CN103435517B - A kind of Increasing Production and Energy Saving method of carbonic acid gas stripping urea and equipment thereof - Google Patents

A kind of Increasing Production and Energy Saving method of carbonic acid gas stripping urea and equipment thereof Download PDF

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CN103435517B
CN103435517B CN201310327684.1A CN201310327684A CN103435517B CN 103435517 B CN103435517 B CN 103435517B CN 201310327684 A CN201310327684 A CN 201310327684A CN 103435517 B CN103435517 B CN 103435517B
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pressure
tower
urea
stripping
decomposition
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CN201310327684.1A
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CN103435517A (en
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钱伟阳
杨跃平
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北京众联盛化工工程有限公司
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Abstract

The present invention relates to a kind of Increasing Production and Energy Saving technology and equipment thereof of carbonic acid gas stripping urea, comprise pressure in increase and decompose absorption techniques and vacuum heat recovery technology, in increase, pressure decomposes absorption system, changing two-stage evaporation is three sections of evaporations, middle pressure stripping decomposition tower top arranges rectifying section, bottom arranges heating zone, after under synthetic tower, liquid and stripping tower fluid reduce pressure respectively and converge, enter middle pressure and decompose stripping tower, urea first ammonium liquid is in rectifying section and decomposition gas counter current contact, heating zone tube side is entered after rectifying, first ammonium is impelled to be decomposed into carbonic acid gas and ammonia, shell-side is by the steam heating of 185 ~ 195 C, enter mid pressure methyl carbomate condenser condensation again, urea first ammonium liquid at the bottom of tower enters urea rectifying tower and decomposes further, by this programme, overcome the volume increase bottleneck of carbonic acid gas stripping urea, the production capacity of urea be increased dramatically, the corresponding decline of energy consumption index, solve preferably nitrogenous fertilizer enterprises because of synthetic ammonia expand production after the contradiction of urea production capacity deficiency, urea production capacity improves more than 50%.

Description

A kind of Increasing Production and Energy Saving method of carbonic acid gas stripping urea and equipment thereof

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 method and equipment thereof of carbonic acid gas stripping urea.

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.

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 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 there is bias current in stripping tower, first ammonium liquid can not be uniformly distributed film forming at stripping tube, and equipment corrosion aggravates, initiation potential.

In the prior art, carbonic acid gas stripping technique is only 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 energy potentiality are expanded in volume increase.

Summary of the invention

In view of this, main purpose of the present invention is the Increasing Production and Energy Saving method and the equipment thereof that provide a kind of carbonic acid gas stripping urea, pass through the technical program, in increasing in carbonic acid gas stripping urea plant, pressure decomposes absorption techniques and vacuum concentration heat recuperation technology, thus overcome the bottleneck of carbonic acid gas stripping technique yield-increasing technology, provide a kind of facility investment lower, produce effects obvious Technology for Urea Production, 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 realizes like this.

An Increasing Production and Energy Saving method for carbonic acid gas stripping urea is carried out according to the following steps.

A. from synthetic tower temperature 180 ~ 185 C, the urea reaction liquid of pressure 14.0 ~ 14.2MPa is divided into two portions, wherein most of synthetic tower outlet urine delivers to high-pressure stripper, carry out isobaric stripping decomposition, urine after other 1/3 stripping is decompressed to 1.7 ~ 2.0MPa (G), under small portion synthetic tower, liquid is decompressed to 1.7 ~ 2.0MPa (G), after converging stripping urine, presses stripping decomposition tower to carry out stripping Sum decomposition in common feeding.

B. in middle pressure stripping decomposition tower, in urine, first ammonium resolves into carbonic acid gas and ammonia further, the urine after concentrating at the bottom of tower, and enter into urea rectifying tower after being decompressed to 0.3 ~ 0.35MPa, urine concentrates further in low-pressure distillation, its service temperature 132 ~ 138 C.

C. the urine concentration after urea rectifying tower concentrates is 66 ~ 68%, after being decompressed to 0.04 ~ 0.044MPa (A), enter newly-increased vacuum preconcentrator tube side, preheating is carried out from the gas mixture of middle pressure stripping decomposition tower and the reaction heat of first ammonium liquid by shell side, urine after heating enters vacuum pre-concentration separator and carries out gas-liquid separation, make urine concentration rise to 78% by 71%, liquid phase delivers to 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 carbamate condenser level tank, first ammonium liquid after separation is squeezed in the high pressure scrubber of high-pressure system by high pressure carbamate pump, again participates in building-up reactions, and unabsorbed gas enters low-pressure absorption tower and absorbs further.This heat of condensation presses tempered water to take away by mid pressure methyl carbomate condenser tube side, 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 unit, middle pressure stripping decomposition tower is provided with in described middle pressure decomposition absorption unit, the tower body top of described middle pressure stripping decomposition tower is rectifying section, and tower body bottom is heating zone, and the tower body sidewall of rectifying section is provided with urea soln import, arrange steam inlet and condensate outlet at the shell-side of heating zone, the bottom of described heating zone is provided with CO 2gas feed, is respectively arranged with decomposition tower gaseous phase outlet and urea soln outlet bottom tower body top and tower body; Described urea soln import is connected with the fluid of high-pressure stripper with liquid under the synthetic tower in high-pressure system respectively; Described CO 2gas feed and CO 2compressor is connected, and described urea soln outlet is connected with urea rectifying tower in lp system.

Vertical mid pressure methyl carbomate condenser and mid pressure methyl carbomate condenser level tank is provided with in described middle pressure decomposition absorption unit, 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.

Middle pressure washing tower and two horizontal mid pressure methyl carbomate condensers are provided with in described middle pressure decomposition absorption unit, 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 be connected of contacting mutually, and the liquid-phase outlet of described horizontal mid pressure methyl carbomate condenser is connected with high-pressure system mesohigh first ammonium pump.

Middle pressure tempered water water cooler and middle pressure temperature adjustment water pump is provided with in described middle pressure decomposition absorption unit, 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.

Vacuum pre-concentration interchanger is provided with in described middle pressure decomposition absorption unit, vacuum pre-concentration separator and vacuum pre-concentration condenser, the tube side import of described vacuum pre-concentration interchanger is connected with vacuum pre-concentration separator with the rectifying tower in lp system respectively with tube side outlet, 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 of vapo(u)rization system, the shell-side inlet 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 employing technique scheme is: a kind of Increasing Production and Energy Saving method of carbonic acid gas stripping urea and equipment thereof, pass through the technical program, overcome the bottleneck of current carbonic acid gas stripping technique yield-increasing technology, have employed middle pressure and decompose absorption techniques and vacuum concentration heat recuperation technology, and increase relevant device, thus production efficiency is significantly improved, urea production capacity is also increased dramatically, the corresponding decline of every energy consumption index, good solution nitrogenous fertilizer enterprises because of synthetic ammonia expand production after the contradiction of urea production capacity deficiency, urea production capacity can be made to improve more than 50%.

Accompanying drawing explanation

Fig. 1 is the middle pressure adjusting process techniqueflow skeleton diagram in the present invention.

Fig. 2 is the one-piece construction schematic diagram of the embodiment of the present invention one.

Fig. 3 is the one-piece construction schematic diagram of the embodiment of the present invention two.

In figure, in 1, press stripping decomposition tower, 2 tower bodies, 3 rectifying sections, 4 heating zones, 5 urea soln imports, 6CO 2gas feed, 7 decomposition tower gaseous phase outlets, 8 urea soln outlets, 9 synthetic towers, 10 high-pressure stripper, 11CO2 compressor, 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 tower, washing tower is pressed in 17, washing tower feeding pump is pressed in 19, 20 horizontal mid pressure methyl carbomate condensers, tempered water water cooler is pressed in 21, temperature adjustment water pump is pressed 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 of 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 realizes like this.

As shown in Figure 1, the Increasing Production and Energy Saving method of the carbonic acid gas stripping urea that the present invention relates to, carries 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 is divided into two portions, wherein most of urine delivers to high-pressure stripper 10, carry out isobaric stripping decomposition, urine after 1/3 stripping is decompressed to 1.7 ~ 2.0MPa (G), small portion synthetic tower 9 times liquid are directly decompressed to 1.7 ~ 2.0MPa (G), after converging stripping urine, press stripping decomposition tower 1 to carry out stripping decomposition in common feeding.

B., in middle pressure stripping decomposition tower 1, in urine, first ammonium resolves into carbonic acid gas and ammonia further, the urine after concentrating at the bottom of tower, after being decompressed to 0.3 ~ 0.35MPa, enter into urea rectifying tower 12, urine concentrates further 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%, after being decompressed to 0.03 ~ 0.07MPa (A), enter newly-increased vacuum preconcentrator 30 tube side, preheating is carried out from the gas mixture of middle pressure stripping decomposition tower 1 and the reaction heat of first ammonium liquid by shell side, urine after heating enters vacuum pre-concentration separator and carries out gas-liquid separation, make urine concentration rise to about 78% by 71%, liquid phase delivers to urine groove 31, and separation gas enters vacuum pre-concentration condenser 25 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, service temperature is under the condition of 100 ~ 105 C, carry out bubble absorption and heat release, gas-liquid mixture after absorption is separated at carbamate condenser level tank, first ammonium liquid after separation is squeezed in the high pressure scrubber 29 of high-pressure system by high pressure carbamate pump, again participates in building-up reactions, and unabsorbed gas enters low-pressure absorption tower 16 and absorbs further.This heat of condensation presses tempered water to take away by mid pressure methyl carbomate condenser 13 tube side, 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 that the present invention relates to, include high-pressure system and lp system, also include middle pressure and decompose absorption unit, middle pressure stripping decomposition tower 1 is provided with in described middle pressure decomposition absorption unit, tower body 2 top of described middle pressure stripping decomposition tower 1 is rectifying section 3, tower body 2 bottom is heating zone 4, tower body 2 sidewall of rectifying section 3 is provided with urea soln import 5, arrange steam inlet 26 and condensate outlet 27 at the shell-side of heating zone 4, the bottom of described heating zone 4 is provided with CO 2gas feed 6, is respectively arranged with decomposition tower gaseous phase outlet 7 and urea soln outlet 8 bottom tower body 2 top and tower body 2; Described urea soln import 5 is connected with the fluid of high-pressure stripper 10 with the synthetic tower 9 times liquid in high-pressure system 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.

Vertical mid pressure methyl carbomate condenser 13 and mid pressure methyl carbomate condenser level tank 14 is provided with in described middle pressure decomposition absorption unit, 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.

Middle pressure washing tower 17 and two horizontal mid pressure methyl carbomate condensers 20 are provided with in described middle pressure decomposition absorption unit, two horizontal mid pressure methyl carbomate condenser 20 phase serial connections, 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 20 be connected of contacting mutually, 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.

Middle pressure tempered water water cooler 21 and middle pressure temperature adjustment water pump 22 is provided with in described middle pressure decomposition absorption unit, 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.

Vacuum pre-concentration interchanger 23 is provided with in described middle pressure decomposition absorption unit, vacuum pre-concentration separator 24 and vacuum pre-concentration condenser 25, the tube side import of described vacuum pre-concentration interchanger 23 is connected with vacuum pre-concentration separator 24 with the urea rectifying tower 12 in lp system respectively with tube side outlet, 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 of vapo(u)rization system, the shell-side inlet 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 outlet is 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, the middle pressure that have employed 1.7 ~ 2.0MPa (G) decomposes absorption techniques, increases relevant medium-voltage equipment, have employed the Vacuum Heat concentration technique of absolute pressure 0.03 ~ 0.07MPa before vapo(u)rization system, and add vacuum Pre-concentrator apparatus, instead of flash drum of the prior art with this.

Claims (6)

1. an Increasing Production and Energy Saving method for 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 is divided into two portions, wherein most of synthetic tower outlet urine delivers to high-pressure stripper, carry out isobaric stripping decomposition, urine after other 1/3 stripping is decompressed to 1.7 ~ 2.0MPa (G), under small portion synthetic tower, liquid is decompressed to 1.7 ~ 2.0MPa (G), after converging stripping urine, presses stripping decomposition tower to carry out stripping Sum decomposition in common feeding;
B. in middle pressure stripping decomposition tower, in urine, first ammonium resolves into carbonic acid gas and ammonia further, the urine after concentrating at the bottom of tower, and enter into urea rectifying tower after being decompressed to 0.3 ~ 0.35MPa, urine concentrates further in low-pressure distillation, its service temperature 132 ~ 138 C;
C. the urine concentration after urea rectifying tower concentrates is 66 ~ 68%, after being decompressed to 0.03 ~ 0.07MPa (A), enter newly-increased vacuum preconcentrator tube side, shell side is the gas mixture from middle pressure stripping decomposition tower and the first ammonium liquid from lp system, its reaction heat, to the preheating of tube side urine, then enters vacuum pre-concentration separator and carries out gas-liquid separation, make urine concentration rise to 78% by 71%, liquid phase delivers to 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 carbamate condenser level tank, first ammonium liquid after separation is squeezed in the high pressure scrubber of high-pressure system by high pressure carbamate pump, again building-up reactions is participated in, unabsorbed gas enters low-pressure absorption tower and absorbs further, this heat of condensation presses tempered water to take away by mid pressure methyl carbomate condenser tube side, 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 unit, be provided with middle pressure stripping decomposition tower in described middle pressure decomposition absorption unit, the tower body top of described middle pressure stripping decomposition tower is rectifying section, tower body bottom is heating zone, the tower body sidewall of rectifying section is provided with urea soln import, arranges steam inlet and condensate outlet at the shell-side of heating zone, the bottom of described heating zone is provided with CO 2gas feed, is respectively arranged with gaseous phase outlet and urea soln outlet bottom tower body top and tower body; Described urea soln import is connected with the fluid of high-pressure stripper with liquid under the synthetic tower in high-pressure system 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, vertical mid pressure methyl carbomate condenser and mid pressure methyl carbomate condenser level tank is provided with in described middle pressure decomposition absorption unit, 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, middle pressure washing tower and two horizontal mid pressure methyl carbomate condensers are provided with in described middle pressure decomposition absorption unit, 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 be connected of contacting mutually, the liquid-phase outlet of described horizontal mid pressure methyl carbomate condenser is connected with high-pressure system mesohigh first ammonium pump.
5. the Increasing Production and Energy Saving equipment of a kind of carbonic acid gas stripping urea according to claim 3 or 4, it is characterized in that, middle pressure tempered water water cooler and middle pressure temperature adjustment water pump is provided with in described middle pressure decomposition absorption unit, 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 of evaporations, increase vacuum preconcentration technique, be provided with vacuum pre-concentration interchanger, vacuum pre-concentration separator and vacuum pre-concentration condenser, the tube side import of described vacuum pre-concentration interchanger is connected with vacuum pre-concentration separator with the rectifying tower in lp system respectively with tube side outlet, 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 of vapo(u)rization system, the shell-side inlet 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.
CN201310327684.1A 2013-07-31 2013-07-31 A kind of Increasing Production and Energy Saving method of carbonic acid gas stripping urea and equipment thereof CN103435517B (en)

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CN103724232B (en) * 2013-12-24 2015-05-13 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
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
CN104478761A (en) * 2014-08-20 2015-04-01 江苏飞翔泵业制造有限公司 Urea production line
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
CN107586266B (en) * 2016-07-08 2020-10-09 王庆锋 Improved CO2Gas stripping parallel/serial medium pressure urea production process
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