in throttling valve 5 decompression back inflow heat exchanger 2 cold medium channels 22, in interchanger 2, provide cold after inflow ammonia withdrawing can 6.
2, the gas in the gas-liquid separator 3 by pneumatic outlet 31 enter interchanger 2 ' hot media channel 2 ' 1 in, interchanger 2 ' in through overcooling laggard go into gas-liquid separator 3 ', through separation the back ammonia liquor by separator 3 ' liquid exit 3 ' 2 flow out by throttling valve 5 ' inflow heat exchanger 2 ' cold medium channel 2 ' 2, interchanger 2 ' in the ammonia that flows out again through throttling valve 5 decompressions with liquid exit 32 after cold is provided by gas-liquid separator 3 converge, together in the cold medium channel 22 of inflow heat exchanger 2, flow into ammonia withdrawing can 6 after in interchanger 2, providing cold.
3, the ammonia jar off-gas after gas-liquid separator 3 ' minute ammonia by separator 3 ' pneumatic outlet 3 ' 1 enter in the interchanger 2 " hot media channel 2 " 1, interchanger 2 " in through overcooling is laggard go into gas-liquid separator 3 ", through separation the back ammonia liquor by separator 3 " liquid exit 3 " 2 flow out with by gas-liquid separator 3 ' liquid exit 3 ' 2 effusive ammonia liquor converge, technical process thereafter with by gas-liquid separator 3 ' the technical process of liquid exit 3 ' 2 effusive ammonia liquor identical.
4, through the cold medium channel 2 of the pneumatic outlet 3 " 1 backflows successively into interchanger 2 " of gas-liquid separator 3 " the ammonia jar off-gas tail gas after dividing ammonia is by separator 3 " " 2 and interchanger 2 ' cold medium channel 2 ' 3; enter decompressor 4 swell refrigerations after cold is provided in interchanger; temperature reduce the back by the outlet of decompressor 4 backflow successively into interchanger 2 " cold medium channel 2 " 3, interchanger 2 ' cold medium channel 2 ' 4 and the cold medium channel 23 of interchanger 2, discharge by vapor pipe 7 behind the ammonia jar off-gas in the cooling heat exchanger hot media channel.
This equipment can reach the purpose that cold is provided and reclaims ammonia simultaneously
Freeze if use high pressure emptying air film in the synthesis ammonia system tail gas to carry hydrogen tail gas simultaneously, its recovering effect can be better.
As shown in Figure 2, compare with embodiment 1, present embodiment has increased high pressure emptying air film and has carried hydrogen tail gas and come auxiliary cooling.Interchanger 2 and interchanger 2 ' in set up a hot media channel 24 and 2 ' 5 respectively, the inlet of passage 24 with put forward hydrogen tail gas inlet pipe 8 and be connected, the outlet of passage 24 is connected with the inlet of passage 2 ' 5, and the outlet of passage 2 ' 5 is connected to decompressor 4 and passage 2 " on the pipeline between 2.As shown in Figure 2, at interchanger 2 " in set up a cold medium channel 2 " 4, " 4 inlet is connected the cold medium channel 2 that gas-liquid separator 3 " liquid exit 3 " 2 connects throttling valve 5 "; throttling valve 5 " outlet and interchanger 2 ", passage 2 " 4 outlet and throttling valve 5 ' and passage 2 ' 2 between pipe connection, cold medium thread a pipe 2 ' 2 outlet and ammonia withdrawing can 6 ' be connected.
It is as follows that the utility model utilizes equipment shown in Figure 2 to carry out the technical process that ammonia reclaims:
High pressure emptying air film carry hydrogen tail gas by carry hydrogen tail gas inlet pipe 8 enter successively hot media channel 24 in the interchanger 2 and interchanger 2 ' in hot media channel 2 ' 5, carry hydrogen tail gas and flow out, pass through interchanger 2 that " tail gas mixes behind the branch ammonia of re-heat; mixed gas enters in the decompressor 4 by pipeline, and is identical by the technical process of tail gas behind 4 effusive minutes ammonia of decompressor among the workflow of this mixed gas and the embodiment 1 by gas-liquid separator 3 " pneumatic outlet 3 " 1 through interchanger 2 and interchanger 2 ' cooled high pressure emptying air film.
By gas-liquid separator 3 " liquid exit 3 " 2 effusive ammonia liquor through the cold medium channel 2 " in 4; " of throttling valve 5 " decompression back inflow heat exchanger 2 " through interchanger 2 after the re-heat with the ammonia liquor of passing through throttling valve 5 ' decompression by gas-liquid separator 3 ' outflows converge inflow heat exchanger 2 together ' cold medium channel 2 ' 2 in, inflow ammonia withdrawing can 6 after interchanger 2 ' re-heat '.
Other technical process of present embodiment is identical with embodiment 1.
Removing decompressor 4 expansible gases is mixed gass that tail gas and high pressure emptying air film are carried hydrogen tail gas behind the branch ammonia, so expansion tolerance has increased, refrigerating duty has also increased.Use this equipment user can be recovered to the ammonia of different pressures.
If it is a lot of that high pressure emptying air film is put forward hydrogen tail gas amount, compare with embodiment 2, increased in the present embodiment use high pressure emptying air film carry hydrogen tail gas as the decompressor 4 of expanding gas '.As shown in Figure 3, decompressor 4 ' inlet mouth link to each other with the outlet of the hot media channel 24 of interchanger 2, decompressor 4 ' the air outlet connect interchanger 2 ' the inlet of cold medium channel 2 ' 4.
It is as follows that the utility model utilizes equipment shown in Figure 3 to carry out the technical process that ammonia reclaims:
High pressure emptying air film is carried hydrogen tail gas by carrying the hot media channel 24 that hydrogen tail gas inlet pipe 8 enters interchanger 2, after interchanger 2 precoolings, a part carry hydrogen tail gas enter interchanger 2 ' hot media channel 2 ' 5, through the cooling back of interchanger 2 ' further with pass through interchanger 2 " the branch ammonia tail gas of re-heat mixes, and enters the flow process that decompressor 4 carries out embodiment 2; Another part carry hydrogen tail gas enter new boost expander 4 ', cryogenic gas after decompressor 4 ' expansion and the mixed gas that backflows converge, together backflow enter successively interchanger 2 ' cold medium channel 2 ' 4 and the cold medium channel 23 of interchanger 2, cooling heat exchanger 2 ' and the hot media channel of interchanger 2 in gas, self temperature back that raises is discharged by vapor pipe 7.
The liquid ammonia that comes out from each gas-liquid separator liquid exit need not reduce pressure, backflow through or without heat exchanger package, flow into ammonia withdrawing can 6 with the form of high-pressure liquid ammonia.
Other technical process of present embodiment is identical with embodiment 1.
If it is very little or do not have that user's high pressure emptying air film is put forward hydrogen tail gas amount, then can use synthetic decarbonization to come swell refrigeration.
Compare with embodiment 1 and embodiment 2, increased in the present embodiment and used the decompressor 4 of decarbonization " as expanding gas.The outlet of as shown in Figure 4, decompressor 4 " air intake be connected decompressor 4 with decarbonization inlet pipe 9 " connects the inlet of the cold medium channel 25 of interchanger 2, and the outlet of passage 25 is connected with decarbonization vapor pipe 10.
It is as follows that the utility model utilizes equipment shown in Figure 4 to carry out the technical process that ammonia reclaims:
Decarbonization enters decompressor 4 by decarbonization inlet pipe 9 " in; descend through temperature behind the swell refrigeration; by decompressor 4 " outlet enter in the cold medium channel 25 of interchanger 2, gas in the hot media channel of cooling heat exchanger 2, self temperature back that raises is discharged by decarbonization vapor pipe 10.
Other technical process of present embodiment is identical with embodiment 2 with embodiment 1.
Claims (5)
1, a kind of unpowered ammonia recovery system, it is characterized in that, this equipment comprises ammonia jar off-gas inlet pipe, heat exchanger package, the gas-liquid separator group, the expansion unit, the throttling valve group, vapor pipe and ammonia withdrawing can, wherein said heat exchanger package comprises the interchanger more than two or two, every interchanger is provided with one or more than one hot media channels and one or more than one cold medium channel, described throttling valve group comprises one or more throttling valve, described gas-liquid separator group comprises the gas-liquid separator more than two or two, every gas-liquid separator is provided with pneumatic outlet and liquid exit, the liquid exit of every gas-liquid separator is connected with throttling valve, and described expansion unit comprises one or more decompressor;
The hot media channel inlet of first step interchanger is connected with the off-gas inlet pipe, the outlet of this hot media channel connects the inlet of first step gas-liquid separator, the liquid exit of first step gas-liquid separator connects the throttling valve inlet by pipeline, the throttling valve outlet enters the mouth by the cold medium channel that pipeline is connected to first step interchanger, and the outlet of this cold medium channel links to each other with the ammonia withdrawing can;
The pneumatic outlet of first step gas-liquid separator is connected to a hot media channel inlet of second stage interchanger by pipeline, the outlet of this hot media channel connects the inlet of second stage gas-liquid separator, the pneumatic outlet of second stage gas-liquid separator is connected with a hot media channel inlet of next stage interchanger again by pipeline, second stage gas-liquid separator liquid exit is connected to the inlet of throttling valve by pipeline, the outlet of throttling valve is connected to a cold medium channel inlet of upper level interchanger by pipeline, the outlet of this cold medium channel is connected to upper level gas-liquid separator liquid by pipeline and comes out by on the connecting pipeline behind the throttling valve, being connected by that analogy of interchanger thereafter and gas-liquid separator;
The pneumatic outlet of last step gas-liquid separator is connected thereto the inlet of a cold medium channel of first-class heat exchanger, this cold medium pipeline can be connected with the inlet of decompressor through one-level or the above exchanger heat exchange back of one-level, the outlet of decompressor is connected to the inlet of a cold medium channel of last step interchanger, and this cold medium pipeline is connected with vapor pipe after passing all interchanger in front successively.The liquid exit of last step gas-liquid separator is connected to the inlet of throttling valve by pipeline, and the outlet of throttling valve comes out to be connected through the pipe connecting behind the throttling valve with upper level gas-liquid separator liquid by a cold medium channel of prime interchanger.
2, unpowered ammonia recovery system according to claim 1, it is characterized in that, the liquid exit of described last step gas-liquid separator is connected to throttling valve by pipeline, and the outlet of this throttling valve directly comes out to be connected through the pipe connecting behind the throttling valve with upper level gas-liquid separator liquid by pipeline.
3, unpowered ammonia recovery system according to claim 1 and 2, it is characterized in that, this equipment also comprises puies forward hydrogen tail gas inlet pipe, a hot media channel inlet of this inlet pipe and first step interchanger is connected, and this hot media channel is connected with the inlet mouth of decompressor after passing the above interchanger of one-level or one-level.
4, unpowered ammonia recovery system according to claim 3, it is characterized in that, this equipment also comprises carries hydrogen tail gas decompressor, the hot media channel of the inlet of this decompressor by first interchanger with put forward hydrogen tail gas inlet pipe and be connected, the outlet of decompressor is connected with the inlet of a cold medium channel of second stage interchanger, the outlet of this cold medium channel links to each other with the inlet of a cold medium channel of first step interchanger, and the outlet of the cold medium channel of this first step interchanger is connected with vapor pipe.
5, unpowered ammonia recovery system according to claim 3, it is characterized in that, this equipment also comprises decarbonization vapor pipe, decarbonization inlet pipe and the decarbonization decompressor that links to each other with this inlet pipe, and this decompressor outlet links to each other with the decarbonization vapor pipe by a cold medium pipeline of first interchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200620012070XU CN2883330Y (en) | 2006-04-05 | 2006-04-05 | Power-less ammonia recovery equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200620012070XU CN2883330Y (en) | 2006-04-05 | 2006-04-05 | Power-less ammonia recovery equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2883330Y true CN2883330Y (en) | 2007-03-28 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU200620012070XU Expired - Fee Related CN2883330Y (en) | 2006-04-05 | 2006-04-05 | Power-less ammonia recovery equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2883330Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659135A (en) * | 2012-05-03 | 2012-09-12 | 内蒙古乌拉山化肥有限责任公司 | Method for reducing outlet temperature of secondary gas-liquid separator in process of starting ammonia recovery device |
-
2006
- 2006-04-05 CN CNU200620012070XU patent/CN2883330Y/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659135A (en) * | 2012-05-03 | 2012-09-12 | 内蒙古乌拉山化肥有限责任公司 | Method for reducing outlet temperature of secondary gas-liquid separator in process of starting ammonia recovery device |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: PHYSICAL CHEMISTRY TECHNOLOGY INST., CHINESE ACAD Free format text: FORMER OWNER: BEIJING KERUI SAISI GAS LIQUEFACTION TECHNOLOGY CO., LTD. Effective date: 20080222 |
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| C41 | Transfer of patent application or patent right or utility model | ||
| C53 | Correction of patent of invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Wang Wenchuan Inventor after: Yang Kejian Inventor after: Yang Zhongwei Inventor before: Wang Wenchuan Inventor before: Yang Kejian |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: WANG WENCHUAN; YANG KEJIAN TO: WANG WENCHUAN; YANG KEJIAN; YANG ZHONGWEI |
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| TR01 | Transfer of patent right |
Effective date of registration: 20080222 Address after: Beijing, Zhongguancun, Haidian District, No. 2, north, zip code: 100080 Patentee after: Technical Institute of Physics and Chemistry Chinese Academy of Sciences Address before: Beijing, Zhongguancun, Haidian District, No. 2, north, zip code: 100080 Patentee before: Beijing Cryosys Technical Company of Gas Liquefaction Co.,Ltd. |
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| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |