CN204039301U - A kind of carbonic acid gas stripping urea is expanded production device - Google Patents
A kind of carbonic acid gas stripping urea is expanded production device Download PDFInfo
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- CN204039301U CN204039301U CN201420404361.8U CN201420404361U CN204039301U CN 204039301 U CN204039301 U CN 204039301U CN 201420404361 U CN201420404361 U CN 201420404361U CN 204039301 U CN204039301 U CN 204039301U
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 58
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 239000004202 carbamide Substances 0.000 title claims abstract description 46
- 235000011089 carbon dioxide Nutrition 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 28
- 238000005406 washing Methods 0.000 claims abstract description 39
- 229960005286 carbaryl Drugs 0.000 claims abstract description 28
- -1 methyl carbomate Chemical compound 0.000 claims abstract description 28
- 238000004094 preconcentration Methods 0.000 claims abstract description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 15
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000003860 storage Methods 0.000 claims abstract description 7
- KXDHJXZQYSOELW-UHFFFAOYSA-M Carbamate Chemical compound NC([O-])=O KXDHJXZQYSOELW-UHFFFAOYSA-M 0.000 claims description 62
- 239000007788 liquid Substances 0.000 claims description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 11
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 238000003825 pressing Methods 0.000 claims description 3
- 238000005260 corrosion Methods 0.000 abstract description 6
- 230000007797 corrosion Effects 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 13
- 238000000034 method Methods 0.000 description 8
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 241000521257 Hydrops Species 0.000 description 1
- 206010030113 Oedema Diseases 0.000 description 1
- 241000269799 Perca fluviatilis Species 0.000 description 1
- BVCZEBOGSOYJJT-UHFFFAOYSA-N ammonium carbamate Chemical compound [NH4+].NC([O-])=O BVCZEBOGSOYJJT-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- KXDHJXZQYSOELW-UHFFFAOYSA-N carbonic acid monoamide Natural products NC(O)=O KXDHJXZQYSOELW-UHFFFAOYSA-N 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Classifications
-
- 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
- Y02P20/141—Feedstock
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a kind of carbonic acid gas stripping urea to expand production device, comprise carbon dioxide air source, liquid ammonia storage tank, high-pressure system, medium voltage network and lp system, described medium voltage network comprises middle pressure stripping tower, mid pressure methyl carbomate condenser group, middle pressure washing tower, vacuum pre-concentration interchanger, washing pump.The utility model aims to provide a kind ofly can improve urea production, system corrosion is little, urea concentration is high, the carbonic acid gas stripping urea of stable yield is expanded production device.
Description
Technical field
The utility model relates to carbon dioxide stripping process and produces the device field, particularly a kind of carbonic acid gas stripping urea of urea and to expand production device.
Background technology
Urea generates by following reaction formula under 170 ~ 185 DEG C and 13.5 ~ 14.5MPa condition with liquefied ammonia and carbon dioxide.
2NH3 (gas)+CO2 (gas) → NH2COONH4 (liquid)
NH2COONH4 (liquid) → CO (NH2) 2 (liquid)+H2O (liquid)
In first reaction formula, carbonic acid gas and ammonia generate first ammonium, react fast and heat release; In second reaction formula, the dehydration of first ammonium generates urea and water, reacts slow and heat absorption.
In the prior art, carbonic acid gas stripping urea plant is by the restriction of high-pressure system, the particularly constraint of high-pressure stripper, its design loading is 70% ~ 115% of normal value, when exceeding design maximum, steam stripping efficiency can decline to a great extent, stripping tower liquid level meeting big ups and downs, high-pressure system superpressure, gas phase band liquid; When lower than design minimum value, can bias current be there is in stripping tower, first ammonium liquid can not be uniformly distributed film forming at stripping tube, equipment corrosion aggravates, initiation potential, traditional carbonic acid gas stripping technique is only provided with high-pressure synthesis system and low pressure recycle system, although overall procedure is relatively short, but turndown ratio is little, it is very limited that energy potentiality are expanded in volume increase.
Along with the development of technology, medium voltage network is expanded production and is used, but still there is certain problem, as pipeline corrosion is excessive, and the problems such as system throughput is unstable, urea concentration is difficult.
Utility model content
The purpose of this utility model is to provide a kind ofly can improve urea production, system corrosion is little, urea concentration is high, the carbonic acid gas stripping urea of stable yield is expanded production device.
The technical scheme that the utility model provides is: a kind of carbonic acid gas stripping urea is expanded production device, comprise carbon dioxide air source, liquid ammonia storage tank, high-pressure system, medium voltage network and lp system, described medium voltage network comprises middle pressure stripping tower, mid pressure methyl carbomate condenser group, middle pressure washing tower, vacuum pre-concentration interchanger, washing pump, the top of described middle pressure stripping tower is provided with the entrance of the urea soln from high-pressure system, the bottom of described middle pressure stripping tower is connected with carbon dioxide air source, the bottom of described middle pressure stripping tower is provided with urea soln outlet, the top of described middle pressure stripping tower is provided with pneumatic outlet, the entrance of described vacuum pre-concentration interchanger is connected with the liquid exit of the low pressure carbamate condenser of lp system by middle pressure first ammonium pump, the entrance of described vacuum pre-concentration interchanger is also connected with the pneumatic outlet of middle pressure stripping tower, described vacuum pre-concentration heat exchanger exit is connected with the entrance of mid pressure methyl carbomate condenser group, the pneumatic outlet of described mid pressure methyl carbomate condenser group is connected with middle pressure wash tower bottoms entrance, the liquid exit of described mid pressure methyl carbomate condenser group is connected with the entrance of the High Pressure Carbamate pump of high-pressure system, the top of described middle pressure washing tower is provided with liquid inlet, the liquid inlet of described middle pressure washing tower is connected by the outlet at bottom of washing pump with the low-pressure absorption tower of lp system, the bottom liquid outlet of described middle pressure washing tower is connected with the entrance of mid pressure methyl carbomate condenser group, the middle part of described middle pressure stripping tower is provided with one for the air line of pressing input air in stripping tower in described, the synthetic tower diameter of described high-pressure system is 2600 ~ 2700mm, height is 27800 ~ 27900mm, volume is 150 ~ 160 cubic metres, 18 pieces of tower trays are provided with in described synthetic tower, 1100 ~ 1200 tubulations are distributed with in described middle pressure stripping tower.
Expand production in device at above-mentioned carbonic acid gas stripping urea, described mid pressure methyl carbomate condenser group is the first carbamate condenser and second Carbamate Condenser of series connection, described vacuum pre-concentration heat exchanger exit is connected with the entrance of the first carbamate condenser, the pneumatic outlet of the first described carbamate condenser is connected with the entrance of the second Carbamate Condenser, the entrance of the second described Carbamate Condenser is also connected with the bottom liquid outlet of middle pressure washing tower, the liquid exit of the second described Carbamate Condenser is connected with the entrance of the first carbamate condenser, the liquid exit of the first described carbamate condenser is connected with the entrance of the High Pressure Carbamate pump of high-pressure system.
Expand production in device at above-mentioned carbonic acid gas stripping urea, also comprise recirculated water cooling cutter, described water recirculator is used for the cold cut recirculated water cold cut by the first carbamate condenser and the second Carbamate Condenser, and the heat interchanging area of described water recirculator is 566 square metres.
Expand production in device at above-mentioned carbonic acid gas stripping urea, the heat interchanging area of the first described Carbamate Condenser is 382 ~ 385 square metres, and the heat interchanging area of the second described Carbamate Condenser is 295 ~ 300 square metres.
Expand production in device at above-mentioned carbonic acid gas stripping urea, the volume of described middle pressure washing tower is 2.35 cubic metres.
Expand production in device at above-mentioned carbonic acid gas stripping urea, the quantity of described washing pump is two, and described washing pump arranges in parallel.
Expand production in device at above-mentioned carbonic acid gas stripping urea, the heat interchanging area of described middle pressure stripping tower is 520 square metres.
Expand production in device at above-mentioned carbonic acid gas stripping urea, the flow of described high pressure carbamate pump is 16 ~ 35 cubes ms/h.
By above-mentioned improvement, the output of urea is brought up to 1700 tons from daily output 1300 tons, by setting up middle pressure stripping tower and corresponding equipment, improve steam stripping efficiency, system running is stablized.In order to avoid high density first ammonium is to the corrosion of pipeline, introduce an air line in the tower side of middle pressure stripping tower, make the oxygen level in tower maintain certain level, reduce the pipeline corrosion of medium voltage network.Meanwhile, in the synthetic tower of high-pressure system, replace original tower tray with novel radial-flow type high-efficient tower plate, number of trays increases, and makes the transformation efficiency in synthetic tower tower improve 1% ~ 2% on the original basis, and then reduces the urea concentration difficulty of medium voltage network.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present utility model.
Embodiment
Below in conjunction with embodiment, the technical solution of the utility model is described in further detail, but does not form any restriction of the present utility model.
Embodiment 1
As shown in Figure 1, a kind of carbonic acid gas stripping urea is expanded production device, comprise carbon dioxide air source, liquid ammonia storage tank, high-pressure system, medium voltage network and lp system, carbon dioxide air source is carbon dioxide compressor h, described medium voltage network comprises middle pressure stripping tower 1, mid pressure methyl carbomate condenser group 2, middle pressure washing tower 3, vacuum pre-concentration interchanger 4, washing pump 5, the top of described middle pressure stripping tower 1 is provided with the entrance of the urea soln from high-pressure system, the bottom of described middle pressure stripping tower 1 is connected with carbon dioxide air source, the bottom of described middle pressure stripping tower 1 is provided with urea soln outlet, the top of described middle pressure stripping tower 11 is provided with pneumatic outlet, the entrance of described vacuum pre-concentration interchanger 4 is connected with the liquid exit of the low pressure carbamate condenser of lp system by middle pressure first ammonium pump b, the entrance of described vacuum pre-concentration interchanger 4 is also connected with the pneumatic outlet of middle pressure stripping tower 1, described vacuum pre-concentration interchanger 4 exports and is connected with the entrance of mid pressure methyl carbomate condenser group 2, the pneumatic outlet of described mid pressure methyl carbomate condenser group 2 is connected with middle pressure washing tower 3 bottom inlet, the liquid exit of described mid pressure methyl carbomate condenser group 2 is connected with the entrance of the High Pressure Carbamate pump of high-pressure system, the top of described middle pressure washing tower 3 is provided with liquid inlet, the liquid inlet of described middle pressure washing tower 3 is connected with the outlet at bottom of the low-pressure absorption tower a of lp system by washing pump 5, the bottom liquid outlet of described middle pressure washing tower 3 is connected with the entrance of mid pressure methyl carbomate condenser group 2, the middle part of described middle pressure stripping tower 1 is provided with one for the air line of pressing input air in stripping tower 1 in described, a high-pressure air storage tank f is set specifically, middle pressure stripping tower 1 input air is thought by high-pressure air storage tank f, the synthetic tower d diameter of described high-pressure system is 2600 ~ 2700mm, height is 27800 ~ 27900mm, volume is 150 ~ 160 cubic metres, 18 pieces of tower trays are provided with in described synthetic tower d, 1100 ~ 1200 tubulations are distributed with in described middle pressure stripping tower 1, wherein, described mid pressure methyl carbomate condenser group 2 is the first carbamate condenser 21 and the second Carbamate Condenser 22 of series connection, described vacuum pre-concentration interchanger 4 exports and is connected with the entrance of the first carbamate condenser 21, the pneumatic outlet of the first described carbamate condenser 21 is connected with the entrance of the second Carbamate Condenser 22, the entrance of the second described Carbamate Condenser 22 is also connected with the bottom liquid outlet of middle pressure washing tower 3, the liquid exit of the second described Carbamate Condenser 22 is connected with the entrance of the first carbamate condenser 21, the described liquid exit of the first carbamate condenser 21 is connected with the entrance of the High Pressure Carbamate pump of high-pressure system.
In the present embodiment, also comprise water recirculator 6, described water recirculator 6 is for the cold cut recirculated water cold cut by the first carbamate condenser 21 and the second Carbamate Condenser 22, the heat interchanging area of described water recirculator 6 is 566 square metres, the heat interchanging area of the first described Carbamate Condenser 21 is 382.4 square metres, the heat interchanging area of the second described Carbamate Condenser 22 is 298.7 square metres, the volume of described middle pressure washing tower 3 is 2.35 cubic metres, the quantity of described washing pump 5 is two, described washing pump 5 arranges in parallel, the heat interchanging area of described middle pressure stripping tower 1 is 520 square metres, the flow of described high pressure carbamate pump i is 16 ~ 35 cubes ms/h.
Specifically, the urea soln of a part of urea soln of the synthetic tower d of high-pressure system and the stripping tower of high-pressure system enters middle pressure stripping tower 1 top, the carbonic acid gas that carbon dioxide compressor h comes enters bottom middle pressure stripping tower 1, exchanged and step-down by gas-liquid, first ammonium in urea soln is decomposed, the rectifying tower g that the bottom liquid of middle pressure stripping tower 1 sends to lp system purifies further, the carbonic acid gas decomposed, ammonia, the pneumatic outlet at stripping tower 1 top is pressed to enter vacuum pre-concentration interchanger 4 in the mixed gas warps such as hydrogen, simultaneously lp system low pressure carbamate condenser c urea soln and the urea soln of rectifying tower g also enter vacuum pre-concentration interchanger 4 and carry out cooling heat exchange, then the part solution of vacuum pre-concentration interchanger 4 enters in the first mid pressure methyl carbomate condenser and absorbs gas, urea storage tank j is sent into after the part solution of vacuum pre-concentration interchanger 4 goes flash tank 7 to carry out flash concentration, the gas do not absorbed completely enters in the second mid pressure methyl carbomate condenser 22 and continues to absorb, the gas do not absorbed completely enters middle pressure washing tower 3 and washs, heat exchange is carried out with the ammoniacal liquor from low-pressure absorption tower a in middle pressure washing tower 3, absorb further gas, the low pressure carbamate condenser c that the gas do not absorbed completely sends to lp system absorbs.The bottom liquid of middle pressure washing tower 3 enters in the second carbamate condenser 22 and absorbs gas as absorption liquid, then enters the first carbamate condenser 21 and absorbs gas as absorption liquid.The liquid of the first mid pressure methyl carbomate condenser 21 sends into high pressure carbamate pump i.First the cooled recirculated water that recirculated water cooling condenser produces enter the second mid pressure methyl carbomate condenser 22, enter the first mid pressure methyl carbomate condenser 21 as refrigerant from the water outlet of the second mid pressure methyl carbomate condenser 22, finally get back to recirculated water cooling condenser 6 pairs of recirculated waters and lower the temperature.
Driving flow process: 1, normal procedure is pressed to high-pressure system and lp system and drive, after stable conditions, check medium voltage network pipeline, guarantee unimpeded, the pipeline of emphasis inspection is, synthetic tower d to middle pressure stripping tower 1, high-pressure stripper e to middle pressure stripping tower 1, the rectifying tower g of middle pressure stripping tower 1 to lp system, middle pressure washing tower 3 gas phase coldly to cut to low pressure carbamate condenser c, high pressure carbamate pump i to high pressure methylamine, middle pressure first ammonium pump b entrance.
2, set up steam system, to middle pressure stripping tower 1 steam hydrops groove topping up to 10%, slowly open into steam by-pass, control into intercepting basin steam flow, slowly pressure-controlling is thrown after 0.8MPa automatic control,
2.3 set up tempered water system
Open after pressure tempered water enters phlegma valve straight lofty perch emptying water outlet and close, press temperature adjustment water meter in startup, slowly open low-pressure steam to tempered water valve, tempered water temperature is controlled close after 75 degrees Celsius.
2.4 pressurising
Open and export into middle pressure decomposition tower valve from CO2 compressor h tri-sections, reach after 0.7MPa until pressure and open middle pressure washing tower 3 gas phase to low pressure carbamate condenser c variable valve throwing automatic control.
2.5 topping up
Press washing pump 5 to mid pressure methyl carbomate condenser topping up to liquid level 50% in unlatching.
2.6 high first pump inlets change middle pressure
Open low pressure carbamate condenser c to middle pressure first ammonium pump b imported valve, press first ammonium pump b in startup, main line send mid pressure methyl carbomate condenser.Open middle pressure condenser and enter high pressure carbamate pump i valve, close low-pressure condenser valve (speed wants fast, prevents low pressure superpressure), main line walks former flow process.Restart newly-increased high pressure carbamate pump i, main line send in hp ammonium carbamate condenser liquid distributor.
2.7 punishment in advance
Slowly open synthetic tower d, high-pressure stripper e enters middle pressure stripping tower 1 variable valve, for preventing medium voltage network superpressure, speed is wanted slowly.After middle pressure decomposition tower has liquid level to show, regulate into tower carbon dioxide flow 150-300 cubes ms/h, Non-follow control intercepting basin enters steam valve and Liquid level adjusting valve, guarantees that middle pressure stripping tower 1 goes out liquid temp at 155-160 DEG C, throws automatic control.Open low-pressure distillation tower g variable valve after middle pressure stripping tower 1 liquid level to 30%, Liquid level is at 30%-40%.In slow adjustment, pressure pressure is at 1.75MPa, and mid pressure methyl carbomate condenser Liquid level is 50% one 80%.
After technological transformation is driven, the condition of production is stablized, and equipment normal operation, every technic index is qualified.Output reaches 1750 tons, and most high energy reaches 1770 tons, and ammonia consumes 575 kilograms, and steam consumes 0.95 ton, and middle pressure device is easy to operate, can be incorporated to and produces and exit production, do not affect former technical process according to front workshop section load variations.
Above-describedly be only preferred embodiment of the present utility model, all do in spirit of the present utility model and spirit any amendment, equivalently to replace and improvement etc., all should be included within protection domain of the present utility model.
Claims (8)
1. a carbonic acid gas stripping urea is expanded production device, comprise carbon dioxide air source, liquid ammonia storage tank, high-pressure system, medium voltage network and lp system, it is characterized in that, described medium voltage network comprises middle pressure stripping tower, mid pressure methyl carbomate condenser group, middle pressure washing tower, vacuum pre-concentration interchanger, washing pump, the top of described middle pressure stripping tower is provided with the entrance of the urea soln from high-pressure system, the bottom of described middle pressure stripping tower is connected with carbon dioxide air source, the bottom of described middle pressure stripping tower is provided with urea soln outlet, the top of described middle pressure stripping tower is provided with pneumatic outlet, the entrance of described vacuum pre-concentration interchanger is connected with the liquid exit of the low pressure carbamate condenser of lp system by middle pressure first ammonium pump, the entrance of described vacuum pre-concentration interchanger is also connected with the pneumatic outlet of middle pressure stripping tower, described vacuum pre-concentration heat exchanger exit is connected with the entrance of mid pressure methyl carbomate condenser group, the pneumatic outlet of described mid pressure methyl carbomate condenser group is connected with middle pressure wash tower bottoms entrance, the liquid exit of described mid pressure methyl carbomate condenser group is connected with the entrance of the High Pressure Carbamate pump of high-pressure system, the top of described middle pressure washing tower is provided with liquid inlet, the liquid inlet of described middle pressure washing tower is connected by the outlet at bottom of washing pump with the low-pressure absorption tower of lp system, the bottom liquid outlet of described middle pressure washing tower is connected with the entrance of mid pressure methyl carbomate condenser group, the middle part of described middle pressure stripping tower is provided with one for the air line of pressing input air in stripping tower in described, the synthetic tower diameter of described high-pressure system is 2600 ~ 2700mm, height is 27800 ~ 27900mm, volume is 150 ~ 160 cubic metres, 18 pieces of tower trays are provided with in described synthetic tower, 1100 ~ 1200 tubulations are distributed with in described middle pressure stripping tower.
2. carbonic acid gas stripping urea according to claim 1 is expanded production device, it is characterized in that, described mid pressure methyl carbomate condenser group is the first carbamate condenser and second Carbamate Condenser of series connection, described vacuum pre-concentration heat exchanger exit is connected with the entrance of the first carbamate condenser, the pneumatic outlet of the first described carbamate condenser is connected with the entrance of the second Carbamate Condenser, the entrance of the second described Carbamate Condenser is also connected with the bottom liquid outlet of middle pressure washing tower, the liquid exit of the second described Carbamate Condenser is connected with the entrance of the first carbamate condenser, the liquid exit of the first described carbamate condenser is connected with the entrance of the High Pressure Carbamate pump of high-pressure system.
3. carbonic acid gas stripping urea according to claim 2 is expanded production device, it is characterized in that, also comprise recirculated water cooling cutter, described water recirculator is used for the cold cut recirculated water cold cut by the first carbamate condenser and the second Carbamate Condenser, and the heat interchanging area of described water recirculator is 566 square metres.
4. carbonic acid gas stripping urea according to claim 2 is expanded production device, and it is characterized in that, the heat interchanging area of the first described Carbamate Condenser is 382 ~ 385 square metres, and the heat interchanging area of the second described Carbamate Condenser is 295 ~ 300 square metres.
5. carbonic acid gas stripping urea according to claim 1 is expanded production device, and it is characterized in that, the volume of described middle pressure washing tower is 2.35 cubic metres.
6. carbonic acid gas stripping urea according to claim 1 is expanded production device, and it is characterized in that, the quantity of described washing pump is two, and described washing pump arranges in parallel.
7. carbonic acid gas stripping urea according to claim 1 is expanded production device, and it is characterized in that, the heat interchanging area of described middle pressure stripping tower is 520 square metres.
8. carbonic acid gas stripping urea according to claim 1 is expanded production device, and it is characterized in that, the flow of described high pressure carbamate pump is 16 ~ 35 cubes ms/h.
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| CN201420404361.8U CN204039301U (en) | 2014-07-22 | 2014-07-22 | A kind of carbonic acid gas stripping urea is expanded production device |
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| CN201420404361.8U CN204039301U (en) | 2014-07-22 | 2014-07-22 | A kind of carbonic acid gas stripping urea is expanded production device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110388638A (en) * | 2019-08-01 | 2019-10-29 | 河南晋开化工投资控股集团有限责任公司 | A kind of steam thermal energy utilization process in carbon dioxide stripping their urea production |
| CN114409573A (en) * | 2022-01-05 | 2022-04-29 | 中国五环工程有限公司 | Improved low energy CO2Urea process by steam stripping method |
-
2014
- 2014-07-22 CN CN201420404361.8U patent/CN204039301U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110388638A (en) * | 2019-08-01 | 2019-10-29 | 河南晋开化工投资控股集团有限责任公司 | A kind of steam thermal energy utilization process in carbon dioxide stripping their urea production |
| CN110388638B (en) * | 2019-08-01 | 2020-11-03 | 河南晋开化工投资控股集团有限责任公司 | Steam heat energy recycling process in urea production by carbon dioxide gas stripping method |
| CN114409573A (en) * | 2022-01-05 | 2022-04-29 | 中国五环工程有限公司 | Improved low energy CO2Urea process by steam stripping method |
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