CN100400430C - Energy saving, purifying and recovering process for urea process condensate - Google Patents
Energy saving, purifying and recovering process for urea process condensate Download PDFInfo
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- CN100400430C CN100400430C CNB2006100439832A CN200610043983A CN100400430C CN 100400430 C CN100400430 C CN 100400430C CN B2006100439832 A CNB2006100439832 A CN B2006100439832A CN 200610043983 A CN200610043983 A CN 200610043983A CN 100400430 C CN100400430 C CN 100400430C
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Abstract
The present invention discloses an energy-saving purifying and recovering process for urea process condensate. After sent to a first heat exchanger and a second heat exchanger by a feeding pump, the urea process condensate carries out an exchange with waste liquid discharged from the bottom part of a hydrolyzing tower. The temperature of materials discharged by the heat exchangers is from 160 to 170DEG C. The materials enter tower disks above the hydrolyzing tower, pass through multiple layers of the tower disks, and then, reach a distillation effect by passing through gradient overflow falling liquid in the tower disks. After the materials enter a distributing device by passing through the tower disks and steam among the tower disks to rise the temperature, the materials flow into the tower bottom, and then, are further heated by a third heat exchanger at the tower bottom for causing residue urea to be decomposed. Carbon dioxide gas and the steam are added at the tower bottom by a gas mixing device for causing ammonia and the urea to be reduced to be not less than or equal to 10 ppm. Then, heat quantity is recovered by the heat exchange of the first heat exchanger and the second heat exchanger, and the waste liquid is recovered for use after the temperature of the waste liquid is reduced. The present invention can reach discharge standards required by national environmental protection, reduce consumption, etc.
Description
Technical field
The present invention relates to effluent purifying technology in the Chemicals production, is a kind of energy saving, purifying and recovering process for urea process condensate.
Background technology
The production of urea has reached 3,800 ten thousand tons/year, occupies first place in the world.Yet urea contaminated wastewater aborning is more serious, to this, this area had been developed different waste water treatment process in recent years, but did not find a kind of technology of comparative maturity so far yet, when making condensed liquid in urea preparing process reach emission standard, and reduce consumption.Its emission standard of treatment process of the process condensate of external report is lower than domestic disclosed treatment process, and still, technology and equipment are all complicated, the processing cost height.
Summary of the invention
The objective of the invention is, a kind of energy saving, purifying and recovering process for urea process condensate is provided, it can reach the emission standard of national requirements for environmental protection, and can reduce consumption etc.
The present invention is achieved through the following technical solutions for achieving the above object: energy saving, purifying and recovering process for urea process condensate, condensed liquid in urea preparing process is sent into the waste liquid of discharging behind first interchanger and second interchanger by feeding pump bottom hydrolysis tower exchange, the temperature of charge that goes out second interchanger is 160-170 ℃, enter hydrolysis tower top tower tray, through the multilayer tower tray, through the gradient overflow in the tower tray liquid falls again, reach distilling effect, material enters distribution apparatus through the steam between tower tray and the tower tray again and elevates the temperature at the bottom of the back flows into tower, further heat by the 3rd interchanger at the bottom of the tower again, remaining urea is decomposed, at the bottom of tower, add carbon dioxide and steam by gas mixer, ammonia and urea are reduced to≤10ppm, and then through first interchanger and second interchanger heat exchange recovery heat, reclaim use after reducing waste liquid temperature, process condensate is through adding thermal distillation, gas is carried ammonia and the carbonic acid gas that obtains, water mixed gas enters reflux exchanger through hydrolysis tower and absorption cell, the first ammonium liquid that generates enters the backflow liquid bath again, send the heat energy utilization section to make phegma by condensate pump pressurization back one tunnel, uncooled gas is sent to urea plant by the backflow liquid bath, the overhead condenser water coolant enters the warm water water cooler after absorbing heat, recycles with the warm water recycle pump behind the employing ornithine cycle water for cooling.Bubble-cap in the hydrolysis tower on the tower tray is closed the connection with Steam Pipe, fixedlys connected with the top board of bubble-cap in the top of Steam Pipe, and the top of Steam Pipe is provided with opening, and the bottom of bubble-cap is connected with Steam Pipe.Gradient overflow liquid discharging plate is installed on the tower tray in the hydrolysis tower.Gradient overflow liquid discharging plate has riser and transverse slat, and riser vertically is connected with transverse slat, perforate on the transverse slat.The top of transverse slat is a waviness.Offer the long strip shape hole on the circumferential wall of bubble-cap.Vapor distributor is installed in the hydrolysis tower bottom, and clog-free spiral nozzle is installed on the circulating line on the vapor distributor.The hydrolysis tower epimere is provided with ammonium fluid body pipe joint, below ammonium fluid body pipe joint the reflux pipeline interface is set, and the hydrolysis tower stage casing is provided with the first steam-pipe interface and the second steam-pipe interface, and section is provided with the 3rd steam-pipe interface at the bottom of the hydrolysis tower.
Positively effect of the present invention is outstanding: under the emission standard that has reached national requirements for environmental protection, reduced consumption by a relatively large margin, the vapor pressure of employing is 1.3-1.8Mpa, and the user can adjust accordingly as required; Adopt the ammoniacal liquor of different concns to carry out staged and layered backflow adding, the unnecessary ammoniacal liquor of condensed liquid in urea preparing process and synthetic ammonia is handled in the lump, process simplification, and the operation investment cost reduces; Outer the 3rd interchanger that is provided with can improve steam utilization to greatest extent at the bottom of the hydrolysis tower, and the interior temperature of charge height of hydrolysis tower is easily decomposed, but promptly in order to be effective save energy again; The gradient overflow liquid discharging plate that increases in hydrolysis tower can make the liquid distribution gradient in the tower, has prolonged the residence time, thereby has guaranteed mass-and heat-transfer efficient, makes recovering effect good; Hydrolysis condensate liquid part is pressed absorption system in returning with the form of first ammonium liquid, has reduced water amount, utilizes the control of systematic water balance, has also reduced low pressure simultaneously and has absorbed load.The effect that promptly provides heat to play system's ftercompction again, easy handling are provided through staged and layered in the position that steam of the present invention adds; For making urea production have continuity, require the cycle of operation long, producing load should not fluctuate too big, the present invention has designed the totally enclosed bubble-cap, it is good to have satisfied mass transfer effect, turndown ratio is big, and gas phase revolution is the pressure drop minimum during by Steam Pipe, condition such as kept good bubbling effect and tower tray debugging, can not overhaul substantially after installing; Liqiud-gas mixing device of the present invention has guaranteed the uniform mixing of material; Reclaim ammonia and the urea in the process condensate, reduced consumption, improved economic benefit etc.
Description of drawings
Embodiment
Energy saving, purifying and recovering process for urea process condensate of the present invention, the waste liquid that condensed liquid in urea preparing process is sent into first interchanger 5 and second interchanger, 4 backs and the discharge of hydrolysis tower 2 bottoms by feeding pump 8 exchanges, the temperature of charge that goes out second interchanger 4 is 160-170 ℃, enter hydrolysis tower 2 top tower trays, through the multilayer tower tray, through the gradient overflow in the tower tray liquid falls again, reach distilling effect, material enters distribution apparatus through the steam between tower tray and the tower tray again and elevates the temperature at the bottom of the back flows into tower, further heat by the 3rd interchanger 3 at the bottom of the tower again, remaining urea is decomposed, at the bottom of tower, add carbon dioxide and steam by gas mixer 1, ammonia and urea are reduced to≤10ppm, and then through first interchanger 5 and second interchanger, 4 heat exchange recovery heat, reclaim use after reducing waste liquid temperature, process condensate is through adding thermal distillation, gas is carried ammonia and the carbonic acid gas that obtains, water mixed gas enters reflux exchanger 9 through hydrolysis tower 2 and absorption cell 6, the first ammonium liquid that generates enters backflow liquid bath 10 again, send the heat energy utilization section to make phegma by condensate pump 7 pressurization backs one tunnel, uncooled gas is sent to urea plant by backflow liquid bath 10, the overhead condenser water coolant enters warm water water cooler 13 after absorbing heat, recycles with warm water recycle pump 11 behind the employing ornithine cycle water for cooling.Bubble-cap 27 in the hydrolysis tower 2 on the tower tray 26 is closed connections with Steam Pipe 28, fixedlys connected with the top board of bubble-cap 27 in the top of Steam Pipe 28, and the top of Steam Pipe 28 is provided with opening 18, and the bottom of bubble-cap 27 is connected with Steam Pipe 28.Gradient overflow liquid discharging plate 19 is installed on the tower tray 26 in the hydrolysis tower 2.Gradient overflow liquid discharging plate 19 has riser 20 and transverse slat 21, and riser 20 vertically is connected with transverse slat 21, perforate on the transverse slat 21.The top of transverse slat 21 is wavinesss.Offer long strip shape hole 29 on the circumferential wall of bubble-cap 27.Vapor distributor 23 is installed in hydrolysis tower 2 bottoms, and clog-free spiral nozzle 22 is installed on the circulating line on the vapor distributor 23.Hydrolysis tower 2 epimeres are provided with ammonium fluid body pipe joint 14, below ammonium fluid body pipe joint 14, reflux pipeline interface 15 is set, hydrolysis tower 2 stage casings are provided with the first steam-pipe interface 16 and the second steam- pipe interface 25, and 2 end of hydrolysis tower section is provided with the 3rd steam-pipe interface 17.The steam of technology middle steam tube of the present invention is 1.3-1.8Mpa, the flow of steam is controlled by variable valve, one the tunnel advance the 3rd interchanger 3 heat exchange of outside at the bottom of the tower after, through first interchanger 5 with directly add in the hydrolysis towers 2 after second interchanger 4 further improves steam utilizations from different positions, make full use of steam thermal energy and carry out mass-and heat-transfer, the CO that another road steam and carbon dioxide compressor come
2Go into hydrolysis tower 2 bottoms through gas mixer 1 is laggard behind the gas regulation flow, to satisfy the needs of energy-saving and purifying.Hydrolysis tower 2 top backflow add-ons of the present invention can make ammonia absorb, and do not influence the purification recovering effect of process condensate and material, temperature equilibrium simultaneously.The top absorption cell 6 that the present invention increases at hydrolysis tower 2 tops is made absorption liquid with tower item phlegma, progressively recovery part ammonia and CO
2, the mixture that goes out absorption cell 6 enters cat head warm water condenser 13 and further reclaims ammonia, CO
2, adopt ammonium fluid to add the backflow of hydrolysis tower 2 tops simultaneously from the urea battery limit (BL), process condensate decomposes to increase, the effect of desorb.The present invention increases the method that the steam-pipe interface adds steam in hydrolysis tower 2 stage casings, promptly save steam consumption, has played the effect of system pressure stable operation again.Technology of the present invention is with the urea in the not labile process condensate under traditional desorption condition, under higher temperature and suitable pressure, through hydrolysis reaction, transform ammonification and carbonic acid gas, the first ammonium liquid that ammonia, carbonic acid gas and hydrolysis is generated through retrieving arrangement is recovered in the urea production and goes then.Raffinate after the desorb is up to standard.After purifying, reclaim to use, reached the purpose that not only reclaims urea but also reclaiming clean water.
A represents ammonium fluid from the urea battery limit (BL) among Fig. 1, and H represents that fixed gas removes urea plant, G represents that cooling water goes out-of-bounds, and F represents cooling water from out-of-bounds, and E represents process condensate From urea production, D represents the reuse of purifying waste water, and C represents the steam source, and B represents carbon dioxide Compression enters mixing arrangement 1,12nd, process condensate liquid bath. The 24th, clog-free spiral nozzle. This Inventing not, detailed description is known technology.
Claims (8)
1. energy saving, purifying and recovering process for urea process condensate, it is characterized in that: the waste liquid that condensed liquid in urea preparing process is sent into first interchanger (5) and the discharge bottom hydrolysis tower (2) of second interchanger (4) back by feeding pump (8) exchanges, the temperature of charge that goes out second interchanger (4) is 160-170 ℃, enter hydrolysis tower (2) top tower tray, through the multilayer tower tray, through the gradient overflow in the tower tray liquid falls again, reach distilling effect, material enters distribution apparatus through the steam between tower tray and the tower tray again and elevates the temperature at the bottom of the back flows into tower, again by further heating of the 3rd interchanger (3) at the bottom of the tower, remaining urea is decomposed, at the bottom of tower, add carbon dioxide and steam by gas mixer (1), ammonia and urea are reduced to≤10ppm, and then through first interchanger (5) and second interchanger (4) heat exchange recovery heat, reclaim use after reducing waste liquid temperature, process condensate is through adding thermal distillation, gas is carried ammonia and the carbonic acid gas that obtains, water mixed gas enters reflux exchanger (9) through hydrolysis tower (2) and absorption cell (6), the first ammonium liquid that generates enters backflow liquid bath (10) again, send the heat energy utilization section to make phegma by condensate pump (7) pressurization back one tunnel, uncooled gas is sent to urea plant by backflow liquid bath (10), the overhead condenser water coolant enters warm water water cooler (13) after absorbing heat, recycles with warm water recycle pump (11) behind the employing ornithine cycle water for cooling.
2. energy saving, purifying and recovering process for urea process condensate according to claim 1, it is characterized in that: the bubble-cap (27) in the hydrolysis tower (2) on the tower tray (26) is closed the connection with Steam Pipe (28), fixedly connected with the top board of bubble-cap (27) in the top of Steam Pipe (28), the top of Steam Pipe (28) is provided with opening (18), and the bottom of bubble-cap (27) is connected with Steam Pipe (28).
3. energy saving, purifying and recovering process for urea process condensate according to claim 1 and 2 is characterized in that: tower tray (26) is gone up gradient overflow liquid discharging plate (19) is installed in the hydrolysis tower (2).
4. energy saving, purifying and recovering process for urea process condensate according to claim 3 is characterized in that: gradient overflow liquid discharging plate (19) has riser (20) and transverse slat (21), and riser (20) vertically is connected with transverse slat (21), and transverse slat (21) is gone up perforate.
5. energy saving, purifying and recovering process for urea process condensate according to claim 4 is characterized in that: the top of transverse slat (21) is a waviness.
6. energy saving, purifying and recovering process for urea process condensate according to claim 2 is characterized in that: offer long strip shape hole (29) on the circumferential wall of bubble-cap (27).
7. according to claim 1 or 4 described energy saving, purifying and recovering process for urea process condensate, it is characterized in that: vapor distributor (23) is installed in hydrolysis tower (2) bottom, and clog-free spiral nozzle (22) is installed on the circulating line on the vapor distributor (23).
8. energy saving, purifying and recovering process for urea process condensate according to claim 7, it is characterized in that: hydrolysis tower (2) epimere is provided with ammonium fluid body pipe joint (14), in ammonium fluid body pipe joint (14) below reflux pipeline interface (15) is set, hydrolysis tower (2) stage casing is provided with the first steam-pipe interface (16) and the second steam-pipe interface (25), and hydrolysis tower (2) end section is provided with the 3rd steam-pipe interface (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100439832A CN100400430C (en) | 2006-05-18 | 2006-05-18 | Energy saving, purifying and recovering process for urea process condensate |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2006100439832A CN100400430C (en) | 2006-05-18 | 2006-05-18 | Energy saving, purifying and recovering process for urea process condensate |
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| CN1858005A CN1858005A (en) | 2006-11-08 |
| CN100400430C true CN100400430C (en) | 2008-07-09 |
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| CNB2006100439832A Expired - Fee Related CN100400430C (en) | 2006-05-18 | 2006-05-18 | Energy saving, purifying and recovering process for urea process condensate |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103030665A (en) * | 2012-12-11 | 2013-04-10 | 安徽国星生物化学有限公司 | Water-washing purification method of chlorpyrifos |
| CN103058436B (en) * | 2012-12-25 | 2014-01-08 | 中国海洋石油总公司 | Method for reducing content of ammonia nitrogen in urea process condensate |
| CN104477939B (en) * | 2014-10-28 | 2017-01-18 | 河南骏化发展股份有限公司 | Low-pressure hydrolysis technology |
| CN112495323B (en) * | 2020-11-27 | 2021-11-09 | 昱创(天津)化工科技有限公司 | For CO2Medium-pressure desorption hydrolysis tower for gas stripping urea production and energy-saving production increasing method |
Citations (7)
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|---|---|---|---|---|
| US4410503A (en) * | 1981-02-28 | 1983-10-18 | Unie Van Kunst-Mestfabrieken | Process for the removal of urea, ammonia, and carbon dioxide from dilute aqueous solutions |
| US4456535A (en) * | 1980-11-28 | 1984-06-26 | Unie Van Kunstmestfabrieken, B.V. | Process for the removal of urea, ammonia, and carbon dioxide from dilute aqueous solutions |
| CN88101281A (en) * | 1987-03-13 | 1988-09-28 | 东洋工程株式会社 | The hydrolysis of urea method of low concentration urea solution |
| CN1050171A (en) * | 1989-09-15 | 1991-03-27 | 斯南普罗吉蒂联合股票公司 | The purifying treatment of effluent from urea production plants |
| US5223238A (en) * | 1992-01-16 | 1993-06-29 | The M. W. Kellogg Company | Method for treating ammonia and urea condensates |
| CN2637484Y (en) * | 2003-08-14 | 2004-09-01 | 宁波远东化工科技有限公司 | Synthetic ammonia, urea waste liquid treatment device |
| CN1539748A (en) * | 2003-10-31 | 2004-10-27 | 刘金成 | Technique for recycling waste fluid containing urea |
-
2006
- 2006-05-18 CN CNB2006100439832A patent/CN100400430C/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4456535A (en) * | 1980-11-28 | 1984-06-26 | Unie Van Kunstmestfabrieken, B.V. | Process for the removal of urea, ammonia, and carbon dioxide from dilute aqueous solutions |
| US4410503A (en) * | 1981-02-28 | 1983-10-18 | Unie Van Kunst-Mestfabrieken | Process for the removal of urea, ammonia, and carbon dioxide from dilute aqueous solutions |
| CN88101281A (en) * | 1987-03-13 | 1988-09-28 | 东洋工程株式会社 | The hydrolysis of urea method of low concentration urea solution |
| CN1050171A (en) * | 1989-09-15 | 1991-03-27 | 斯南普罗吉蒂联合股票公司 | The purifying treatment of effluent from urea production plants |
| US5223238A (en) * | 1992-01-16 | 1993-06-29 | The M. W. Kellogg Company | Method for treating ammonia and urea condensates |
| CN2637484Y (en) * | 2003-08-14 | 2004-09-01 | 宁波远东化工科技有限公司 | Synthetic ammonia, urea waste liquid treatment device |
| CN1539748A (en) * | 2003-10-31 | 2004-10-27 | 刘金成 | Technique for recycling waste fluid containing urea |
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Assignee: Anhui Jinmei Zhongneng Chemical Co.,Ltd. Assignor: Liu Guosheng|Li Honglin Contract record no.: 2011340000241 Denomination of invention: Energy saving, purifying and recovering process for urea process condensate Granted publication date: 20080709 License type: Exclusive License Open date: 20061108 Record date: 20110803 |
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080709 Termination date: 20180518 |