CN103435517A - Yield-increasing and energy-saving technology of carbon dioxide stripping urea and equipment of carbon dioxide stripping urea - Google Patents

Yield-increasing and energy-saving technology of carbon dioxide stripping urea and equipment of carbon dioxide stripping urea Download PDF

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CN103435517A
CN103435517A CN2013103276841A CN201310327684A CN103435517A CN 103435517 A CN103435517 A CN 103435517A CN 2013103276841 A CN2013103276841 A CN 2013103276841A CN 201310327684 A CN201310327684 A CN 201310327684A CN 103435517 A CN103435517 A CN 103435517A
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pressure
tower
urea
stripping
decomposition
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CN103435517B (en
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钱伟阳
杨跃平
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BEIJING UNITY ENGINEERING Co Ltd
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BEIJING UNITY ENGINEERING Co Ltd
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Abstract

The invention relates to a yield-increasing and energy-saving technology of carbon dioxide stripping urea and equipment of the carbon dioxide stripping urea. A medium-pressure decomposition and absorption technology, a vacuum heat recovery technology and a medium-pressure decomposition and absorption system are adopted additionally; two-section evaporation is changed to three-section evaporation; a rectifying section is arranged at the upper part of a medium-pressure stripping decomposition tower; a heating section is arranged at the lower part of the medium-pressure stripping decomposition tower; lower liquid of a synthetic tower and discharge liquid of a stripping tower are subjected to pressure reduction convergence, and then enter the medium-pressure stripping decomposition tower; urea methylamine liquid is in countercurrent contact with decomposition gas at the rectifying section, is rectified and then enters a heating section tube pass to urge methylamine to be decomposed into carbon dioxide and ammonia; a housing side is heated by steam of 185-195 DEG C, and then enters a medium-pressure methylamine condenser to be condensed; and the urea methylamine liquid at the bottom of the tower enters a urea rectifying tower to be further decomposed. With the adoption of the scheme, the yield-increase difficulty of the carbon dioxide stripping urea is overcome; the productivity of the urea can be improved greatly; an energy consumption index is reduced correspondingly; the problem of a nitrogenous fertilizer enterprise that the productivity of the urea is insufficient after a yield of synthesis ammonia is increased is solved better; and the productivity of the urea can be improved by above 50%.

Description

A kind of Increasing Production and Energy Saving technology and equipment thereof of carbonic acid gas stripping urea
Technical field
The present invention relates to a kind of urea intermediate-pressure and decompose absorption and vacuum pre-concentration technology, particularly relate to a kind of Increasing Production and Energy Saving technology and equipment thereof of carbonic acid gas stripping urea.
Background technology
Urea be with liquefied ammonia and carbon dioxide under 170~185 ℃ and 13.5~14.5MPa condition by following reaction formula generation.
2NH 3(gas)+CO2 (gas) NH 2cOONH 4(liquid) (1).
NH 2cOONH 4(liquid) CO(NH 2) 2(liquid)+H 2o(liquid) (2).
In first reaction formula, carbonic acid gas and ammonia generate the 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 subject to the restriction of high-pressure system, the particularly constraint of high-pressure stripper, its design loading is 70% ~ 115% of normal value, when surpassing design maximum, steam stripping efficiency can decline to a great extent, stripping tower liquid level meeting big ups and downs, the high-pressure system superpressure, gas phase band liquid; When lower than the design minimum value, bias current can occur in stripping tower, and first ammonium liquid can not be uniformly distributed film forming at stripping tube, equipment corrosion aggravation, initiation potential.
In the prior art, carbonic acid gas stripping technique only is provided with high pressure synthesis system and low pressure recycle system, although overall procedure is relatively short, turndown ratio is little, and it is very limited that the energy potentiality are expanded in volume increase.
Summary of the invention
In view of this, main purpose of the present invention is to provide a kind of Increasing Production and Energy Saving technology and equipment thereof of carbonic acid gas stripping urea, pass through the technical program, press absorption techniques and the vacuum concentration heat recuperation technology of decomposing in increasing in carbonic acid gas stripping urea plant, thereby overcome the bottleneck of carbonic acid gas stripping technique yield-increasing technology, provide a kind of facility investment lower, obvious Technology for Urea Production produces effects, the urea production capacity is increased dramatically, the corresponding decline of every energy consumption.
In order to achieve the above object, technical scheme of the present invention is to realize like this.
A kind of Increasing Production and Energy Saving technology of carbonic acid gas stripping urea is to carry out according to the following steps.
A. from synthetic tower temperature 180 ~ 185 C, the urea reaction liquid of pressure 14.0 ~ 14.2MPa (G) is divided into two portions, wherein most of urine is delivered to high-pressure stripper, isobaric stripping decomposes, approximately the urine after 1/3 stripping is decompressed to 1.7 ~ 2.0MPa (G), under the small portion synthetic tower, liquid directly is decompressed to 1.7 ~ 2.0MPa (G), after converging the stripping urine, jointly sends into middle pressure stripping decomposition tower and carries out stripping and decomposition.
B. in middle pressure stripping decomposition tower, in urine, the first ammonium further resolves into carbonic acid gas and ammonia, and the urine after concentrated at the bottom of tower enters into the urea rectifying tower after being decompressed to 0.3 ~ 0.35MPa, and urine is further concentrated in low-pressure distillation, its service temperature 132 ~ 138 C.
C. the urine concentration after the urea rectifying tower is concentrated is 66 ~ 68%, be decompressed to 0.04 ~ 0.044MPa (A), enter newly-increased vacuum preconcentrator tube side, by shell side from the gas mixture of pressure stripping decomposition tower and the reaction heat of first ammonium liquid carry out preheating, urine after heating enters vacuum pre-concentration separator and carries out gas-liquid separation, make urine concentration rise to 78% left and right by 71%, liquid phase is delivered to the urine groove, and separation gas enters vacuum pre-concentration condenser condenses.
D. the gas mixture after heat exchange enters the shell side of mid pressure methyl carbomate condenser, at working pressure 1.65 ~ 1.9MPa, under the condition of service temperature 100 ~ 105 C, carry out bubble absorption and heat release, gas-liquid mixture after absorption is separated at the carbamate condenser level tank, in the high pressure scrubber that first ammonium liquid after separation is squeezed into high-pressure system by high pressure carbamate pump, again participate in building-up reactions, unabsorbed gas enters the low pressure absorption tower and further absorbs.This heat of condensation pressure tempered water in the mid pressure methyl carbomate condenser tube side is taken away, and its service temperature is 80 ~ 90 C.
A kind of Increasing Production and Energy Saving equipment of carbonic acid gas stripping urea, include high-pressure system and lp system, also include middle pressure and decompose absorption system, be provided with middle pressure stripping decomposition tower in described middle pressure decomposition absorption system, the tower body top of described middle pressure stripping decomposition tower is rectifying section, and the tower body bottom is heating zone, on the tower body sidewall of rectifying section, is provided with the urea soln import, shell-side in heating zone arranges steam inlet and condensate outlet, and the bottom of described heating zone is provided with CO 2gas feed, tower body top and tower body bottom are respectively arranged with decomposition tower gaseous phase outlet and urea soln outlet; Described urea soln import is connected with the fluid of liquid under synthetic tower in high-pressure system and high-pressure stripper respectively; Described CO 2gas feed and CO 2compressor is connected, and described urea soln outlet is connected with urea rectifying tower in lp system.
Be provided with vertical mid pressure methyl carbomate condenser and mid pressure methyl carbomate condenser level tank in described middle pressure decomposition absorption system, the import of described vertical mid pressure methyl carbomate condenser is connected with the gaseous phase outlet on middle pressure stripping decomposition tower, the import of described mid pressure methyl carbomate condenser level tank is connected with the outlet of vertical mid pressure methyl carbomate condenser, and the liquid-phase outlet of mid pressure methyl carbomate condenser level tank is connected with the low pressure carbamate condenser in lp system with high-pressure system mesohigh first ammonium pump respectively with gaseous phase outlet.
Be provided with middle pressure washing tower and two horizontal mid pressure methyl carbomate condensers in described middle pressure decomposition absorption system, two horizontal mid pressure methyl carbomate condensers are connected in series mutually, the liquid-phase outlet of described middle pressure washing tower is connected with the low pressure absorption tower in lp system with horizontal mid pressure methyl carbomate condenser respectively with gaseous phase outlet, the decomposition tower gaseous phase outlet of described middle pressure stripping decomposition tower is connected with two horizontal mid pressure methyl carbomate condensers that are connected mutually, and the liquid-phase outlet of described horizontal mid pressure methyl carbomate condenser is connected with high-pressure system mesohigh first ammonium pump.
Be provided with middle pressure tempered water water cooler and middle pressure temperature adjustment water pump in described middle pressure decomposition absorption system, described middle pressure tempered water water cooler is connected in series mutually with middle pressure temperature adjustment water pump, and the two ends after serial connection are connected with two heat exchange ends of vertical mid pressure methyl carbomate condenser or the heat exchange end of horizontal mid pressure methyl carbomate condenser respectively.
Be provided with vacuum pre-concentration interchanger in described middle pressure decomposition absorption system, vacuum pre-concentration separator and vacuum pre-concentration condenser, with tube side, outlet is connected with vacuum pre-concentration separator with the rectifying tower in lp system respectively in the tube side import of described vacuum pre-concentration interchanger, the gaseous phase outlet of described vacuum pre-concentration separator is connected with vacuum pre-concentration condenser, the liquid-phase outlet of described vacuum pre-concentration separator is connected with one section vapo(u)rization system, the shell-side entrance of described vacuum pre-concentration interchanger is connected with the decomposition tower gaseous phase outlet of middle pressure stripping decomposition tower, described vacuum pre-concentration interchanger shell-side outlet is connected with the gas phase entrance of vertical mid pressure methyl carbomate condenser or the gas phase entrance of mid pressure methyl carbomate condenser.
Beneficial effect after the employing technique scheme is: a kind of Increasing Production and Energy Saving technology and equipment thereof of carbonic acid gas stripping urea, pass through the technical program, overcome the bottleneck of current carbonic acid gas stripping technique yield-increasing technology, adopted middle pressure to decompose absorption techniques and vacuum concentration heat recuperation technology, and increase relevant device, thereby production efficiency is significantly improved, the urea production capacity also is increased dramatically, the corresponding decline of every energy consumption index, solve preferably nitrogenous fertilizer enterprises because of the expand production contradiction of rear urea production capacity deficiency of synthetic ammonia, can make the urea production capacity improve more than 50%.
The accompanying drawing explanation
Fig. 1 is the middle pressure adjusting process techniqueflow skeleton diagram in the present invention.
The one-piece construction schematic diagram that Fig. 2 is the embodiment of the present invention one.
The one-piece construction schematic diagram that Fig. 3 is the embodiment of the present invention two.
In figure, press stripping decomposition tower, 2 tower bodies, 3 rectifying sections, 4 heating zones, 5 urea soln imports, 6 CO in 1 2gas feed, 7 decomposition tower gaseous phase outlets, 8 urea soln outlets, 9 synthetic towers, 10 high-pressure stripper, 11 CO2 compressors, 12 urea rectifying tower, 13 mid pressure methyl carbomate condensers, 14 mid pressure methyl carbomate condenser level tanks, 15 high pressure carbamate pumps, 16 low pressure absorption towers, press washing tower in 17, press the washing tower feeding pump in 19, 20 horizontal mid pressure methyl carbomate condensers, press the tempered water water cooler in 21, press the temperature adjustment water pump in 22, 23 vacuum pre-concentration interchanger, 24 vacuum pre-concentration separators, 25 vacuum pre-concentration condensers.26 steam inlets, 27 condensate outlets, 28 1 sections vapo(u)rization systems, 29 high pressure scrubbers, 30 vacuum preconcentrators, 31 urine grooves.
Embodiment
Below in conjunction with accompanying drawing, specific embodiment in the present invention is described in further detail.
In order to achieve the above object, technical scheme of the present invention is to realize like this.
As shown in Figure 1, the Increasing Production and Energy Saving technology of the carbonic acid gas stripping urea the present invention relates to, carry out according to the following steps.
.A. from synthetic tower 9 temperature 180 ~ 185 C, the urea reaction liquid of pressure 14.0 ~ 14.2MPa (G) is divided into two portions, wherein most of urine is delivered to high-pressure stripper 10, isobaric stripping decomposes, approximately the urine after 1/3 stripping is decompressed to 1.7 ~ 2.0MPa (G), 9 times liquid of small portion synthetic tower directly are decompressed to 1.7 ~ 2.0MPa (G), after converging the stripping urine, jointly send into middle pressure stripping decomposition tower 1 and carry out stripping and decomposition.
B. in middle pressure stripping decomposition tower 1, in urine, the first ammonium further resolves into carbonic acid gas and ammonia, the urine after concentrating at the bottom of tower, after being decompressed to 0.3 ~ 0.35MPa, enter into urea rectifying tower 12, urine is further concentrated in urea rectifying tower 12, its service temperature 132 ~ 138 C.
C. the urine concentration after urea rectifying tower 36 is concentrated is 66 ~ 68%, be decompressed to 0.03 ~ 0.07MPa (A), enter newly-increased vacuum preconcentrator 30 tube sides, by shell side from the gas mixture of pressure stripping decomposition tower 1 and the reaction heat of first ammonium liquid carry out preheating, urine after heating enters vacuum pre-concentration separator and carries out gas-liquid separation, make urine concentration rise to 78% left and right by 71%, liquid phase is delivered to urine groove 31, and separation gas enters vacuum preconcentrator 30 and carries out condensation.
D. the gas mixture after heat exchange enters the shell side of mid pressure methyl carbomate condenser 13, working pressure is 1.65 ~ 1.9MPa, under the condition that service temperature is 100 ~ 105 C, carry out bubble absorption and heat release, gas-liquid mixture after absorption is separated at the carbamate condenser level tank, in the high pressure scrubber 29 that first ammonium liquid after separation is squeezed into high-pressure system by high pressure carbamate pump, again participate in building-up reactions, unabsorbed gas enters low pressure absorption tower 16 and further absorbs.This heat of condensation pressure tempered water in mid pressure methyl carbomate condenser 13 tube sides is taken away, and its service temperature is 80 ~ 90 C.
As shown in Figures 2 and 3, the Increasing Production and Energy Saving equipment of a kind of carbonic acid gas stripping urea the present invention relates to, include high-pressure system and lp system, also include middle pressure and decompose absorption system, be provided with middle pressure stripping decomposition tower 1 in described middle pressure decomposition absorption system, tower body 2 tops of described middle pressure stripping decomposition tower 1 are rectifying sections 3, tower body 2 bottoms are heating zone 4, be provided with urea soln import 5 on tower body 2 sidewalls of rectifying section 3, shell-side in heating zone 4 arranges steam inlet 26 and condensate outlet 27, and the bottom of described heating zone 4 is provided with CO 2gas feed 6, tower body 2 tops and tower body 2 bottoms are respectively arranged with decomposition tower gaseous phase outlet 7 and urea soln outlet 8; Described urea soln import 5 is connected with 9 times liquid of synthetic tower in high-pressure system and the fluid of high-pressure stripper 10 respectively; Described CO 2gas feed 6 and CO 2compressor 11 is connected, and described urea soln outlet 8 is connected with urea rectifying tower 12 in lp system.
Be provided with vertical mid pressure methyl carbomate condenser 13 and mid pressure methyl carbomate condenser level tank 14 in described middle pressure decomposition absorption system, the import of described vertical mid pressure methyl carbomate condenser is connected with the decomposition tower gaseous phase outlet 7 on middle pressure stripping decomposition tower, the import of described mid pressure methyl carbomate condenser level tank is connected with the outlet of vertical mid pressure methyl carbomate condenser, and the liquid-phase outlet of mid pressure methyl carbomate condenser level tank is connected with the low pressure carbamate condenser in lp system with high-pressure system mesohigh first ammonium pump respectively with gaseous phase outlet.
Be provided with middle pressure washing tower 17 and two horizontal mid pressure methyl carbomate condensers 20 in described middle pressure decomposition absorption system, two horizontal mid pressure methyl carbomate condensers 20 are connected in series mutually, the liquid-phase outlet of described middle pressure washing tower 17 is connected with the low pressure absorption tower 16 in lp system with horizontal mid pressure methyl carbomate condenser 20 respectively with gaseous phase outlet, the decomposition tower gaseous phase outlet 7 of described middle pressure stripping decomposition tower 1 is connected with two horizontal mid pressure methyl carbomate condensers that are connected mutually 20, and the liquid-phase outlet of described horizontal mid pressure methyl carbomate condenser 20 is connected with high-pressure system mesohigh first ammonium pump 15.
Be provided with middle pressure tempered water water cooler 21 and middle pressure temperature adjustment water pump 22 in described middle pressure decomposition absorption system, described middle pressure tempered water water cooler 21 is connected in series mutually with middle pressure temperature adjustment water pump 22, and the two ends after serial connection are connected with two heat exchange ends of vertical mid pressure methyl carbomate condenser 13 or the heat exchange end of horizontal mid pressure methyl carbomate condenser 20 respectively.
Be provided with vacuum pre-concentration interchanger 25 in described middle pressure decomposition absorption system, vacuum pre-concentration separator 24 and vacuum pre-concentration condenser 25, with tube side, outlet is connected with vacuum pre-concentration separator 24 with the urea rectifying tower 12 in lp system respectively in the tube side import of described vacuum pre-concentration interchanger 25, the gaseous phase outlet of described vacuum pre-concentration separator 24 is connected with vacuum pre-concentration condenser 25, the liquid-phase outlet of described vacuum pre-concentration separator 24 is connected 28 with one section vapo(u)rization system, the shell-side entrance of described vacuum pre-concentration interchanger 23 is connected with the decomposition tower gaseous phase outlet 7 of middle pressure stripping decomposition tower 1, described vacuum pre-concentration interchanger shell 23 side outlets are connected with the gas phase entrance of vertical mid pressure methyl carbomate condenser 13 or the gas phase entrance of horizontal mid pressure methyl carbomate condenser 20.
In the present invention, adopted the middle pressure of 1.7 ~ 2.0MPa to decompose absorption techniques, increased relevant medium-voltage equipment, adopted the Vacuum Heat concentration technique of 0.03 ~ 0.07MPa before vapo(u)rization system, and increased vacuum pre-concentration equipment, replaced flash drum of the prior art with this.

Claims (6)

1. the Increasing Production and Energy Saving technology of a carbonic acid gas stripping urea, is characterized in that, carries out according to the following steps:
A. from synthetic tower temperature 180 ~ 185 C, the urea reaction liquid of pressure 14.0 ~ 14.2MPa (G) is divided into two portions, wherein most of urine is delivered to high-pressure stripper, isobaric stripping decomposes, approximately the urine after 1/3 stripping is decompressed to 1.7 ~ 2.0MPa (G), under the small portion synthetic tower, liquid directly is decompressed to 1.7 ~ 2.0MPa (G), after converging the stripping urine, jointly sends into middle pressure stripping decomposition tower and carries out stripping and decomposition;
B. in middle pressure stripping decomposition tower, in urine, the first ammonium further resolves into carbonic acid gas and ammonia, and the urine after concentrated at the bottom of tower enters into the urea rectifying tower after being decompressed to 0.3 ~ 0.35MPa, and urine is further concentrated in low-pressure distillation, its service temperature 132 ~ 138 C;
C. the urine concentration after the urea rectifying tower is concentrated is 66 ~ 68%, be decompressed to 0.03 ~ 0.07MPa (A), enter newly-increased vacuum preconcentrator tube side, shell side is from the gas mixture of middle pressure stripping decomposition tower with from the first ammonium liquid of lp system, its reaction heat, to the preheating of tube side urine, then enters vacuum pre-concentration separator and carries out gas-liquid separation, makes urine concentration rise to 78% left and right by 71%, liquid phase is delivered to the urine groove, and separation gas enters vacuum pre-concentration condenser condenses;
D. the gas mixture after heat exchange enters the shell side of mid pressure methyl carbomate condenser, at working pressure 1.65 ~ 1.9MPa, under the condition of service temperature 100 ~ 105 C, carry out bubble absorption and heat release, gas-liquid mixture after absorption is separated at the carbamate condenser level tank, in the high pressure scrubber that first ammonium liquid after separation is squeezed into high-pressure system by high pressure carbamate pump, again participate in building-up reactions, unabsorbed gas enters the low pressure absorption tower and further absorbs, this heat of condensation pressure tempered water in the mid pressure methyl carbomate condenser tube side is taken away, and its service temperature is 80 ~ 90 C.
2. the Increasing Production and Energy Saving equipment of a carbonic acid gas stripping urea, include high-pressure system and lp system, it is characterized in that, also include middle pressure and decompose absorption system, in described middle pressure decomposition absorption unit, be provided with middle pressure stripping decomposition tower, the tower body top of described middle pressure stripping decomposition tower is rectifying section, the tower body bottom is heating zone, be provided with the urea soln import on the tower body sidewall of rectifying section, at the shell-side of heating zone, steam inlet and condensate outlet be set, the bottom of described heating zone is provided with CO 2gas feed, tower body top and tower body bottom are respectively arranged with gaseous phase outlet and urea soln outlet; Described urea soln import is connected with the fluid of liquid under synthetic tower in high-pressure system and high-pressure stripper respectively; Described CO 2gas feed and CO 2compressor is connected, and described urea soln outlet is connected with urea rectifying tower in lp system.
3. the Increasing Production and Energy Saving equipment of a kind of carbonic acid gas stripping urea according to claim 2, it is characterized in that, be provided with vertical mid pressure methyl carbomate condenser and mid pressure methyl carbomate condenser level tank in described middle pressure decomposition absorption system, the import of described vertical mid pressure methyl carbomate condenser is connected with the decomposition tower gaseous phase outlet on middle pressure stripping decomposition tower, the import of described mid pressure methyl carbomate condenser level tank is connected with the outlet of vertical mid pressure methyl carbomate condenser, the liquid-phase outlet of mid pressure methyl carbomate condenser level tank is connected with the low pressure carbamate condenser in lp system with high-pressure system mesohigh first ammonium pump respectively with gaseous phase outlet.
4. the Increasing Production and Energy Saving equipment of a kind of carbonic acid gas stripping urea according to claim 2, it is characterized in that, be provided with middle pressure washing tower and two horizontal mid pressure methyl carbomate condensers in described middle pressure decomposition absorption system, two horizontal mid pressure methyl carbomate condensers are connected in series mutually, the liquid-phase outlet of described middle pressure washing tower is connected with the low pressure absorption tower in lp system with horizontal mid pressure methyl carbomate condenser respectively with gaseous phase outlet, the decomposition tower gaseous phase outlet of described middle pressure stripping decomposition tower is connected with two horizontal mid pressure methyl carbomate condensers that are connected mutually, the liquid-phase outlet of described horizontal mid pressure methyl carbomate condenser is connected with high-pressure system mesohigh first ammonium pump.
5. according to the Increasing Production and Energy Saving equipment of the described a kind of carbonic acid gas stripping urea of claim 2 or 3, it is characterized in that, be provided with middle pressure tempered water water cooler and middle pressure temperature adjustment water pump in described middle pressure decomposition absorption system, described middle pressure tempered water water cooler is connected in series mutually with middle pressure temperature adjustment water pump, and the two ends after serial connection are connected with two heat exchange ends of vertical mid pressure methyl carbomate condenser or the heat exchange end of horizontal mid pressure methyl carbomate condenser respectively.
6. the Increasing Production and Energy Saving equipment of a kind of carbonic acid gas stripping urea according to claim 2, it is characterized in that, changing dual circulation is three sections evaporations, increase the vacuum preconcentration technique, be provided with vacuum pre-concentration interchanger, vacuum pre-concentration separator and vacuum pre-concentration condenser, with tube side, outlet is connected with vacuum pre-concentration separator with the rectifying tower in lp system respectively in the tube side import of described vacuum pre-concentration interchanger, the gaseous phase outlet of described vacuum pre-concentration separator is connected with vacuum pre-concentration condenser, the liquid-phase outlet of described vacuum pre-concentration separator is connected with one section vapo(u)rization system, the shell-side entrance of described vacuum pre-concentration interchanger is connected with the decomposition tower gaseous phase outlet of middle pressure stripping decomposition tower, described vacuum pre-concentration interchanger shell-side outlet is connected with the gas phase entrance of vertical mid pressure methyl carbomate condenser or the gas phase entrance of mid pressure methyl carbomate condenser.
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CN103724232A (en) * 2013-12-24 2014-04-16 天津市昊永化工科技有限公司 Energy-saving optimization technology of deep hydrolysis system for improving urea production capacity
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CN103819365B (en) * 2014-02-17 2015-07-08 王庆锋 CO2 gas-striping parallel /serial connection medium-pressure urea energy-saving and yield-increasing novel technology
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CN104844479A (en) * 2015-03-25 2015-08-19 山东润昌工程设计有限公司 Tail gas recycling system and process used for stable co-production of melamine and urea
CN104844479B (en) * 2015-03-25 2016-11-16 山东润昌工程设计有限公司 A kind of exhaust gas recovery system and technique stablizing coproduction for tripolycyanamide and carbamide
CN107586266A (en) * 2016-07-08 2018-01-16 王庆锋 Modified CO2Urea production process is pressed during air lift is parallel/serial
CN107586266B (en) * 2016-07-08 2020-10-09 王庆锋 Improved CO2Gas stripping parallel/serial medium pressure urea production process
CN107400066A (en) * 2017-08-08 2017-11-28 内蒙古鄂尔多斯联合化工有限公司 A kind of high-quality process for producing urea and production system
CN107400066B (en) * 2017-08-08 2020-04-24 内蒙古鄂尔多斯联合化工有限公司 High-quality urea production method and production system

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