CN201545718U - Urea process condensed fluid treatment device - Google Patents
Urea process condensed fluid treatment device Download PDFInfo
- Publication number
- CN201545718U CN201545718U CN2009202577588U CN200920257758U CN201545718U CN 201545718 U CN201545718 U CN 201545718U CN 2009202577588 U CN2009202577588 U CN 2009202577588U CN 200920257758 U CN200920257758 U CN 200920257758U CN 201545718 U CN201545718 U CN 201545718U
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- tower
- links
- desorption tower
- epimere
- hydrolysis
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Abstract
The utility model belongs to a waste fluid treatment device of chemical product production, and relates to a urea process condensed fluid treatment device with high separating efficiency and fine purifying effect. The urea process condensed fluid treatment device comprises a urea process condensed fluid tank with a pump; the urea process condensed fluid tank is connected with a heat exchanger through the pump; the heat exchanger is connected with the upper section of a desorption tower through a pipeline; the upper section of the desorption tower is connected with the heat exchanger through the pump connected with the desorption tower; the heat exchanger is connected with a hydrolysis tower; the hydrolysis tower includes an upper section and a lower section which are communicated through two inverted U-shaped pipes; the heat exchanger connected with the hydrolysis tower is connected with the upper section of the hydrolysis tower; the top portion of the hydrolysis tower is connected with the desorption tower; the top portion of the desorption tower is connected with a condensing absorption system through a reflux condenser; the reflux condenser is connected with the desorption tower through the pump connected with the reflux condenser; the hydrolysis tower is connected with the desorption tower through the heat exchanger connected with the hydrolysis tower; and the bottom portion of the desorption tower is connected with a self-circulation water system through the heat exchanger. The waste fluid treatment device has the advantages of high treatment capacity and capability of thoroughly eliminating environment pollution of waste fluid drained by a urea device.
Description
Technical field
The utility model belongs to liquid waste treating apparatus in the Chemicals production, is specifically related to a kind of separation efficiency height, the device for processing urea process condensate of good purification.
Background technology
The production of China's urea has at present reached 3,800 ten thousand tons/year, occupies first place in the world.Yet the contaminated wastewater that urea discharges in process of production is serious, to this, the industry had been developed different waste water treatment process in recent years, but do not find a kind of equipment and technology of comparative maturity so far yet, can and cut down the consumption of energy again when can either make the condensed liquid in urea preparing process discharging reach standard.Under the situation of current country, address the above problem extremely urgent to the environmental requirement increasingly stringent.
Summary of the invention
The purpose of this utility model is to overcome the deficiencies in the prior art and provides a kind of device structure uniqueness, operation control easily, and processing power is high and can thoroughly eliminate the device for processing urea process condensate of urea plant eliminating waste liquid to the pollution of environment.
The object of the present invention is achieved like this: comprise the condensed liquid in urea preparing process groove that pump is installed, the condensed liquid in urea preparing process groove links to each other with interchanger through pump; Desorption tower is divided into epimere and hypomere, between epimere and the hypomere gas hood is installed, described gas hood intersegmental part on desorption tower, and hypomere is provided with the low-pressure steam inlet mouth; Described interchanger links to each other by the top of pipeline with the epimere of desorption tower, and the bottom of the epimere of desorption tower links to each other by pump that links to each other with desorption tower and the interchanger that links to each other with hydrolysis tower; Hydrolysis tower is divided into epimere and hypomere, is communicated with by two inverted-loop tubes between epimere and the hypomere, and hypomere is provided with the middle pressure steam inlet mouth; The interchanger that links to each other with hydrolysis tower links to each other with hydrolysis tower epimere top, the top of described hydrolysis tower epimere links to each other with the desorption tower epimere, desorption tower epimere top links to each other with the condensation absorption system by reflux exchanger, and the bottom of reflux exchanger links to each other with the epimere top of desorption tower by the pump that links to each other with reflux exchanger; The bottom of described hydrolysis tower hypomere links to each other with the top of desorption tower hypomere by the interchanger that links to each other with hydrolysis tower, and the bottom of desorption tower hypomere links to each other with the self-circulating water system by interchanger.Described gas hood is higher than the link to each other position of pipe joint of pump that the bottom of the epimere of desorption tower links to each other with desorption tower.The position that the top of described hydrolysis tower epimere links to each other with the desorption tower epimere is higher than the position that pump that the bottom of the epimere of desorption tower links to each other with desorption tower links to each other.Described middle pressure steam inlet mouth is at least one.
The utlity model has device structure uniqueness, operation control easily, processing power is high and can thoroughly eliminate the advantage that urea plant is got rid of the waste liquid environmental pollution.
Description of drawings
Fig. 1 is a structural representation of the present utility model.
Embodiment
As shown in Figure 1, the utility model comprises the condensed liquid in urea preparing process groove 1 that pump 2 is installed, and condensed liquid in urea preparing process groove 1 links to each other with interchanger 3 through pump 2; Desorption tower 4 is divided into epimere and hypomere, and gas hood 12 is installed between epimere and the hypomere, described gas hood 12 intersegmental part on desorption tower 4, and hypomere is provided with low-pressure steam inlet mouth 10; Described interchanger 3 links to each other by the top of pipeline with the epimere of desorption tower 4, and the bottom of the epimere of desorption tower 4 links to each other with the interchanger 6 that links to each other with hydrolysis tower 7 by the pump 5 that links to each other with desorption tower 4; Hydrolysis tower 7 is divided into epimere and hypomere, is communicated with by two inverted-loop tubes between epimere and the hypomere, and hypomere is provided with middle pressure steam inlet mouth 11; The interchanger 6 that links to each other with hydrolysis tower 7 links to each other with hydrolysis tower 7 epimere tops, the top of described hydrolysis tower 7 epimeres links to each other with desorption tower 4 epimeres, desorption tower 4 epimere tops link to each other with condensation absorption system 14 by reflux exchanger 8, and the bottom of reflux exchanger 8 links to each other with the epimere top of desorption tower 4 by the pump 9 that links to each other with reflux exchanger 8; The bottom of described hydrolysis tower 7 hypomeres links to each other with the top of desorption tower 4 hypomeres by the interchanger 6 that links to each other with hydrolysis tower 7, and the bottom of desorption tower 4 hypomeres links to each other with self-circulating water system 13 by interchanger 3.Described gas hood 12 is higher than the link to each other position of pipe joints of pump 5 that the bottom of the epimere of desorption tower 4 links to each other with desorption tower 4.The position that the top of described hydrolysis tower 7 epimeres links to each other with desorption tower 4 epimeres is higher than the position that pump 5 that the bottom of the epimere of desorption tower 4 links to each other with desorption tower 4 links to each other.Described middle pressure steam inlet mouth 11 is at least one.
Principle of work of the present utility model is: from about 38 ℃ of the condensed liquid in urea preparing process temperature of condensed liquid in urea preparing process groove 1, wherein contain NH
3～6%, CO
2～2%, urea～1.5%, entering interchanger 3 after pump 2 is forced into 0.4Mpa heats up with the following liquid heat exchange that desorption tower 4 comes out, after being elevated to 110 ℃, temperature enters desorption tower 4 epimeres, desorption tower 4 has the gas hood 12 of certain altitude to be communicated with in the middle of being divided into two sections, 135 ℃ of temperature, pressure 0.35Mpa in the epimere tower, temperature is 155 ℃ in the hydrops that certain altitude is arranged, hypomere tower.The epimere top that condensed liquid in urea preparing process enters desorption tower 4 contacts with the back flow of gas that rises in defluent process, is heated and stripping cutting out partial NH
3And CO
2After being forced into 1.6Mpa, the pump 5 of hydrops outflow through linking to each other with desorption tower 4 of desorption tower 4 epimeres send into the interchanger 6 that links to each other with hydrolysis tower 7, with interchanger 6 that hydrolysis tower 7 links to each other in heat up with the following liquid heat exchange of hydrolysis tower 7, temperature rises to 155 ℃, enters the top of hydrolysis tower 7 epimeres.Hydrolysis tower 7 also is divided into two sections, 165 ℃ of epimere pressure 1.55Mpa, temperature, and hypomere pressure 1.7Mpa, temperature are more than 190 ℃, middle isolated, the two sections of hydrolysis tower 7 are communicated with by two inverted-loop tubes, and one is the hydrops inflow hypomere of epimere, and another root is that the gas of hypomere flows into epimere.The liquid that enters hydrolysis tower 7 epimeres is heated and stripping cutting out partial NH with the ascending gas counter current contact in the decline process
3And CO
2, enter the top of hydrolysis tower 7 hypomeres then through inverted-loop tube.Pressure 2.5Mpa, the middle pressure steam that temperature is 220 ℃ enters hydrolysis tower 7 and keeps its hypomere internal temperature more than 190 ℃ from a plurality of height orientation of hydrolysis tower 7 hypomeres, these middle pressure steams are the liquid heat stripping to flowing downward in uphill process, isolates NH wherein
3And CO
2And urea is heated be hydrolyzed into MH
3And CO
2, the ascending gas of hydrolysis tower 7 hypomeres enters the bottom of the epimere of hydrolysis tower 7 through inverted-loop tube, and the liquid heat stripping that in uphill process hydrolysis tower 7 epimere tops is flow down is isolated NH wherein
3And CO
2, giving vent to anger of hydrolysis tower 7 comes out to enter the bottom of desorption tower 4 epimeres from the top, and enters NH the condensed liquid in urea preparing process of desorption tower 4 with the gas that comes from the desorption tower 4 bottoms heating stripping that rises
3And CO
2Interchanger 6 heat exchange that the following liquid of hydrolysis tower 7 bottoms flows out through linking to each other with hydrolysis tower 7 from the bottom are cooled to 185 ℃, enter the top of desorption tower 4 hypomeres then, and the low-pressure steam counter current contact stripping that comes with 4 times pars infrasegmentalises of desorption tower goes out NH wherein in dirty process
3And CO
2, the gas of desorption tower 4 hypomeres gas hood 12 in tower enters epimere, the NH under desorption tower 4 bottoms in the liquid
3Content is reduced to below the 25ppm, CO
2, urea separates substantially fully, following liquid is flowed out by the bottom of desorption tower 4 and enter self-circulating water system 13 after interchanger 3 cooling.The 0.35Mpa that gives vent to anger of desorption tower 4 comes out to enter reflux exchanger 8 by the top, and portion gas is condensed into liquid in flow condenser 8, wherein contains water and more NH
3And CO
2, and after 9 pressurizations of the pump through linking to each other with reflux exchanger 8 again the circulation top recirculation that flows into desorption tower 4 epimeres separate, the gas that is not condensed in the flow condenser 8 flows into outer workshop section low pressure condensation absorption system 14 and absorbs.
Claims (4)
1. a device for processing urea process condensate comprises the condensed liquid in urea preparing process groove (1) that pump (2) is installed, and it is characterized in that: condensed liquid in urea preparing process groove (1) links to each other with interchanger (3) through pump (2); Desorption tower (4) is divided into epimere and hypomere, and gas hood (12) is installed between epimere and the hypomere, and described gas hood (12) is at the last intersegmental part of desorption tower (4), and hypomere is provided with low-pressure steam inlet mouth (10); Described interchanger (3) links to each other by the top of pipeline with the epimere of desorption tower (4), and the bottom of the epimere of desorption tower (4) links to each other by pump (5) that links to each other with desorption tower (4) and the interchanger (6) that links to each other with hydrolysis tower (7); Hydrolysis tower (7) is divided into epimere and hypomere, is communicated with by two inverted-loop tubes between epimere and the hypomere, and hypomere is provided with middle pressure steam inlet mouth (11); The interchanger (6) that links to each other with hydrolysis tower (7) links to each other with hydrolysis tower (7) epimere top, the top of described hydrolysis tower (7) epimere links to each other with desorption tower (4) epimere, desorption tower (4) epimere top links to each other with condensation absorption system (14) by reflux exchanger (8), and the bottom of reflux exchanger (8) links to each other with the epimere top of desorption tower (4) by the pump (9) that links to each other with reflux exchanger (8); The bottom of described hydrolysis tower (7) hypomere links to each other with the top of desorption tower (4) hypomere by the interchanger (6) that links to each other with hydrolysis tower (7), and the bottom of desorption tower (4) hypomere links to each other with self-circulating water system (13) by interchanger (3).
2. device for processing urea process condensate according to claim 1 is characterized in that: described gas hood (12) is higher than the link to each other position of pipe joint of pump (5) that the bottom of the epimere of desorption tower (4) links to each other with desorption tower (4).
3. device for processing urea process condensate according to claim 1 is characterized in that: the position that the top of described hydrolysis tower (7) epimere links to each other with desorption tower (4) epimere is higher than the position that pump (5) that the bottom of the epimere of desorption tower (4) links to each other with desorption tower (4) links to each other.
4. device for processing urea process condensate according to claim 1 is characterized in that: described middle pressure steam inlet mouth (11) is at least one.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202577588U CN201545718U (en) | 2009-11-02 | 2009-11-02 | Urea process condensed fluid treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202577588U CN201545718U (en) | 2009-11-02 | 2009-11-02 | Urea process condensed fluid treatment device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201545718U true CN201545718U (en) | 2010-08-11 |
Family
ID=42600885
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202577588U Expired - Fee Related CN201545718U (en) | 2009-11-02 | 2009-11-02 | Urea process condensed fluid treatment device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201545718U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103058436A (en) * | 2012-12-25 | 2013-04-24 | 中国海洋石油总公司 | Method for reducing content of ammonia nitrogen in urea process condensate |
| CN103936091A (en) * | 2013-12-26 | 2014-07-23 | 重庆宜化化工有限公司 | Weak liquid distillation method |
| CN105413406A (en) * | 2015-12-27 | 2016-03-23 | 安徽淮化股份有限公司 | Recycling system of ammonia gas in emptying tail gas and operation method therefor |
| CN112495323A (en) * | 2020-11-27 | 2021-03-16 | 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 |
-
2009
- 2009-11-02 CN CN2009202577588U patent/CN201545718U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103058436A (en) * | 2012-12-25 | 2013-04-24 | 中国海洋石油总公司 | Method for reducing content of ammonia nitrogen in urea process condensate |
| CN103936091A (en) * | 2013-12-26 | 2014-07-23 | 重庆宜化化工有限公司 | Weak liquid distillation method |
| CN103936091B (en) * | 2013-12-26 | 2015-09-02 | 重庆宜化化工有限公司 | A kind of light liquid distil process method |
| CN105413406A (en) * | 2015-12-27 | 2016-03-23 | 安徽淮化股份有限公司 | Recycling system of ammonia gas in emptying tail gas and operation method therefor |
| CN105413406B (en) * | 2015-12-27 | 2017-10-24 | 安徽淮化股份有限公司 | The recovery system and its operating method of gas ammonia in a kind of emptying end gas |
| CN112495323A (en) * | 2020-11-27 | 2021-03-16 | 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 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100811 Termination date: 20121102 |