CN101684082A - New recycling preseparation process of urea intermediate pressure system - Google Patents
New recycling preseparation process of urea intermediate pressure system Download PDFInfo
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- CN101684082A CN101684082A CN200810156087A CN200810156087A CN101684082A CN 101684082 A CN101684082 A CN 101684082A CN 200810156087 A CN200810156087 A CN 200810156087A CN 200810156087 A CN200810156087 A CN 200810156087A CN 101684082 A CN101684082 A CN 101684082A
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- heat energy
- preseparator
- distillation column
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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
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The invention belongs to the field of chemical industries, in particular to a new recycling preseparation process of a urea intermediate pressure system. A urea synthesizing tower is connected with apreseparator; the lower end of the preseparator is connected with the upper end of a pre-distillation tower; a first partial heater is connected with the lower end of the pre-distillation tower; the bottom end of the pre-distillation tower is connected with a second partial tower; the upper end of the pre-distillation tower is connected with a heat energy recovering section at the lower end of a first section evaporator by a pipeline and also connected with the lower end of a heat energy utilizing section of a flash evaporation heat exchanger by the heat energy recovering section of the firstsection evaporator; the heat energy utilizing section is connected with a cold absorber by a pipeline; and the upper end of the preseparator is connected with the pipeline of the heat energy utilizingsection of the flash evaporation heat exchanger by a pipeline. The components are mutually connected into integration and the new intermediate pressure recycling preseparation process is adopted; thesynthetic fluid of the urea synthesizing tower contains amine carbamate excess ammonia and water, and the amine carbamate excess ammonia and the water need to be separated from urine in a decompression heating way and then recycled, thereby not only saving a plurality of steam , but also achiveing the beneficial effects of energy saving and discharge reduction.
Description
Technical field
The invention belongs to the chemical industry field, relate to circulation and recovery process in a kind of urea production process, the pre-separation new process is reclaimed in particularly a kind of circulation of urea medium voltage network.
Background technology
Along with social progress and industry develop fast, obtained good economic benefit, the pollution that has simultaneously also brought environment influences existent environment of people, only one earth in the world, the pollution of environment has caused the concern of countries in the world government.The reform and opening-up preferential policy of China has been accelerated the emergence of China's industry, and simultaneously: industry has also brought environmental pollution; and causing the great attention of China governments at all levels, energy-saving and emission-reduction have been stood into state basic policy, make people have the ideology of energy-saving, emission-reducing, environment friendly; the protection environment is protected the home exactly.Particularly chemical enterprise more possesses the environmental consciousness and the sense of duty of height, to the source of pollution of production chemical product, accomplish energy-saving and emission-reduction, particularly water solution total cycling method is produced the middle pressure recirculation system of urea, former employing fore-distillation technology, steam consumption is big, and after load strengthened, it is bad that middle pressure is decomposed effect, wasted a large amount of energy again, operation is difficult to control again, has also caused gas leakage sometimes, has brought local pollution.
Summary of the invention
The objective of the invention is to overcome above deficiency, provide a kind of urea medium voltage network circulation to reclaim the pre-separation new process, urea synthesizer is gone out the tower urine before advancing pre-distillation column, set up a kind of new preseparator, change the production technique that falls behind, a large amount of steams of recovery capable of circulation, save energy, reduce to pollute again, easy to operate, safety reaches the effect of energy-saving and emission-reduction, enhance productivity, improved the quality product of urea again.
The technical solution adopted for the present invention to solve the technical problems is: contain urea synthesizer, preseparator, one fen well heater, pre-distillation column, two fens towers, one section vaporizer, the heat exchange of flash evaporation device, one cold absorber is formed, urea synthesizer connects mutually with preseparator, the lower end of preseparator connects mutually with the upper end of pre-distillation column, well heater connect mutually with the lower end of pre-distillation column in one minute, the bottom of pre-distillation column connects mutually with two fens towers, the upper end of pre-distillation column connects with the lower end energy recovery section of one section vaporizer mutually by pipeline, energy recovery section by one section vaporizer connects mutually with the lower end of the heat energy utilization section of heat exchange of flash evaporation device again, the heat energy utilization section connects with a cold absorber mutually by pipeline, the upper end of preseparator connects mutually by the pipeline of pipeline with the heat energy utilization section of heat exchange of flash evaporation device, and it is as a whole to be that they interconnect into.
In producing urea process, adopted middle pressure circulation to reclaim the pre-separation novel process, in the synthetic liquid of urea synthesizer, contain carboxylamine amine, superfluous ammonia and water need be separated from urine by the mode of decompression heating, and recovery again circulates.Synthetic liquid enters in the pre-distillation column by the pressure controlled valve PRCA-204 1.70Mpa (table) that reduces pressure, synthetic liquid enters the heat exchange of flash evaporation device at this and carries out flash distillation, liquid phase is carried out the mass-and heat-transfer effect at the pre-distillation column with bubble cap plate composition and the gas of one fen well heater, make exhaust gas phase temperature reduce, going out the tower liquidus temperature increases, the liquid phase that goes out pre-distillation column enters one fen well heater, shell-side the latter heats with 1.25Mpa (table) saturation steam, heater temperature TRCA-301 was controlled at 160 ℃～165 ℃ in one minute, the rate of decomposition of carboxylamine amine reaches 89%, and total ammonia steam rate reaches 90%.Heating back material enters the separator of pre-distillation column bottom, carries out gas-liquid separation.Separator liquid level LRCA-302 by the automatic control of LRCA-302 variable valve, delivers to Er Fenta after the material decompression.Eject next gas from pre-distillation column, enter one section vaporizer bottom energy recovery section, the first ammonium liquid that comes from the diformazan pump also enters this energy recovery section, enter heat exchange of flash evaporation device heat energy utilization section then together, enter a cold absorber again, with water circulating pump de-mineralized water is sent into the cold absorber cooling that circulates, make gas further in a cold absorber condensation.Liquidus temperature is at 85-95 ℃ at the bottom of utilizing backflow ammonia control tower.Because a large amount of ammonia is separated in preseparator, alleviated the heating load of one fen well heater, reach and reduce water-content and the purpose of saving one fen well heater steam consumption in the exhaust gas body, reach energy-saving and emission-reduction, easy to operate, safety had both guaranteed quality product, increased economic efficiency again.
The invention has the beneficial effects as follows: urea synthesizer is gone out the tower urine before advancing pre-distillation column, set up a kind of new preseparator, changed the production technique of original backwardness, adopted middle pressure circulation to reclaim the pre-separation novel process, in the synthetic liquid of urea synthesizer, contain carboxylamine amine, superfluous ammonia and water, need separate from urine by the mode of decompression heating, recovery again circulates.Not only save a large amount of steam, reduce environmental pollution again, enhance productivity, improved the quality product of urea again, easy to operate, safety is saved cost, reaches the beneficial effect of energy-saving and emission-reduction again.
Description of drawings
Be in conjunction with the accompanying drawings and embodiments the present invention to be further described below
Pre-separation processing method process flow sheet is reclaimed in the circulation that among the figure is the urea medium voltage network
In the drawings: 1. urea synthesizer, 2. preseparator, 3. one fen well heater, 4. pre-distillation column, 5. two fens towers, 6. one section vaporizer, 7. heat exchange of flash evaporation device, a 8. cold absorber.
Embodiment
In the drawings: urea synthesizer 1 connects mutually with preseparator 2, the lower end of preseparator 2 connects mutually with the upper end of pre-distillation column 4, well heater 3 connect mutually with the lower end of pre-distillation column 4 in one minute, the bottom of pre-distillation column 4 connects mutually with two fens towers 5, the upper end of pre-distillation column 4 connects with the lower end energy recovery section of one section vaporizer 6 mutually by pipeline, energy recovery section by one section vaporizer 6 connects mutually with the lower end of the heat energy utilization section of heat exchange of flash evaporation device 7 again, the heat energy utilization section connects with a cold absorber 8 mutually by pipeline, the upper end of preseparator 2 connects mutually by the pipeline of pipeline with the heat energy utilization section of heat exchange of flash evaporation device 7, and it is as a whole to be that they interconnect into.
Urea synthesizer 1 is a large-scale jar shape object, and synthetic liquid is equipped with in the inside, and synthetic liquid contains urea, ammonium carbamate, superfluous ammonia and water.Enter preseparator 2 by the pressure controlled valve PIRCA-204 1.70MPa (table) that reduces pressure.Synthetic liquid carries out flash distillation at this, a large amount of ammonia is separated and heat exchange of flash evaporation device 7 liquid mixture of working off one's feeling vent one's spleen converges into a cold absorber 8, after liquid phase enters pre-distillation column 4 further flash distillations, liquid phase is carried out the mass-and heat-transfer effect at the rectifying section with bubble cap plate composition and the gas of one fen well heater 3, make exhaust gas phase temperature reduce, going out the tower liquidus temperature increases, and the liquid phase that goes out pre-distillation column 4 enters one fen well heater 3, in 1.25MPa (table) the saturation steam heating of the latter's shell-side.Go out one fen well heater 3 temperature T RCA-301 and be controlled at 160～165 ℃.The rate of decomposition of ammonium carbamate reaches 89%, and total ammonia steam rate reaches 90%.Heating back material enters the preseparator 2 of pre-distillation column bottom, carries out gas-liquid separation.Separator liquid level LRCA-302 is by the automatic control of LRCA-302 variable valve.Deliver to the effect of 5, two fens towers 5 of two fens towers after the material decompression, mainly, different with one fen well heater 3 pressure rating to heating, the decomposition of urine.CO from the gas that pre-distillation column 4 ejects
2Content fore-distillation technology is greatly improved, and enters first ammonium liquid mixing the carrying out thermopositive reaction that one section vaporizer, 6 bottom energy recovery Duan Houyu come from the diformazan pump, because CO
2The raising reaction fore-distillation technology of dividing potential drop is more complete, has emitted a large amount of heats, is used for heating the into urine of one section vaporizer 6, has reduced the thermal load of one section vaporizer 6, has saved a large amount of steam.Enter heat exchange of flash evaporation device 7 heat energy utilization sections then together, enter a cold absorber 8 again, de-mineralized water is sent into a cold absorber 8 cooling that circulates, make gas further in a cold absorber 8 condensations with water circulating pump, utilize backflow ammonia control tower at the bottom of liquidus temperature at 85-95 ℃.Because a large amount of ammonia is separated in preseparator, alleviated the heating load of one fen well heater 3, reach and reduce water-content and the purpose of saving one fen well heater 3 steam consumption in the exhaust gas body, make a large amount of steam be recycled recovery utilization.
Claims (1)
- The pre-separation new process is reclaimed in a kind of circulation of urea medium voltage network, contain urea synthesizer, preseparator, one fen well heater, pre-distillation column, two fens towers, one section vaporizer, the heat exchange of flash evaporation device, one cold absorber is formed, it is characterized in that: urea synthesizer connects mutually with preseparator, the lower end of preseparator connects mutually with the upper end of pre-distillation column, well heater connect mutually with the lower end of pre-distillation column in one minute, the bottom of pre-distillation column connects mutually with two fens towers, the upper end of pre-distillation column connects with the lower end energy recovery section of one section vaporizer mutually by pipeline, energy recovery section by one section vaporizer connects mutually with the lower end of the heat energy utilization section of heat exchange of flash evaporation device again, the heat energy utilization section connects with a cold absorber mutually by pipeline, the upper end of preseparator connects mutually by the pipeline of pipeline with the heat energy utilization section of heat exchange of flash evaporation device, and it is as a whole to be that they interconnect into.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810156087A CN101684082A (en) | 2008-09-25 | 2008-09-25 | New recycling preseparation process of urea intermediate pressure system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810156087A CN101684082A (en) | 2008-09-25 | 2008-09-25 | New recycling preseparation process of urea intermediate pressure system |
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| Publication Number | Publication Date |
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| CN101684082A true CN101684082A (en) | 2010-03-31 |
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| CN200810156087A Pending CN101684082A (en) | 2008-09-25 | 2008-09-25 | New recycling preseparation process of urea intermediate pressure system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103748071A (en) * | 2011-10-14 | 2014-04-23 | 斯塔米卡邦有限公司 | Urea finishing method |
-
2008
- 2008-09-25 CN CN200810156087A patent/CN101684082A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103748071A (en) * | 2011-10-14 | 2014-04-23 | 斯塔米卡邦有限公司 | Urea finishing method |
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Open date: 20100331 |