CN203393072U - Low-energy CO2 vaporizing extract process urea system - Google Patents

Low-energy CO2 vaporizing extract process urea system Download PDF

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CN203393072U
CN203393072U CN201320483707.3U CN201320483707U CN203393072U CN 203393072 U CN203393072 U CN 203393072U CN 201320483707 U CN201320483707 U CN 201320483707U CN 203393072 U CN203393072 U CN 203393072U
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pressure
urea
low
stripping
recovery system
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夏炎华
孙喜
杨志国
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China Wuhuan Engineering Co Ltd
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China Wuhuan Engineering Co Ltd
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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
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Abstract

The utility model discloses a low-energy CO2 vaporizing extract process urea system which solves the problems that the energy-saving effect of the existing urea technology needs improving, and the production cost and equipment investment are high. The low-energy CO2 vaporizing extract process urea system comprises a high pressure decomposition recovery system, wherein the high temperature decomposition recovery system comprises a high pressure CO2 stripping tower, a low pressure decomposition tower and a flash drum which are connected in sequence, the low-energy CO2 vaporizing extract process urea system also comprises a medium pressure decomposition recovery system connected with the high pressure decomposition recovery system in parallel, the medium pressure decomposition recovery system comprises a medium pressure CO2 stripping tower, and a urea steam stripping liquor outlet of the medium pressure CO2 stripping tower is connected with a urea steam stripping liquor inlet of the low pressure decomposition tower. The system is simple, can effectively utilize low pressure steam, expands the capacity, has obvious energy-saving and cost-reducing effects, and is low in equipment investment and running cost.

Description

Less energy-consumption CO 2vaporizing extract process urea system
Technical field
The utility model relates to a kind of carbamide production system, specifically a kind of less energy-consumption CO 2vaporizing extract process urea system.
Background technology
Industrialization urea production is with CO 2gas and liquefied ammonia are raw material, through high being pressed into middle pressure or/and the operations such as low pressure recovery and vacuum concentration, granulation are processed into solid urea product.
At present, urea plant production technique mainly contains several as follows both at home and abroad: Dutch Stamicarbon (Stamicarbon) CO 2the ACES21 technique of vaporizing extract process technique, Italian Si Namu (Snamprogetti) ammonia vaporizing extract process technique, Japanese TOYO, the efficient synthesis technique in Switzerland card Surrey (Casale), water solution total cycling method technique etc.Wherein, the most competitive with carbonic acid gas stripping technique and ammonia stripping process.
Typical CO 2vaporizing extract process technical process is, raw material ammonia and CO 2after supercharging, send into urea synthesizer (pressure 14 ~ 14.5MPaA) urea synthesis, go out urea synthesizer and containing the urea soln (being urea synthesis solution) of first ammonium, through high-pressure decomposing, reclaim the operations such as (pressure 14 ~ 14.5MPaA), low pressure recovery (pressure 0.3 ~ 0.4MPaA) and vacuum concentration, granulation and be processed into solid urea product.Conventionally, high-pressure decomposing adopts the middle pressure steam heating that pressure is 2.3MPaA, and low pressure is decomposed and vacuum concentration utilizes the 0.45MPaA low-pressure steam of high pressure relief system by-product to heat.
Common CO 2in vaporizing extract process process unit, middle pressure steam (2.3MPaA) is mainly used in high pressure CO 2the urea hydrolyser heating of the heating of stripping tower and process condensate liquid treating system, the steam consumption of urea per ton is about 900 ~ 950kg, the 0.45MPaA low-pressure steam of hp ammonium carbamate condenser by-product is removed for outside low pressure decomposition tower, and urea per ton approximately has 200kg low-pressure steam to need outer seeing off.But because the 0.45MPaA low-pressure steam grade of by-product is lower, be generally difficult to utilize, even be injected into CO 2compressor steam turbine (steam turbine driving), its efficiency is also very low, some factory haves no alternative but, by its emptying, waste.
Summary of the invention
The purpose of this utility model is in order to solve the problems of the technologies described above, and a kind of less energy-consumption CO is provided 2vaporizing extract process urea system, has that facility investment is low, production capacity is high, can reduce high pressure CO 2the specification of stripping tower, hp ammonium carbamate condenser or size, the less energy-consumption CO of reduction difficulty of construction 2vaporizing extract process urea system, its production technique is simple, under middle press strip part, can utilize 0.45MPaA low-pressure steam to carry out the first ammonium in urea synthesis solution to carry out stripping heating, shunting high pressure CO 2the load of stripping tower, effectively reduces CO 2vaporizing extract process process unit middle pressure steam consumes, and low-pressure steam is all rationally utilized, and accomplishes the less energy-consumption CO of Self sufficient balance 2vaporizing extract process urea technique.
Technique comprises less energy-consumption CO 2vaporizing extract process urea technique, sends in high-pressure decomposing recovery system urea synthesis solution at high pressure CO 2in stripping tower, carry out high pressure CO 2stripping, in low pressure decomposition tower, carry out low pressure decomposition, finally in flash drum, flash distillation obtains process gas and urea soln, urea synthesis solution is divided into two portions, a part is sent into high-pressure decomposing recovery system, another part is sent into the middle pressure recovery system in parallel with high-pressure decomposing recovery system, the middle pressure CO of described another part urea synthesis solution in middle pressure recovery system 2in stripping tower, carry out middle pressure CO 2stripping, obtains mixed gas and urea stripping liquid, described urea stripping liquid and high pressure CO 2urea stripping liquid after stripping is sent into low pressure decomposition tower after merging and is carried out low pressure decomposition, and the low-pressure steam of described high-pressure decomposing recovery system by-product is pressed CO in introducing 2heating zone in stripping tower is stripping process heating.
Described middle pressure CO 2the working pressure of stripping tower is 1.7 ~ 2.5MpaA, and the ammonia carbon mol ratio of absorption liquid is: 2.3 ~ 2.5, and stripping temperature is 130 ~ 140 ° of C, middle pressure CO 2in the urea stripping liquid obtaining after stripping, temperature is 135 ° of C, and urea concentration is 55 ~ 60%(weight).In described introducing, press CO 2the urea synthesis solution of stripping tower accounts for 10 ~ 40%(weight of total urea synthesis solution).
The urea soln that flash distillation obtains in described flash drum is sent into vacuum preconcentrator, and further heating is concentrated, obtains 100 ~ 115 ° of C of temperature, and concentration is 75 ~ 85%(weight) urea soln sends into subsequent processing; Described middle pressure CO 2stripping tower top mixed gas is out sent into the bottom energy recovery section of vacuum preconcentrator, obtains gas-liquid mixture with first ammonium liquid blended absorbent condensation from low pressure recovery system, and heat of condensation is for heating the concentrated urea soln from flash drum.
Described gas-liquid mixture further absorbs through mid pressure methyl carbomate condenser condensation, then enters mid pressure methyl carbomate condenser level tank and carries out gas-liquid separation, and isolated first ammonium liquid is sent into subsequent processing after the pressurization of high pressure first ammonia pump; Isolated tail gas through in discharge after pressing washer washing.
The closed loop cooling system that the reaction heat of described mid pressure methyl carbomate condenser is comprised of mid pressure methyl carbomate condenser water recirculator and mid pressure methyl carbomate condenser water circulating pump is removed.
The utility model less energy-consumption CO 2vaporizing extract process urea system, comprises high-pressure decomposing recovery system, and described high-pressure decomposing recovery system comprises the high pressure CO connecting successively 2stripping tower, low pressure decomposition tower and flash drum, also include the middle pressure recovery system in parallel with high-pressure decomposing recovery system, and described middle pressure decomposing system comprises middle pressure CO 2stripping tower, described middle pressure CO 2the urea stripping liquid outlet of stripping tower is connected with the urea stripping liquid import of low pressure decomposition tower.
The urea outlet of described flash drum is connected with the urea import of vacuum preconcentrator; Described middle pressure CO 2the mixed gas outlet of stripping tower is connected with the combi inlet port of vacuum preconcentrator, the combi inlet port of described vacuum preconcentrator also with first ammonium liquid pipeline communication from low pressure recovery system.
The gas-liquid mixture outlet of described vacuum preconcentrator connects mid pressure methyl carbomate condenser and mid pressure methyl carbomate condenser level tank successively, and the tail gas outlet of described mid pressure methyl carbomate condenser level tank is connected with middle pressure washer, and the outlet of first ammonium liquid is connected with high pressure carbamate pump.
Described middle pressure CO 2the heating zone of stripping tower adopts falling film type well heater.
In the utility model, by increasing in one, press recovery system, by CO 2gas is introduced the middle pressure CO in this system 2stripping tower bottom, as steam stripping agent, can reduce the temperature that first ammonium decomposes, thereby can use hp ammonium carbamate condenser by-product low-pressure steam as CO 2the heat source of stripping tower, makes to decompose at this from the first ammonium in the urea synthesis solution of urea synthesizer; In addition, owing to introducing the CO of MP steam stripper 2the pressure of gas can significantly reduce (the middle pressure CO of introducing 2the pressure of gas only needs 1.7 ~ 2.2MPaA left and right), do not need to be compressed to the pressure that 14 ~ 14.5MPaA is so high, also greatly reduce CO 2the energy consumption of compressor
Described low-pressure steam refers to that pressure range is the low-pressure steam of 0.45 ~ 0.9MPaA.
On the other hand, in the warp of the first ammonium in urea synthesis solution, press CO 2stripping tower decompose Hou，You Qi top out contain NH 3, CO 2and H 2the mixed gas of O and the bottom energy recovery section (top still can adopt low-pressure steam heating) that enters in the lump vacuum preconcentrator from the first ammonium liquid of (as from low pressure carbamate condenser) in follow-up low pressure recovery system, in vacuum preconcentrator, mixed gas and first ammonium liquid reaction condensation absorb, heat of condensation is for heating the urea soln from flash drum, this partial heat energy is recycled, further reduces steam consumption.
The gas-liquid mixture obtaining after condensation absorbs, through further condensation, gas-liquid separation, washing, obtains middle pressure tail gas and high pressure methylamine liquid.
Beneficial effect:
1. there is significant effect of increasing production: by setting up in one, press recovery system, in the production capacity of original high-pressure decomposing recovery system, can improve production capacity 20 ~ 40%, scrap build is simple, invests low.
2. there is significant energy-saving effect: under the prerequisite of volume increase, adopt stripping process on the one hand, the decomposition temperature of first ammonium is declined, thereby can utilize the low-pressure steam of by-product in high-pressure decomposing recovery system as steam stripped thermal source; On the other hand, utilize obtain after stripping containing CO 2, ammonia, H 2the gaseous mixture of O mixes the principle that can produce condensation absorption reaction with first ammonium liquid, first ammonium liquid in low pressure recovery system from follow-up is returned and caused in vacuum preconcentrator and gas mixing and contacting reaction, the reaction heat that condensation obtains is simultaneously for heating urea solution, further concentrating urea solution.
3. the heat energy supply of adding in devices all in the middle pressure recovery system increasing after system except original high-pressure decomposing all adopts Self sufficient balance, or utilize hp ammonium carbamate condenser byproduct steam, do not consume in addition medium-pressure or high pressure steam, or utilize condensation reaction hot, all heat energy all obtains efficient recovery, when improving output, also greatly reduce production cost, environmentally friendly.Take that to produce 520000 tons/year of urea plants per year be example, can save every year middle pressure steam and consume 10.4 ~ 130,000 tons, with the calculation of price of 150 yuan of middle pressure steams per ton, annual expense of saving is 1560 ~ 1,950 ten thousand yuan.If adopt the utility model Technology to transform, only take and save energy and reduce the cost as object, increase foregoing middle pressure recovery system, its newly-increased investment, less than 1,000 ten thousand yuan, in the time of volume increase, was recyclable fully invested less than 1 year.
4. for the capacity expansion revamping project of determining, can solve the problem of original high-pressure decomposing recovery system scarce capacity; For new device, can reduce specification or the size of high-pressure decomposing recovery system relevant device, can reduce investment.
Accompanying drawing explanation
Fig. 1 is the utility model schema and system diagram, and the part that wherein dotted line frame goes out is existing system part.
In 1-, press CO 2in stripping tower, 2-vacuum preconcentrator, 3-mid pressure methyl carbomate condenser, 4-mid pressure methyl carbomate condenser level tank, 5-, press washer, 6-mid pressure methyl carbomate condenser water recirculator, 7-mid pressure methyl carbomate condenser water circulating pump, 8-high pressure carbamate pump, 101-high pressure CO 2stripping tower, 102-low pressure decomposition tower, 103-flash drum, 104-hp ammonium carbamate condenser, 105-low-pressure steam bag.
Embodiment
Below in conjunction with accompanying drawing, the utility model is further explained to explanation:
With reference to Fig. 1, less energy-consumption CO 2vaporizing extract process urea system comprises high-pressure decomposing recovery system, and described high-pressure decomposing recovery system comprises the high pressure CO connecting successively 2stripping tower 101, low pressure decomposition tower 102 and flash drum 103, wherein high pressure CO 2the stripping gas outlet of stripping tower 101 is connected with hp ammonium carbamate condenser 104, on described hp ammonium carbamate condenser 104, low-pressure steam bag 105 is housed.Middle pressure recovery system is in parallel with high-pressure decomposing recovery system, and described middle pressure decomposing system comprises middle pressure CO 2stripping tower 1, described middle pressure CO 2the urea stripping liquid outlet of stripping tower 1 is connected with the urea stripping liquid import of low pressure decomposition tower 102.That is to say high pressure CO 2the urea stripping liquid of stripping tower 101 and middle pressure CO 2the urea stripping liquid merging of stripping tower 1 enters low pressure decomposition tower 102 and carries out low pressure decomposition.The urea outlet of described flash drum 103 is connected with the urea import of vacuum preconcentrator 2; Described middle pressure CO 2the mixed gas outlet of stripping tower 1 is connected with the combi inlet port of vacuum preconcentrator 2, the combi inlet port of described vacuum preconcentrator 2 also with first ammonium liquid pipeline communication from low pressure recovery system, can be used for introducing mixed gas and low pressure first ammonium liquid simultaneously.The gas-liquid mixture outlet of described vacuum preconcentrator 2 connects mid pressure methyl carbomate condenser 3 and mid pressure methyl carbomate condenser level tank 4 successively, the tail gas outlet of described mid pressure methyl carbomate condenser level tank 4 is connected with middle pressure washer 5, and the outlet of first ammonium liquid is connected with high pressure carbamate pump 8.Described middle pressure CO 2cO is pressed in can introducing in stripping tower bottom 2as steam stripping agent, its heating zone adopts falling film type well heater, and can pass into low-pressure steam provides first ammonium liquid to decompose required heat energy.
Technological process:
By at the bottom of urea synthesizer out containing the urea synthesis solution (first ammonium content is about 34%(weight) of first ammonium, urea concentration is about 33.6%(weight), temperature is 183 ° of C) entering high pressure CO 2before stripping tower 101, distribute one (10 ~ 40%(weight), adjustable according to load) send into middle pressure CO after decompression 2stripping tower 1 top gas-liquid separation, isolated mixed gas is (containing CO 2, ammonia, H 2the mixed gas of O) by press CO 2discharge at stripping tower 1 top, and liquid is descending in heating zone (being falling film type well heater) and CO 2gas is (by CO 2compressor come after desulfurization, dehydrogenation, the CO of pressure 2.2MPAa 2gas) counter current contact, carries out stripping, and first ammonium is further decomposed, and the heat energy of described heating zone is provided by the 0.45 ~ 0.9MPaA low-pressure steam from high-pressure decomposing system, by press CO 2the urea stripping liquid (130 ~ 140 ° of C, urea concentration is weight percentage 55 ~ 60%) that flow out stripping tower 1 bottom, through pipeline send into low pressure decomposition tower 102 in high-pressure decomposing recovery system with from high pressure CO 2the urea stripping liquid of stripping tower 101 carries out low pressure decomposition after merging, and low pressure is decomposed required heat energy also to be provided by the low-pressure steam (from low-pressure steam bag 105) of high-pressure decomposing recovery system by-product.Described middle pressure CO 2the working pressure of stripping tower 1 is 1.7 ~ 2.5MPaA, and the ammonia carbon mol ratio of absorption liquid is: 2.2 ~ 2.5.
Meanwhile, the remaining urea synthesis solution containing first ammonium enters high pressure CO 2stripping tower 101 carries out stripping, high pressure CO 2the urea stripping liquid that flow out stripping tower 101 bottoms enters low pressure decomposition tower 102 and carries out low pressure decomposition, the stripping gas that discharge at top is sent into hp ammonium carbamate condenser 104 condensations and is reclaimed first ammonium liquid, and discharge process gas, in removal process, by low-pressure steam bag 105, introduce oiler feed and reclaim heat energy, obtain low-pressure steam.
Urea soln after low pressure decomposition tower 102 low pressure are decomposed enters flash drum 103 and carries out flash distillation, first ammonium in further decomposing urea solution, the process gas flashing off is discharged by top, and isolated urea soln is sent into vacuum preconcentrator 2 by flash drum 103 bottoms outflows and carried out further heating concentrated, described middle pressure CO 2after mixing with low pressure first ammonium liquid (from the low pressure first ammonium liquid in follow-up low pressure recovery system), the mixed gas that discharge at stripping tower 1 top sends into vacuum preconcentrator 2, in the energy recovery section of vacuum preconcentrator 2, and the CO in mixed gas 2generate reacting of first ammonium with ammonia and water in low pressure first ammonium solution, heat of condensation provides heat energy for the urea soln from flash drum 103, make urea soln further concentrated, as required, also can above energy recovery section, add evaporation heating zone, further heating is concentrated to the urea soln after the heating of energy recovery section to utilize the low-pressure steam (from low-pressure steam bag 105) obtaining while reclaiming heat energy in high-pressure decomposing recovery system, urea soln (approximately 110 ° of C of temperature after concentrated, urea concentration is 80%wt) discharge and to enter subsequent processing, the process gas producing enters subsequent processing,
Leave the gas-liquid mixture of vacuum preconcentrator 2 bottom heat energy utilization sections and send into the further condensation absorption of mid pressure methyl carbomate condenser 3 through pipeline, then send into mid pressure methyl carbomate condenser level tank 4 and carry out gas-liquid separation, isolated gas through in discharge after pressing washing tower 5 washing, isolated first ammonium liquid is sent into subsequent processing after high pressure carbamate pump pressurization.The closed loop cooling system that the reaction heat of described mid pressure methyl carbomate condenser 3 is comprised of the mid pressure methyl carbomate condenser water recirculator of connecting with mid pressure methyl carbomate condenser 3 and mid pressure methyl carbomate condenser water circulating pump is removed.
Take that to produce 520000 tons/year of urea plants per year be example, adopt the utility model technique and system can save every year middle pressure steam and consume 10.4 ~ 130,000 tons, can improve production capacity 20 ~ 40% simultaneously, calculation of price with 150 yuan of middle pressure steams per ton, annual expense of saving is 1560 ~ 1,950 ten thousand yuan (not considering to improve the benefit that production capacity produces), newly-increased investment, less than 1,000 ten thousand yuan, was recyclable fully invested less than 1 year.

Claims (4)

1. a less energy-consumption CO 2vaporizing extract process urea system, comprises high-pressure decomposing recovery system, and described high-pressure decomposing recovery system comprises the high pressure CO connecting successively 2stripping tower, low pressure decomposition tower and flash drum, is characterized in that, also includes the middle pressure recovery system in parallel with high-pressure decomposing recovery system, and described middle pressure decomposing system comprises middle pressure CO 2stripping tower, described middle pressure CO 2the urea stripping liquid outlet of stripping tower is connected with the urea stripping liquid import of low pressure decomposition tower.
2. less energy-consumption CO as claimed in claim 1 2vaporizing extract process urea system, is characterized in that, the urea outlet of described flash drum is connected with the urea import of vacuum preconcentrator; Described middle pressure CO 2the mixed gas outlet of stripping tower is connected with the combi inlet port of vacuum preconcentrator, the combi inlet port of described vacuum preconcentrator also with first ammonium liquid pipeline communication from low pressure recovery system.
3. less energy-consumption CO as claimed in claim 1 or 2 2vaporizing extract process urea system, it is characterized in that, the gas-liquid mixture outlet of described vacuum preconcentrator connects mid pressure methyl carbomate condenser and mid pressure methyl carbomate condenser level tank successively, the tail gas outlet of described mid pressure methyl carbomate condenser level tank is connected with middle pressure washer, and the outlet of first ammonium liquid is connected with high pressure carbamate pump.
4. less energy-consumption CO as claimed in claim 1 or 2 2vaporizing extract process urea system, is characterized in that, described middle pressure CO 2the heating zone of stripping tower adopts falling film type well heater.
CN201320483707.3U 2013-08-08 2013-08-08 Low-energy CO2 vaporizing extract process urea system Expired - Lifetime CN203393072U (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107586266A (en) * 2016-07-08 2018-01-16 王庆锋 Modified CO2Urea production process is pressed during air lift is parallel/serial
CN114409573A (en) * 2022-01-05 2022-04-29 中国五环工程有限公司 Improved low energy CO2Urea process by steam stripping method

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
CN114409573A (en) * 2022-01-05 2022-04-29 中国五环工程有限公司 Improved low energy CO2Urea process by steam stripping method

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