CN103724232B - Energy-saving optimization technology of deep hydrolysis system for improving urea production capacity - Google Patents
Energy-saving optimization technology of deep hydrolysis system for improving urea production capacity Download PDFInfo
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- CN103724232B CN103724232B CN201310743560.1A CN201310743560A CN103724232B CN 103724232 B CN103724232 B CN 103724232B CN 201310743560 A CN201310743560 A CN 201310743560A CN 103724232 B CN103724232 B CN 103724232B
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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
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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
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Abstract
The invention belongs to the technical field of urea production, discloses a urea production technology applied to an aqueous solution total recycle process, a CO2 vaporizing extract process, an NH3 vaporizing extract process and the others, and particularly discloses an energy-saving optimization technology of a deep hydrolysis system for improving urea production capacity, of which the operation pressure is within a range of 1.1-2.5MPa. A gas phase ejected by a stripping-hydrolyzing tower is directly led to a resolving device of a low-pressure system by a stripping-hydrolyzing single tower technology; the top gas-phase heat of the stripping-hydrolyzing tower can be recycled to the maximal extent; excessive moisture is limited in an urea solution of the low-pressure system, so that the water/carbon ratio of urea synthetic tower material is controllable. Thus, the transformation rate of CO2 in urea synthesis is improved, production energy consumption of unit urea is reduced, and the value is lower than the design value. By adopting the energy-saving optimization technology, reflux liquid in the existing stripping-hydrolyzing single tower technology is also removed, energy consumption and investment on equipment are further reduced, and the operation of the system is simplified.
Description
Technical field
The present invention relates to urea production, be specifically related to a kind of depth hydrolysis's energy saving of system Optimization Technology improving urea production capacity, the not only steam/hydrocarbons ratio of active control urea synthesizer, improve CO
2transformation efficiency, thus increase urea production, significantly can also reduce the energy consumption in urea production process, simplify the technical process of depth hydrolysis system, reduce investment, belong to technical field of urea production, can be used for water solution total cycling method, CO
2vaporizing extract process, NH
3vaporizing extract process and other urea production process.
Technical background
With regard to the production technique of urea plant, the process for process condensate only has desorption tower by original, the ammonia (NH namely in a recovery process phlegma
3) and carbonic acid gas (CO
2), wherein contain the urea ((NH of about 1%
2)
2cO) arrange outward with waste water.Along with the raising of environmental requirement and the Appropriate application of water resources, present urea plant has depth hydrolysis's system of process condensate.By wherein about 1% hydrolysis of urea ammonification (NH
3) and carbonic acid gas (CO
2) reclaim, depth hydrolysis's system send outside and purify waste water in ammonia (NH
3), urea ((NH
2)
2cO) all lower than 5ppm, can be used as the feedwater of low pressure boiler or deliver to the pretreatment system of high pressure boiler water supply, so not only having reclaimed the raw material ammonia (NH of urea synthesis
3) and carbonic acid gas (CO
2), also the waste water of former outer row is used as oiler feed simultaneously.
Depth hydrolysis's system used at present mainly contains two classes.First desorb-hydrolysis flow process, major equipment is desorption tower and hydrolysis tower (device) and relevant interchanger and pump.It two is Single-tower stripping-hydrolysis flow processs.Two kinds of flow processs all can make the ammonia in process condensate and urea be not more than 5ppm and reach the recycling of water resources.But desorb-hydrolysis process long flow path, equipment are more, and power consumption is high, complicated operation, and output investment ratio Single-tower stripping-hydrolysis process is large.Single-tower stripping-hydrolysis process only has a stripping hydrolysis tower, hydrolysis interchanger, a hydrolysis pump, and have flow process simple, power consumption is low, maneuverable feature.Two kinds of depth hydrolysis's techniques, go out desorption tower (stripping hydrolysis tower) top gas mutually in water content be about (50wt%), become rare first ammonium liquid and return Urea Conversion System, the NH namely reclaimed after condensation, cooling
3, CO
2the water carrying 50% returns Urea Conversion System, makes the steam/hydrocarbons ratio of urea synthesizer exceed design load, and is not enough to the steam/hydrocarbons ratio that ACTIVE CONTROL enters urea synthesizer.Water is the product of urea synthesis, and it occupies again the useful space of urea synthesizer simultaneously, and therefore steam/hydrocarbons ratio increase must affect CO
2transformation efficiency, reduce urea production; Unnecessary water circulates in whole urea system, can increase power consumption and the steam consumption of urea plant.Two kinds of process steam consumption all about 300kg/t process condensates.In patent CN101696177A, CN1356313A, CN102267754A, stripping hydrolysis tower gas is to two sections of decomposition towers (low pressure decomposition tower), recovery heat grade is low, simultaneously because working pressure is lower, cause desorption tower eject the gas phase band water come more cause finally enter urea synthesizer material water carbon ratio higher than design load; In above-mentioned patent, add ammonium fluid backflow at tower top, heat can not be reclaimed completely, add cooling-water consumption simultaneously.Single-tower stripping-hydrolysis flow process such as patent ZL200520013319.4 is provided with the equipment such as condenser, reflux pump, investment is large, and do not reclaim the heat of stripping gas, consume water coolant simultaneously, be unfavorable for the environmental protection policies such as current saving energy, lowering energy consumption and reducing pollutants discharge, be badly in need of being optimized it enhancing productivity while energy-conservation.
Summary of the invention
The object of the invention is to solve the above-mentioned shortcoming of process condensate strong hydrolysis device in existing urea production and deficiency, reclaim sensible heat and the latent heat of Single-tower stripping-hydrolysis tower exhaust gas phase completely, use it for middle pressure decomposition tower (liquid structure, the NH of urea plant
3stripping process) or rectifying tower (CO
2stripping process), press water-content in decomposition gas simultaneously in reducing, the steam/hydrocarbons ratio of urea synthesizer can be entered by active control, urea synthesizer be run under best steam/hydrocarbons ratio, improves CO in urea synthesis
2transformation efficiency, thus improve the throughput of urea, and significantly reduce the energy consumption in urea production process, reduce the investment of depth hydrolysis's system, simplify the operation flow process.
Instant invention overcomes the shortcomings and deficiencies of existing strong hydrolysis device, invent a kind of depth hydrolysis energy saving of system Optimization Technology that improve urea production capacity of working pressure within the scope of 1.1-2.5Mpa, be exactly stripping-be hydrolyzed single tower process specifically, stripping-hydrolysis tower is ejected the gas phase come directly to introduce in the resolving device of middle low-pressure system, reclaim out the gas phase heat of stripping-hydrolysis tower to greatest extent, the moisture that it is unnecessary is limited in middle low-pressure system, make the steam/hydrocarbons ratio into urea synthesizer controlled, thus improve CO in urea synthesis
2transformation efficiency, improve urea production, reduce the production energy consumption of unit urea, make it lower than design load.The present invention also eliminates existing stripping-the be hydrolyzed phegma in single tower process, further reduces the consumption of energy and the investment of refluxing unit, and the operation of simplified system runs.
For achieving the above object, a kind of depth hydrolysis's energy saving of system Optimization Technology improving urea production capacity, its feature mainly comprises the following steps:
1. the process condensate containing ammonia, carbonic acid gas, urea and water come by process condensate liquid bath is pumped to high-performance heat exchanger through stripping-hydrolysis, carry out heat exchange with from 190-220 DEG C of fluid at the bottom of stripping-hydrolysis tower, after being preheating to 180-200 DEG C, entering stripping-hydrolysis tower.Urea in process condensate is high temperature and complete hydrolysis under enough residence time in stripping-hydrolysis tower, final waste hydrolyzed liquid drains into out-of-bounds through high-performance heat exchanger and liquid waste cooler at the bottom of tower, the content of its urea and ammonia is not more than 5ppm, can directly as low pressure boiler feedwater or deliver to the Water pretreatrnent system of high-duty boiler, realize the high-level utilization of water.Ammonia free in stripping-hydrolysis tower, carbonic acid gas and the ammonia, carbonic acid gas and the water that are obtained by hydrolysis of urea are together discharged from stripping-hydrolysis tower top, and temperature is 170-190 DEG C, directly enters the gas-phase space of the resolving device bottom of medium low pressure system.
The key control parameter of stripping-hydrolysis tower is send the ammonia in purifying waste water, urea content outside, can enter the quantity of steam of stripping-hydrolysis tower and exhaust gas phase internally piloted valve adjusts by regulating.
2. give vent to anger from the stripping-hydrolysis tower top of the gas-phase space charging of resolving device bottom with the cold urine of self-decomposition equipment its top feed by tower tray or filler counter current contact.The give vent to anger water vapor of middle 60%-85% of stripping-hydrolysis tower top is condensed in urine, and the latent heat of releasing and sensible heat make the ammonium carbamate decomposed in urine be free ammonia and carbonic acid gas, and discharge from tower top with a small amount of water vapor, enter recovery system; Enter urea concentration system post-treatment from resolving device liquid phase out and become urea product.
Wherein resolving device can adopt tray column or packing tower according to different urea techniques, is provided with gas and liquid distribution device in tower.
3. stripping-hydrolysis tower ejects gas and directly enters in mesolow resolving device without condensing reflux, the latent heat in stripping-hydrolysis gas and sensible heat are fully reclaimed, drastically reduce the area the water-content in ammonium carbamate solution, thus reduce into the steam/hydrocarbons ratio in urea synthesizer solution, add the turndown ratio of follow-up low pressure recycle system, by regulating the amount of water ACTIVE CONTROL of low pressure recovery system to enter the steam/hydrocarbons ratio of urea synthesizer at optimum range, make CO in urea synthesis
2transformation efficiency improve 1%-3%, reduce in decomposition course, low-pressure steam consumption and power consumption.
Wherein stripping-hydrolysis tower does not establish reflux, not only reduces equipment, simplifies operating process, also reduces the steam consumption that some are unnecessary.
The present invention is compared with existing treatment process, and the advantage had is:
1. reclaim stripping-hydrolysis tower top gaseous phase heat to greatest extent, significantly reduce the energy consumption in urea production process, reduce the investment of depth hydrolysis's system, simplify the operation flow process.
2. can enter the steam/hydrocarbons ratio of urea synthesizer by active control, urea synthesizer be run under best steam/hydrocarbons ratio, improves CO in urea synthesis
2transformation efficiency, thus improve the throughput of urea.
3. overcome the shortcomings and deficiencies of existing strong hydrolysis device, invented a kind of depth hydrolysis energy saving of system Optimization Technology that improve urea production capacity of working pressure within the scope of 1.1-2.5Mpa, be applicable to domestic the liquid structure technique, the CO that generally adopt
2stripping process, NH
3stripping process and other urea production process.
Maximum feature of the present invention is: stripping-hydrolysis tower is ejected the gas phase come and directly introduce in the resolving device of middle low-pressure system, reclaim stripping-hydrolysis tower top gaseous phase heat to greatest extent, the moisture that it is unnecessary is limited in middle low-pressure system, make the steam/hydrocarbons ratio into urea synthesizer controlled, thus improve CO in urea synthesis
2transformation efficiency, reduce the production energy consumption of unit urea, make it lower than design load.
Accompanying drawing explanation
Accompanying drawing 1 is process flow diagram of the present invention;
Wherein 1-process condensate liquid bath, 2-stripping-hydrolysis pump, 3-high-performance heat exchanger, 4-stripping-hydrolysis tower, 5-resolving device, 6-liquid waste cooler, V1-process condensate flow control valve, V2-steam regulating valve, V3-waste liquor stream adjustable valve, V4-gas phase internally piloted valve.
Embodiment
Below in conjunction with accompanying drawing 1, technical process of the present invention and embodiment are described:
1. the process condensate containing ammonia, carbonic acid gas, urea and water come by process condensate liquid bath (1) delivers to high-performance heat exchanger (3) through stripping-hydrolysis pump (2), carry out heat exchange with the 190-220 DEG C of fluid from stripping-hydrolysis tower (4) end, after being preheated to 180-200 DEG C, entering stripping-hydrolysis tower (4).Urea in process condensate is high temperature and complete hydrolysis under enough residence time in stripping-hydrolysis tower (4), final waste hydrolyzed liquid drains into out-of-bounds through high-performance heat exchanger (3) and liquid waste cooler (6) at the bottom of tower, the content of its urea and ammonia is not more than 5ppm, can directly as low pressure boiler feedwater or deliver to the Water pretreatrnent system of high-duty boiler, realize the high-level recycle of water.Ammonia free in stripping-hydrolysis tower (4), carbonic acid gas and the ammonia, carbonic acid gas and the water that are obtained by hydrolysis of urea are together discharged from stripping-hydrolysis tower (4) top, temperature is about 170-190 DEG C, directly enters the gas-phase space of resolving device (5) bottom of middle low-pressure system.The key control parameter of stripping-hydrolysis tower (4) is send the ammonia in purifying waste water, urea content outside, can enter the steam regulating valve (V2) of stripping-hydrolysis tower (4) and exhaust gas phase internally piloted valve (V4) adjusts by adjustment.
2. give vent to anger from stripping-hydrolysis tower (4) top of the gas-phase space charging of resolving device (5) bottom with the cold urine of self-decomposition equipment (5) its top feed by tower tray or filler counter current contact.The give vent to anger water vapor of middle 60%-85% of stripping-hydrolysis tower (4) top is condensed in urine, the latent heat of releasing and sensible heat make the ammonium carbamate decomposed in urine be free ammonia and carbonic acid gas, and discharge from tower top with part water vapor, enter recovery system; From resolving device 5) liquid phase out enters urea concentration system, and deliver to prilling tower after treatment and carry out granulation.Wherein resolving device (5) can adopt tray column or packing tower according to different urea techniques, is provided with gas and liquid distribution device in tower.
3. stripping-hydrolysis tower (4) ejects gas and directly enters in resolving device (5) without condensing reflux, the latent heat in stripping-hydrolysis gas and sensible heat are fully recycled, drastically reduce the area the water-content in ammonium carbamate solution, thus reduce into the steam/hydrocarbons ratio in urea synthesizer solution, add the turndown ratio of follow-up low pressure recycle system, by regulating the amount of water ACTIVE CONTROL of low pressure recovery system to enter the steam/hydrocarbons ratio of urea synthesizer at optimum range, make CO in urea synthesis
2transformation efficiency improve 1%-3%, reduce in decomposition course, low-pressure steam consumption.Wherein stripping-hydrolysis tower (4) does not establish reflux, not only reduces equipment, simplifies operating process, also reduces the steam consumption that some are unnecessary.
Claims (3)
1. improve depth hydrolysis's energy saving of system Optimization Technology of urea production capacity, it is characterized in that:
1), that is come by process condensate liquid bath contains ammonia, carbonic acid gas, the process condensate of urea and water is pumped to high-performance heat exchanger through stripping-hydrolysis, heat exchange is carried out with from DEG C fluid of the 190-220 at the bottom of stripping-hydrolysis tower, stripping-hydrolysis tower is entered after being preheated to 180-200 DEG C, urea in process condensate is high temperature and complete hydrolysis under enough residence time in stripping-hydrolysis tower, final waste hydrolyzed liquid drains into out-of-bounds through high-performance heat exchanger and liquid waste cooler at the bottom of tower, the content of its urea and ammonia is not more than 5ppm, can directly as low pressure boiler feedwater or deliver to the Water pretreatrnent system of high-duty boiler, realize the high-level utilization of water, ammonia free in stripping-hydrolysis tower, carbonic acid gas and the ammonia obtained by hydrolysis of urea, carbonic acid gas and water are together discharged from stripping-hydrolysis tower top, temperature is 170-190 DEG C, directly enter the gas-phase space of the resolving device bottom of middle low-pressure system,
The key control parameter of described stripping-hydrolysis tower is send the ammonia in purifying waste water, urea content outside, can enter the quantity of steam of stripping-hydrolysis tower and exhaust gas phase internally piloted valve adjusts by regulating;
2), give vent to anger from the stripping-hydrolysis tower top of the gas-phase space charging of resolving device bottom with the cold urine of self-decomposition equipment its top feed by tower tray or filler counter current contact, the give vent to anger water vapor of middle 60%-85% of stripping-hydrolysis tower top is condensed in urine, the latent heat of releasing and sensible heat make the ammonium carbamate decomposed in urine be free ammonia and carbonic acid gas, and discharge from tower top with part water vapor, enter recovery system; Enter urea concentration system post-treatment from resolving device liquid phase out and become urea product;
Described resolving device can adopt tray column or packing tower according to different urea techniques, is provided with gas and liquid distribution device in tower;
3), stripping-hydrolysis tower ejects gas and directly enters in resolving device without condensing reflux, the latent heat in stripping-hydrolysis gas and sensible heat are fully recycled, drastically reduce the area the water-content in ammonium carbamate solution, thus reduce into the steam/hydrocarbons ratio in urea synthesizer solution, add the turndown ratio of follow-up low pressure recycle system, by regulating the amount of water ACTIVE CONTROL of low pressure recovery system to enter the steam/hydrocarbons ratio of urea synthesizer at optimum range, make CO in urea synthesis
2transformation efficiency improve 1%-3%, reduce the steam consumption in decomposition course and power consumption;
Described stripping-hydrolysis tower does not establish reflux, not only reduces equipment, simplifies operating process, also reduces the steam consumption that some are unnecessary.
2. energy saving optimizing technique according to claim 1, can be used for water solution total cycling method, CO
2vaporizing extract process, NH
3vaporizing extract process and other urea production process.
3. energy saving optimizing technique according to claim 1, its working pressure scope is 1.1-2.5Mpa.
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| CN112495323B (en) * | 2020-11-27 | 2021-11-09 | 昱创(天津)化工科技有限公司 | For CO2Medium-pressure desorption hydrolysis tower for gas stripping urea production and energy-saving production increasing method |
| CN115253944B (en) * | 2022-07-14 | 2023-11-03 | 华能国际电力股份有限公司大连电厂 | Device for preparing ammonia by catalytic hydrolysis of urea and preparation method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1100412A (en) * | 1993-09-16 | 1995-03-22 | 中国化学工程总公司 | Stripping recirculation technology & apparatus for urea production |
| CN101397144A (en) * | 2007-10-22 | 2009-04-01 | 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 |
| CN101696177A (en) * | 2009-11-02 | 2010-04-21 | 河南心连心化肥有限公司 | Device for processing urea process condensate and method thereof |
| CN103435517A (en) * | 2013-07-31 | 2013-12-11 | 北京众联盛化工工程有限公司 | Yield-increasing and energy-saving technology of carbon dioxide stripping urea and equipment of carbon dioxide stripping urea |
-
2013
- 2013-12-24 CN CN201310743560.1A patent/CN103724232B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1100412A (en) * | 1993-09-16 | 1995-03-22 | 中国化学工程总公司 | Stripping recirculation technology & apparatus for urea production |
| CN101397144A (en) * | 2007-10-22 | 2009-04-01 | 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 |
| CN101696177A (en) * | 2009-11-02 | 2010-04-21 | 河南心连心化肥有限公司 | Device for processing urea process condensate and method thereof |
| CN103435517A (en) * | 2013-07-31 | 2013-12-11 | 北京众联盛化工工程有限公司 | Yield-increasing and energy-saving technology of carbon dioxide stripping urea and equipment of carbon dioxide stripping urea |
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Address after: 300308 1114, Hua Ying building, Central Avenue, Airport Economic Zone, Tianjin Binhai New Area Patentee after: Tianjin Hao Yong chemical engineering company limited Address before: 300308 1114, Hua Ying building, Central Avenue, Airport Economic Zone, Tianjin Binhai New Area Patentee before: Tianjin Haoyong Chemical Technology Co., Ltd. |