CN103418211B - Process and device for heat utilization of high-pressure temperature-regulation water in shell side of high pressure scrubber in production in urea steam stripping method - Google Patents
Process and device for heat utilization of high-pressure temperature-regulation water in shell side of high pressure scrubber in production in urea steam stripping method Download PDFInfo
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- CN103418211B CN103418211B CN201310372088.5A CN201310372088A CN103418211B CN 103418211 B CN103418211 B CN 103418211B CN 201310372088 A CN201310372088 A CN 201310372088A CN 103418211 B CN103418211 B CN 103418211B
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Abstract
The invention relates to a process and a device for heat utilization of high-pressure temperature-regulation water in a shell side of a high pressure scrubber in production in a urea steam stripping method. Heat of the high-pressure temperature-regulation water is used fully through multistage heat exchange by adopting the process procedure that the high-pressure temperature-regulation water is delivered while being supplemented. After heat exchange is conducted on the high-pressure temperature-regulation water in the shell side of the high pressure scrubber and methyl ammonium solution in a tube side of the high pressure scrubber, urea is added to the high-pressure temperature-regulation water in a combined mode to enter a rectifying tower, wherein heat exchange is conducted on urea solution and the high-pressure temperature-regulation water in the shell side through the tube side, the high-pressure temperature-regulation water after having heat exchange in the rectifying tower is conveyed to a copper liquid heater in a synthesis ammonia refining workshop section to have heat exchange, and finally hot water is recovered through a deaerator. The process makes reasonable use of the heat, saves steam, relieves the load of a circulating water system, and meanwhile guarantees the quality of the water used for the high pressure scrubber.
Description
Technical field
The present invention relates to urea vaporizing extract process produce mesohigh washer shell side to a high-profile hydro-thermal utilize technique and equipment thereof, the technological process adopting benefit limit, limit to send reaches through multi-stage heat exchanger the effect that hydro-thermal amount to a high-profile makes full use of.
Background technology
The effect of high pressure scrubber is the first ammonium salt solution come by low pressure absorption cycle system sent here by high pressure carbamate pump, absorbs the unreacted NH that urea synthesizer gas phase is come in a high voltage state
3and CO
2, make NH
3and CO
2directly absorbed in high-pressure system, recycled.First ammonium liquid is produced by the gas phase of low pressure carbamate condenser cooling and absorbing rectifying column decomposing urea, first ammonium mixed liquor.This complex process, heat energy loss is large, greatly consumes steam, in the process simultaneously used in this technique, there is pipeline and occurs potential safety hazard because vapour-liquid carries problems such as producing vibration secretly.
Summary of the invention
The object of the present invention is to provide a kind of urea vaporizing extract process to produce mesohigh washer shell side lofty tone hydro-thermal and utilize technique, the technological process adopting benefit limit, limit to send reduces the consumption of steam in production process, alleviate circulation load, ensure high pressure scrubber shell side water quality.
The object of the present invention is achieved like this, urea vaporizing extract process is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized technique, the technological process that high pressure scrubber shell side water under high pressure adopts benefit limit, limit to send, make temperature reach 135-140 DEG C by after the first ammonium liquid heat exchange of the high water transfer in the high pressure scrubber shell side of 120 DEG C and high pressure scrubber tube side, discharge is 180m
3/ h, passes into urea synthesizing rectifying column by the water after heat exchange, and wherein urine is through the high water transfer heat exchange of tube side and shell side, and the flow after heat exchange is 180m
3/ h, temperature is 120-125 DEG C, the high water transfer after rectifying column heat exchange by pipeline with 14m
3the flow of/h delivers to the copper liquid heater heat exchange of synthetic ammonia refining workshop section, and after heat exchange, water temperature is 85-100 DEG C, flow 14 m
3/ h, the oxygen-eliminating device that high water transfer sends into refining workshop section through tube side reclaims hot water, for synthesis ammonia system after oxygen-eliminating device deoxygenation.
The temperature adopting water cooler recirculated water to a high-profile to maintain high water transfer after high water transfer heat exchange in described high pressure scrubber shell side is 135-140 DEG C, and wherein the flow of water cooler recirculated water is 200m to a high-profile
3/ h.
Adopt steam condensate to regulate and control after high water transfer heat exchange in described high pressure scrubber shell side and keep discharge to be 180m
3/ h, wherein the temperature of steam condensate is 80-90 DEG C, fills into 14m to condensate liquid simultaneously
3the secondary desalted water of/h.
Another object of the present invention is to provide a kind of urea vaporizing extract process to produce mesohigh washer shell side lofty tone hydro-thermal and utilize process equipment.
The present invention realizes above-mentioned purpose like this, urea vaporizing extract process is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized equipment, HP steam drum boiler and flush water pump pass into high pressure scrubber through constant voltage groove, high pressure scrubber passes into urea synthesizing rectifying column, rectifying column delivers to the copper liquid heater of synthetic ammonia refining workshop section by pipeline, and passes into oxygen-eliminating device.
Described lofty tone water scrubber shell side passes into water cooler to a high-profile by condensate pump after condensation liquid bath, and wherein condensation liquid bath upper end arranges hot secondary desalination tank.
Described lofty tone water scrubber shell side passes into water cooler circulating cooling to a high-profile through two water pumps to a high-profile of parallel connection, and again passes into high pressure scrubber.
Advantage of the present invention: heat exchange is passed through in the water transfer of air-extraction Technology for Urea Production mesohigh washer shell side height, temperature goes up, give rectifying column heat exchange further, reduce rectifying column steam consumption, high water transfer after rectifying column heat exchange delivers to synthesis refining post to the heat exchange of copper liquid heat exchanger, carries out heat utilization further.Save a large amount of steam, alleviated circulation load, ensure that high pressure scrubber water water quality simultaneously.
Accompanying drawing explanation
Fig. 1 is that urea vaporizing extract process production mesohigh washer shell side lofty tone hydro-thermal utilizes process equipment.
Fig. 2 is high pressure scrubber.
Wherein 1. HP steam drum boiler, 2. flush water pumps, 3. constant voltage groove, 4. high pressure scrubber, 5. rectifying column, 6. copper liquid heater, 7. condensation liquid bath, 8. secondary desalination tank, 9. lofty tone water cooler, 10-1. condensate pump, 10-2. is water pump to a high-profile, 11. oxygen-eliminating devices.
Detailed description of the invention
Embodiment 1
Urea vaporizing extract process is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized technique, the technological process that high pressure scrubber shell side water under high pressure adopts benefit limit, limit to send, make temperature reach 135-140 DEG C by after the first ammonium liquid heat exchange of the high water transfer in the high pressure scrubber shell side of 120 DEG C and high pressure scrubber tube side, discharge is 180m
3/ h, passes into urea synthesizing rectifying column by the water after heat exchange, and wherein urine is through the high water transfer heat exchange of tube side and shell side, and the flow after heat exchange is 180m
3/ h, temperature is 120-125 DEG C, and the high water transfer after rectifying column heat exchange delivers to the copper liquid heater heat exchange of synthetic ammonia refining workshop section by pipeline, and after heat exchange, water temperature is 85-100 DEG C, flow 14 m
3/ h, the oxygen-eliminating device that high water transfer sends into refining workshop section through tube side reclaims hot water, for synthesis ammonia system after oxygen-eliminating device deoxygenation.The temperature adopting water cooler recirculated water to a high-profile to maintain high water transfer after high water transfer heat exchange in high pressure scrubber shell side is 135-140 DEG C, and wherein the flow of water cooler recirculated water is 200m to a high-profile
3/ h.Adopt steam condensate to regulate and control after high water transfer heat exchange in high pressure scrubber shell side and keep discharge to be 180m
3/ h, wherein the temperature of steam condensate is 80-90 DEG C, fills into 14m to condensate liquid simultaneously
3the secondary desalination tank of/h.
Urea vaporizing extract process is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized equipment, HP steam drum boiler 1 and flush water pump 2 pass into high pressure scrubber 4 through constant voltage groove 3, high pressure scrubber 4 passes into urea synthesizing rectifying column 5, rectifying column 5 delivers to the copper liquid heater 6 of synthetic ammonia refining workshop section by pipeline, and passes into oxygen-eliminating device 11.Water scrubber shell side 4 passes into water cooler 9 to a high-profile by condensate pump 10-1 after condensation liquid bath 7 to a high-profile, and wherein condensation liquid bath 7 upper end arranges hot secondary desalted water 8.Water scrubber shell side 4 passes into water cooler 9 circulating cooling to a high-profile through two water pump 10-2 to a high-profile of parallel connection to a high-profile, and again passes into high pressure scrubber 4.
Adopt method and apparatus of the present invention, economic benefit draws as calculated: specific heat of water is 4.266kJ/kg/ degree, and the proportion of 120 DEG C of water is 0.9348 × 1000kg/m
3, the caloric value of mark coal is 29308kJ/kg, is: 4.266kJ/kg/ degree × 0.9348 × 1000kg/m by calculating saving per hour mark coal
3× 180 m
3× (135 DEG C-120 DEG C) ÷ 29308kJ/kg=367.4kg/h.The benefit of 1 year is: 367.4kg/h × 24h × 350 day ÷ 1000=30860 ton coal.
Claims (6)
1. urea vaporizing extract process is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized technique, the technological process that high pressure scrubber shell side water under high pressure adopts benefit limit, limit to send, it is characterized in that: make temperature reach 135-140 DEG C by after the first ammonium liquid heat exchange of the high water transfer in the high pressure scrubber shell side of 120 DEG C and high pressure scrubber tube side, discharge is 180m
3/ h, passes into urea synthesizing rectifying column by the water after heat exchange, and wherein urine is through the high water transfer heat exchange of tube side and shell side, and the flow after heat exchange is 180m
3/ h, temperature is 120-125 DEG C, the high water transfer after rectifying column heat exchange by pipeline with 14m
3the flow of/h delivers to the copper liquid heater heat exchange of synthetic ammonia refining workshop section, and after heat exchange, water temperature is 85-100 DEG C, flow 14 m
3/ h, the oxygen-eliminating device that high water transfer sends into refining workshop section through tube side reclaims hot water, for synthesis ammonia system after oxygen-eliminating device deoxygenation.
2. urea vaporizing extract process according to claim 1 is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized technique, it is characterized in that: the temperature adopting water cooler recirculated water to a high-profile to maintain high water transfer after the high water transfer heat exchange in high pressure scrubber shell side is 135-140 DEG C, and wherein the flow of water cooler recirculated water is 200m to a high-profile
3/ h.
3. urea vaporizing extract process according to claim 1 is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized technique, it is characterized in that: adopt steam condensate to regulate and control after the high water transfer heat exchange in high pressure scrubber shell side and keep discharge to be 180m
3/ h, wherein the temperature of steam condensate is 80-90 DEG C, fills into 14m to condensate liquid simultaneously
3the secondary desalted water of/h.
4. urea vaporizing extract process is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized equipment, it is characterized in that: HP steam drum boiler (1) is connected with high pressure scrubber (4) through constant voltage groove (3) with flush water pump (2), high pressure scrubber (4) is connected with the rectifying column (5) of urea synthesizing, two water pumps (10-2) to a high-profile through parallel connection after the conveying pipeline of rectifying column (5) bottom closes with the conveying pipeline congruence of high pressure scrubber (4) shell side are connected with lofty tone water cooler (9), water cooler (9) is connected with high pressure scrubber (4) through conveying pipeline again to a high-profile, to a high-profile water cooler (9) is provided with the pipeline of circulating condensing.
5. urea vaporizing extract process according to claim 4 is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized equipment, it is characterized in that: rectifying column (5) is also connected with the copper liquid heater (6) of synthetic ammonia refining workshop section by pipeline, and copper liquid heater (6) is connected with oxygen-eliminating device (11).
6. urea vaporizing extract process according to claim 4 is produced mesohigh washer shell side lofty tone hydro-thermal and is utilized equipment, it is characterized in that: high pressure scrubber (4) shell side passes into water cooler (9) to a high-profile by condensate pump (10-1) after condensation liquid bath (7), and wherein condensation liquid bath (7) upper end arranges hot secondary desalination tank (8).
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|---|---|---|---|
| CN201310372088.5A CN103418211B (en) | 2013-08-23 | 2013-08-23 | Process and device for heat utilization of high-pressure temperature-regulation water in shell side of high pressure scrubber in production in urea steam stripping method |
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|---|---|---|---|
| CN201310372088.5A CN103418211B (en) | 2013-08-23 | 2013-08-23 | Process and device for heat utilization of high-pressure temperature-regulation water in shell side of high pressure scrubber in production in urea steam stripping method |
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| CN103697620A (en) * | 2013-12-25 | 2014-04-02 | 山西兰花科技创业股份有限公司 | Waste heat refrigeration method and device of urea high pressure temperature regulation water |
| CN106767026A (en) * | 2016-12-30 | 2017-05-31 | 安徽昊源化工集团有限公司 | Urea vaporizing extract process production mesohigh washer shell side lofty tone hydro-thermal utilizes Processes and apparatus |
| 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 |
| CN113233415B (en) * | 2021-05-24 | 2023-05-12 | 大连理工大学 | Process and device for preparing hydrogen from hydrogen iodide in iodine-sulfur cycle |
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| CN1321977C (en) * | 2005-08-03 | 2007-06-20 | 四川泸天化股份有限公司 | Method for concentrating thin urine using falling film type evaporation heater |
| CN1300101C (en) * | 2005-08-03 | 2007-02-14 | 四川泸天化股份有限公司 | Throughput enlarging method for urea production device |
| CN101397144B (en) * | 2007-10-22 | 2010-05-26 | 贵州赤天化股份有限公司 | Method for absorbing ammonia by cooling down of high pressure shift temperature water from stripping urea plant |
| EP2128129A1 (en) * | 2008-05-20 | 2009-12-02 | Urea Casale S.A. | Method for the modernization of a urea production plant |
| CN101774609A (en) * | 2010-01-06 | 2010-07-14 | 倪云飞 | Regeneration process flow for producing, refining and regenerating synthetic ammonia |
| CN202328163U (en) * | 2011-11-11 | 2012-07-11 | 贵州宜化化工有限责任公司 | Urea high-pressure tempered water waste heat recycling device |
| CN102989264A (en) * | 2012-09-24 | 2013-03-27 | 天津大学 | Afterheat recovery coupling system in high-temperature heat pump technology and cuprammonia refining process |
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