CN101607168B - Process and equipment for treating melamine tail gas - Google Patents
Process and equipment for treating melamine tail gas Download PDFInfo
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- CN101607168B CN101607168B CN2009100172420A CN200910017242A CN101607168B CN 101607168 B CN101607168 B CN 101607168B CN 2009100172420 A CN2009100172420 A CN 2009100172420A CN 200910017242 A CN200910017242 A CN 200910017242A CN 101607168 B CN101607168 B CN 101607168B
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- cleaning solution
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Abstract
The invention discloses a process and equipment for treating melamine tail gas. The process comprises the following steps: tail gas generated by melamine is delivered to a condensation chamber below an ammonium carbamate generator of form ammonium carbamate solution; unabsorbed tail gas in the condensation chamber goes up to a washing chamber above the ammonium carbamate generator to form ammonium carbamate solution; the ammonium carbamate solutions generated in the two steps are discharged through an ammonium carbamate delivery pipe at the bottom of the ammonium carbamate generator and are stored; the unabsorbed tail gas in the washing chamber is discharged through a gas discharging outlet at the top of the ammonium carbamate generator, enters a tail gas condenser, and is washed and absorbed in the tail gas condenser with washing liquid ejected by a shower pipe inside the tail gas condenser; remnant gas condensed and absorbed in the tail gas condenser is discharged to an ordinary pressure absorption tower, and is washed and absorbed in the ordinary pressure absorption tower with washing liquid ejected by a shower pipe inside the ordinary pressure absorption tower; and the remnant gas washed and absorbed in the ordinary pressure absorption tower is discharged into air. The invention has the advantages of high concentration of generated ammonium carbamate solutions, high tail gas recovery rate, and the like.
Description
Technical field
The present invention relates to combined production of melamine urea production process field, specifically is melamine tail gas treatment process and equipment in a kind of combined production of melamine urea production.
Background technology
In the combined production of melamine urea technique, be transported in the urea production after tail gas need reclaim after the Melamine Production and use, it is to adopt the absorption tower to reclaim that existing melamine tail gas reclaims method commonly used, in the absorption tower, cleaning solution descends from tower top spray, and tail gas enters the back and carries out reverse absorption with cleaning solution at the bottom of tower, and the liquid after the absorption is sent in the urea system high concentration carbon ammonium liquid bath, carry dense back through desorb, hydrolysis and form first ammonium liquid, send in the urea production process and use.The ammonia in the first ammonium liquid that this method forms and the content of carbon dioxide are all very low, water content is higher, to reduce the conversion ratio of urea synthesizer greatly during coproduction urea, cause the urea synthesizer water-returning rate too high, water-returning rate generally can reach 50%-60%, very big to the carbamide production system influence, and in the process of desorb and hydrolysis, increased the consumption of vapour, water, electricity, cause and produce the load raising, cost increases, and arranges ammon amount height in the waste gas of atmosphere again after reclaiming through the treated device of existing melamine tail gas simultaneously, causes serious environmental to pollute.
Summary of the invention
One of purpose of the present invention is to provide a kind of melamine tail gas treatment process and equipment, it can solve the deficiency that exists in the known technology, by multiple tracks technologies such as first ammonium maker are set melamine tail gas is reclaimed, directly generate high concentration first ammonium salt solution, this first ammonium salt solution water content is little, contains ammonia and amount of carbon dioxide height, being beneficial to coproduction urea more uses, this technology absorbs fully melamine tail gas simultaneously, has significantly reduced the ammon amount of final emission gases, reduces environmental pollution.
Two of purpose of the present invention is to provide above-mentioned melamine tail gas treatment process employed melamine tail gas treatment facility,
The present invention is achieved through the following technical solutions for achieving the above object: the melamine tail gas treatment process comprises following technology:
(1), tail gas generated by melamine is transported to the condensation chamber of first ammonium maker bottom, the heat exchanger place carries out condensation and absorbs in condensation chamber, forms the first ammonium salt solution;
(2), unabsorbed tail gas rises and enters the washing cavities on first ammonium maker top in the condensation chamber, wash absorption, form the first ammonium salt solution with the cleaning solution of washing cavities upper spray pipe ejection;
(3), the first ammonium salt solution that produces in above-mentioned two step process is discharged and is stored through first ammonium maker bottom first ammonium liquid carrier pipe;
(4), unabsorbed tail gas is discharged by first ammonium maker top vent in the washing cavities, enters tail gas condenser, the cleaning solution with the ejection of tail gas condenser internal sparger pipe in tail gas condenser washs absorption;
(5), the survival gas after absorbing through condensation in the tail gas condenser is discharged into the normal pressure absorption tower, the cleaning solution with the ejection of normal pressure absorption tower internal sparger pipe in the normal pressure absorption tower washs absorption;
(6), absorbing the back survival gas through washing in the normal pressure absorption tower is discharged in the atmosphere.
Part first ammonium liquid enters the circulation fluid pipe through first ammonium carrier pipe, enters the air inlet pipe and the condensation chamber middle and upper part of first ammonium maker again through the circulation fluid pipe, and this part first ammonium liquid enters behind the condensation chamber wherein gas and liquid stir.
The liquid that produces in the described tail gas condenser is transported to the cleaning solution cooler through the cleaning solution carrier pipe of tail gas condenser bottom, this liquid cools off in the cleaning solution cooler, form cleaning solution, cleaning solution enters the shower of the washing cavities on first ammonium maker top, is absorbed by shower ejection and the capable washing of washing intracavity gas.
Part cleaning solution and first ammonium liquid are collected through the liquid collecting cavity of washing cavities bottom in the described washing cavities, flow into the cleaning solution cooler by circulation pipe then, this liquid cools off in the cleaning solution cooler, form cleaning solution, this cleaning solution enters the shower of the washing cavities on first ammonium maker top, is absorbed by shower ejection and the capable washing of washing intracavity gas.
The melamine tail gas treatment facility that described melamine tail gas treatment process uses, comprise first ammonium maker, first ammonium maker bottom is a condensation chamber, top is washing cavities, washing cavities communicates with condensation chamber, be installed into tracheae and first ammonium liquid carrier pipe on the outer wall of condensation chamber bottom, first ammonium liquid carrier pipe apart from the distance of first ammonium maker bottom surface less than the distance of air inlet pipe apart from first ammonium maker bottom surface, mounting heat exchanger in the condensation chamber, packing layer is installed in the bottom in the washing cavities, shower is installed on washing cavities top, the washing cavities top is provided with exhaust outlet, exhaust outlet is communicated with the tail gas condenser air inlet by pipeline, and the tail gas condenser upper air vent is communicated with normal pressure absorption tower air inlet by pipeline, and normal pressure absorption tower exhaust outlet communicates with atmosphere.
Described heat exchanger is made up of many " U " type heat exchanger tubes, first ammonium maker bottom is provided with intake antrum and water chamber, intake antrum is communicated with cooling water inlet pipe and " U " type heat exchanger tube water inlet respectively, and water chamber is communicated with cooling water outlet pipe and " U " type heat exchanger tube delivery port respectively.
On described condensation chamber outer wall middle and upper part and the air inlet pipe circulation fluid pipe is installed respectively, circulation fluid Guan Yujia ammonium liquid carrier pipe is communicated with.
Install on the outer wall of described condensation chamber bottom and divide air cavity, divide the tail gas import is installed on the air cavity, offer some air inlets on the outer wall of condensation chamber bottom with on the corresponding position of minute air cavity.
The cleaning solution carrier pipe is installed in described tail gas condenser bottom, the cleaning solution carrier pipe is connected with the cleaning solution cooler, the cleaning solution cooler is communicated with shower, liquid collecting cavity is installed around the bottom in the washing cavities, the cleaning solution drain pipe is installed on the outer wall of washing cavities bottom, and the cleaning solution drain pipe is respectively at being communicated with liquid collecting cavity and cleaning solution cooler.
Beneficial effect of the present invention is: tail gas enters and carries out the two-stage absorption in the first ammonium maker, improved the tail gas absorption efficiency greatly, ammonia and concentration of carbon dioxide height in the first ammonium liquid that is generated, water content is low, ammonia and gas concentration lwevel can reach 70%-80%, can significantly improve the conversion ratio of urea synthesizer during coproduction urea, reduce water-returning rate, the urea synthesizer water-returning rate only is about 30% during this technology coproduction urea, has improved the production efficiency of coproduction urea greatly; The ammonium carbamate concentration height that this technology generates, need not to carry out desorb and hydrolytic process can use by coproduction urea, reduced the consumption of vapour, water, electricity, reduced production cost, existing relatively combined production of melamine urea tail gas treatment process, the present invention extracts ammonia per ton and can save energy 2.2kj, saves 3.95 tons of steam; Tail gas is fully absorbed through the recycling of multiple tracks technology, finally arranges in the gas of atmosphere, and ammon amount is extremely low, reduces environmental pollution greatly; Existing relatively technology, the present invention has improved production efficiency when technology is more succinct, reduced production cost etc.; Melamine tail gas treating apparatus of the present invention has the ammonium carbamate concentration of generation height; Tail gas recycle rate height; Simple for structure reasonable; Low cost and other advantages.
Description of drawings
Accompanying drawing 1 is a structural representation of the present invention; Accompanying drawing 2 is structural representations of first ammonium maker among the present invention.
The specific embodiment
The present invention will be further described for the contrast accompanying drawing:
The melamine tail gas treatment process comprises following technology:
1, tail gas generated by melamine is transported to the condensation chamber of first ammonium maker bottom, and the heat exchanger place carries out the condensation absorption in condensation chamber, forms the first ammonium salt solution;
2, the interior unabsorbed tail gas rising of condensation chamber enters the washing cavities on first ammonium maker top, and the cleaning solution that sprays with the washing cavities upper spray pipe washs absorption, forms the first ammonium salt solution;
3, the first ammonium salt solution that produces in above-mentioned two step process is discharged and storage through first ammonium maker bottom first ammonium liquid carrier pipe, condensation absorbs and washing absorbs the absorption of two steps owing to tail gas in first ammonium maker has passed through, therefore the first ammonium liquid that forms in the first ammonium maker contains ammonia and concentration of carbon dioxide height, water content is low, need not to use in order to coproduction urea through desorb and hydrolysis, when coproduction urea, can significantly improve the conversion ratio of urea synthesizer, improve the production efficiency of coproduction urea, reduced energy consumption;
4, unabsorbed tail gas is discharged by first ammonium maker top vent in the washing cavities, enters tail gas condenser, and the cleaning solution with the ejection of tail gas condenser internal sparger pipe in tail gas condenser washs absorption;
5, be discharged into the normal pressure absorption tower through the survival gas after the condensation absorption in the tail gas condenser, the cleaning solution with the ejection of normal pressure absorption tower internal sparger pipe in the normal pressure absorption tower washs absorption;
6, absorbing the back survival gas through washing in the normal pressure absorption tower is discharged in the atmosphere.
When the two-stage of melamine tail gas process first ammonium maker absorbs, there are 90% ammonia and carbon dioxide to be absorbed approximately, when the washing of process tail gas condenser absorbs, the ammonia and the carbon dioxide of residue 10% are absorbed, the washing on the final normal pressure of process again absorption tower absorbs, basic ammonia and the carbon dioxide realized reclaims fully, makes full use of resource in the melamine tail gas, reduces the pollution of tail gas to environment.
Of the present invention being further characterized in that: in order to improve the absorptivity in the first ammonium maker, part first ammonium liquid is transported to the circulation fluid pipe through first ammonium carrier pipe, enter the air inlet pipe and the condensation chamber middle and upper part of first ammonium maker again through the circulation fluid pipe, this part first ammonium liquid enters behind the condensation chamber wherein gas and liquid is stirred, thereby improves the absorptivity of ammonia and carbon dioxide.
In order to reduce the use of cleaning solution, reduce production costs, the cleaning solution carrier pipe of liquid through the tail gas condenser bottom that produces in the tail gas condenser is transported to the cleaning solution cooler, this liquid cools off in the cleaning solution cooler, form cleaning solution, cleaning solution enters the shower of the washing cavities on first ammonium maker top, is absorbed by shower ejection and the capable washing of washing intracavity gas.Be further characterized in that in the present embodiment: part cleaning solution and first ammonium liquid are after the liquid collecting cavity of washing cavities bottom is collected in the washing cavities, flow into the cleaning solution cooler by circulation pipe, form cleaning solution, this cleaning solution enters the shower of the washing cavities on first ammonium maker top, wash absorption by shower ejection and washing intracavity gas, the present embodiment scheme can make full use of cleaning solution, reduces the use of cleaning solution, further reduces production costs.
The agent structure of the employed melamine tail gas treatment facility of melamine tail gas treatment process of the present invention has first ammonium maker 22, first ammonium maker 22 bottoms are condensation chambers 6, top is washing cavities 10, washing cavities 10 communicates with condensation chamber 6, be installed into tracheae 3 and first ammonium liquid carrier pipe 17 on the condensation chamber 6 bottom outer walls, air inlet pipe 3 communicates with the melamine tail gas carrier pipe, first ammonium liquid carrier pipe 17 apart from the distance of first ammonium maker 22 bottom surfaces less than the distance of air inlet pipe 3 apart from first ammonium maker 22 bottom surfaces, this design can make first ammonium liquid carrier pipe 17 be in first ammonium maker internal pressure maximum, can guarantee the concentration of Generation Liquid, improve ammonia and gas concentration lwevel in the first ammonium liquid.Mounting heat exchanger in the condensation chamber 6, packing layer 9 is installed in the bottom in the washing cavities 10, shower 13 is installed on washing cavities 10 tops, washing cavities 10 tops are provided with exhaust outlet 12, exhaust outlet 12 is communicated with tail gas condenser 24 air inlets by pipeline, tail gas condenser 24 upper air vents are communicated with normal pressure absorption tower 26 air inlets by pipeline, and normal pressure absorption tower 26 exhaust outlets communicate with atmosphere.
Heat exchanger of the present invention can be single heat exchange tube, annular heat exchanger tube etc., and preferred version of the present invention is that heat exchanger is made up of many " U " type heat exchanger tubes 16, and many " U " type heat exchanger tube 16 relative single heat exchange tubes etc. have the high advantage of heat exchange efficiency.Described first ammonium maker 22 bottoms are provided with intake antrum 2 and water chamber 18, intake antrum 2 is communicated with cooling water inlet pipe 1 and " U " type heat exchanger tube 16 water inlets respectively, water chamber 18 is communicated with cooling water outlet pipe 19 and " U " type heat exchanger tube 16 delivery ports respectively, cooling water enters intake antrum 2 by cooling water inlet pipe 1 and carries out heat exchange entering heat exchanger tube 16, flow into water chamber 18 after heat exchange is finished, flow out by cooling water outlet pipe 19 again.
Above-mentioned embodiment is further characterized in that: on condensation chamber 6 outer wall middle and upper parts and air inlet pipe 3 circulation fluid pipe 15 is installed respectively, circulation fluid pipe 15 is communicated with first ammonium liquid carrier pipe 17.Carry first ammonium liquid by circulation fluid pipe 15 in condensation chamber 6, first ammonium liquid carries out condensation with tail gas and absorbs in condensation chamber 6, and first ammonium liquid can also play stirring action simultaneously, thereby improves the absorptivity in the condensation chamber 6.
In order to reduce the use of cleaning solution, reduce production costs, cleaning solution carrier pipe 31 is installed in tail gas condenser 24 bottoms, cleaning solution carrier pipe 31 is connected with cleaning solution cooler 23, cleaning solution cooler 23 is communicated with shower 13, liquid collecting cavity 20 is installed around the bottom in the washing cavities 10, cleaning solution drain pipe 14 is installed on the washing cavities 10 bottom outer walls, cleaning solution drain pipe 14 is respectively at being communicated with liquid collecting cavity 20 and cleaning solution cooler 23, the liquid that reclaims in liquid that produces in the tail gas condenser 24 and the liquid collecting cavity 20 enters cleaning solution cooler 23 backs and forms cleaning solution, is transported to once more in the washing cavities 10 and uses, cleaning solution uses repeatedly, has reduced production cost.
In order to make tail gas can evenly enter condensation chamber 6, improve absorptivity, on condensation chamber 6 bottom outer walls, install and divide air cavity 4, dividing air cavity 4 is loop configuration, be centered around condensation chamber 6 outer wall outsides, tail gas import 3 is installed on the described minute air cavity 4, offer some air inlets 5 on the condensation chamber 6 bottom outer walls with on minute air cavity 4 corresponding positions, melamine tail gas enters branch air cavity 4 by tail gas import 3, some air inlets 5 on condensation chamber 6 outer walls enter condensation chamber 6 then, and tail gas is by after dividing air cavity 4, and it is more even to distribute, can not cause gas to block, help condensation and absorb.
Claims (10)
1. melamine tail gas treatment process is characterized in that: comprise following technology:
(1), tail gas generated by melamine is transported to the condensation chamber of first ammonium maker bottom, the heat exchanger place carries out condensation and absorbs in condensation chamber, forms the first ammonium salt solution;
(2), unabsorbed tail gas rises and enters the washing cavities on first ammonium maker top in the condensation chamber, wash absorption, form the first ammonium salt solution with the cleaning solution of washing cavities upper spray pipe ejection;
(3), the first ammonium salt solution that produces in above-mentioned two step process is discharged and is stored through first ammonium maker bottom first ammonium liquid carrier pipe;
(4), unabsorbed tail gas is discharged by first ammonium maker top vent in the washing cavities, enters tail gas condenser, the cleaning solution with the ejection of tail gas condenser internal sparger pipe in tail gas condenser washs absorption;
(5), the survival gas after absorbing through condensation in the tail gas condenser is discharged into the normal pressure absorption tower, the cleaning solution with the ejection of normal pressure absorption tower internal sparger pipe in the normal pressure absorption tower washs absorption;
(6), absorbing the back survival gas through washing in the normal pressure absorption tower is discharged in the atmosphere.
2. melamine tail gas treatment process according to claim 1, it is characterized in that: part first ammonium liquid enters the circulation fluid pipe through first ammonium carrier pipe, enter the air inlet pipe and the condensation chamber middle and upper part of first ammonium maker again through the circulation fluid pipe, this part first ammonium liquid enters behind the condensation chamber wherein gas and liquid stir.
3. melamine tail gas treatment process according to claim 1 and 2, it is characterized in that: the liquid that produces in the tail gas condenser is transported to the cleaning solution cooler through the cleaning solution carrier pipe of tail gas condenser bottom, this liquid cools off in the cleaning solution cooler, form cleaning solution, cleaning solution enters the shower of the washing cavities on first ammonium maker top, is absorbed by shower ejection and the capable washing of washing intracavity gas.
4. melamine tail gas treatment process according to claim 3, it is characterized in that: part cleaning solution and first ammonium liquid are collected through the liquid collecting cavity of washing cavities bottom in the washing cavities, flow into the cleaning solution cooler by circulation pipe then, this liquid cools off in the cleaning solution cooler, form cleaning solution, this cleaning solution enters the shower of the washing cavities on first ammonium maker top, is absorbed by shower ejection and the capable washing of washing intracavity gas.
5. the melamine tail gas treatment facility that uses according to each described melamine tail gas treatment process of claim 1-4, it is characterized in that: comprise first ammonium maker (22), first ammonium maker (22) bottom is condensation chamber (6), top is washing cavities (10), washing cavities (10) communicates with condensation chamber (6), be installed into tracheae (3) and first ammonium liquid carrier pipe (17) on the outer wall of condensation chamber (6) bottom, first ammonium liquid carrier pipe (17) apart from the distance of first ammonium maker (22) bottom surface less than the distance of air inlet pipe (3) apart from first ammonium maker (22) bottom surface, the interior mounting heat exchanger of condensation chamber (6), packing layer (9) is installed in the interior bottom of washing cavities (10), shower (13) is installed on washing cavities (10) top, washing cavities (10) top is provided with exhaust outlet (12), exhaust outlet (12) is communicated with tail gas condenser (24) air inlet by pipeline, tail gas condenser (24) upper air vent is communicated with normal pressure absorption tower (26) air inlet by pipeline, and normal pressure absorption tower (26) exhaust outlet communicates with atmosphere.
6. melamine tail gas treatment facility according to claim 5, it is characterized in that: heat exchanger is made up of many " U " type heat exchanger tubes (16), first ammonium maker (22) bottom is provided with intake antrum (2) and water chamber (18), intake antrum (2) is communicated with cooling water inlet pipe (1) and " U " type heat exchanger tube (16) water inlet respectively, and water chamber (18) is communicated with cooling water outlet pipe (19) and " U " type heat exchanger tube (16) delivery port respectively.
7. melamine tail gas treatment facility according to claim 5 is characterized in that: on condensation chamber (6) outer wall middle and upper part and the air inlet pipe (3) circulation fluid pipe (15) is installed respectively, circulation fluid pipe (15) is communicated with first ammonium liquid carrier pipe (17).
8. according to claim 5,6 or 7 each described melamine tail gas treatment facilities, it is characterized in that: install on the outer wall of condensation chamber (6) bottom and divide air cavity (4), divide air cavity (4) to go up tail gas import (3) is installed, offer some air inlets (5) on the outer wall of condensation chamber (6) bottom with on the corresponding position of a minute air cavity (4).
9. according to claim 5,6 or 7 each described melamine tail gas treatment facilities, it is characterized in that: cleaning solution carrier pipe (31) is installed in tail gas condenser (24) bottom, cleaning solution carrier pipe (31) is connected with cleaning solution cooler (23), cleaning solution cooler (23) is communicated with shower (13), liquid collecting cavity (20) is installed around the interior bottom of washing cavities (10), cleaning solution drain pipe (14) is installed on the outer wall of washing cavities (10) bottom, and cleaning solution drain pipe (14) is respectively at being communicated with liquid collecting cavity (20) and cleaning solution cooler (23).
10. melamine tail gas treatment facility according to claim 8, it is characterized in that: cleaning solution carrier pipe (31) is installed in tail gas condenser (24) bottom, cleaning solution carrier pipe (31) is connected with cleaning solution cooler (23), cleaning solution cooler (23) is communicated with shower (13), liquid collecting cavity (20) is installed around the interior bottom of washing cavities (10), cleaning solution drain pipe (14) is installed on the outer wall of washing cavities (10) bottom, and cleaning solution drain pipe (14) is respectively at being communicated with liquid collecting cavity (20) and cleaning solution cooler (23).
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| CN2009100172420A CN101607168B (en) | 2009-07-17 | 2009-07-17 | Process and equipment for treating melamine tail gas |
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| CN2009100172420A CN101607168B (en) | 2009-07-17 | 2009-07-17 | Process and equipment for treating melamine tail gas |
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| CN101607168B true CN101607168B (en) | 2011-05-04 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101838246B (en) * | 2010-04-29 | 2012-04-18 | 聊城市鲁西化工工程设计有限责任公司 | Counterblow technique utilizing melamine tail gas and equipment |
| CN102603661B (en) * | 2012-03-12 | 2014-10-22 | 李靖铭 | Process of using medium-pressure gas-phase quenching method to produce melamine |
| CN106167470A (en) * | 2016-07-26 | 2016-11-30 | 湖北宜化集团有限责任公司 | A kind of tripolycyanamide of holding successfully reclaims the system and method for urea plant |
| CN106349117B (en) * | 2016-08-27 | 2018-10-12 | 湖北宜化集团有限责任公司 | A kind of processing method of melamine tail gas |
| CN108299243A (en) * | 2018-05-04 | 2018-07-20 | 山东鸿运工程设计有限公司 | A kind of carbamide production system and method for absorbing melamine tail gas |
| CN110041230B (en) * | 2019-04-30 | 2021-10-15 | 中国五环工程有限公司 | Process for producing urea by stripping method for recovering tail gas of melamine device |
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| CN1234022A (en) * | 1996-08-30 | 1999-11-03 | Dsm有限公司 | Process for prepn. of urea |
| US6344588B1 (en) * | 1996-08-30 | 2002-02-05 | Dsm, N.V. | Process for the preparation of urea |
| CN1746154A (en) * | 2004-09-09 | 2006-03-15 | 乌里阿·卡萨勒有限公司 | Integrated process for urea/melamine production and related plant |
| EP1752447A1 (en) * | 2005-08-10 | 2007-02-14 | Urea Casale S.A. | process for the integrated production of urea and melamine |
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2009
- 2009-07-17 CN CN2009100172420A patent/CN101607168B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1234022A (en) * | 1996-08-30 | 1999-11-03 | Dsm有限公司 | Process for prepn. of urea |
| US6344588B1 (en) * | 1996-08-30 | 2002-02-05 | Dsm, N.V. | Process for the preparation of urea |
| CN1746154A (en) * | 2004-09-09 | 2006-03-15 | 乌里阿·卡萨勒有限公司 | Integrated process for urea/melamine production and related plant |
| EP1752447A1 (en) * | 2005-08-10 | 2007-02-14 | Urea Casale S.A. | process for the integrated production of urea and melamine |
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