CN101837963B - Stepped utilization method of steam in ammonium phosphate production - Google Patents
Stepped utilization method of steam in ammonium phosphate production Download PDFInfo
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- CN101837963B CN101837963B CN2009101029148A CN200910102914A CN101837963B CN 101837963 B CN101837963 B CN 101837963B CN 2009101029148 A CN2009101029148 A CN 2009101029148A CN 200910102914 A CN200910102914 A CN 200910102914A CN 101837963 B CN101837963 B CN 101837963B
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a stepped utilization method of steam in ammonium phosphate production, which comprises the following steps: 1. three-time steam generated by two-stage concentration is introduced into a heat exchanger to heat and pre-concentrate raw material of thin phosphoric acid, and after heating, the steam at the terminal is discharged and condensed, the temperature of which is lowered; and 2. part reaction heat generated by neutralization of raw material of the phosphoric acid and ammonia is still used for secondarily concentrating ammonium phosphate slurry, and the other part of the steam continues to heat the raw material of the phosphoric acid by single-pass falling film evaporation so as to further pre-concentrate the phosphoric acid. The method has the advantages that: (1) by lowering the vaporization temperature at the terminal to 50DEG C-60DEG C, low-temperature pre-concentration of the phosphoric acid is realized, which saves the consumption of primary steam and reduces the emission of waste heat and gas; (2) auxiliary equipment runs steadily, forced circulation has high evaporation intensity, circulating power consumption is reduced, and the size of the equipment and pipelines is reduced; (3) the operation temperature is obviously reduced, and the corrosion and scaling on a heating surface caused by a concentrated medium are improved; and (4) the concentration operation expands towards a low-temperature area, thus improving the functions of the equipment.
Description
Technical field
The present invention relates to ammonium phosphate salt, also relate to steam-heated heat energy utilization.
Background technology
As everyone knows, solid phosphoric acid ammonium (hereinafter to be referred as the phosphorus ammonium) mainly contains " Phosphoric Acid Concentration method (traditional method) " and " in and slurry concentrated process " two kinds of production technique at present.
The phosphorus ammonium is typical resource-intensive product, except phosphorus, sulphur mineral raw material consume and, a large amount of heat energy consumptions are in courses of processing such as evaporation concentration and dryings.Domestic and international various phosphorus ammonium technology all is that to rely on outer energy supply source be main " sectional " dewatering process flow, that is: 1. low pressure is given birth to steam and concentrated dilute phosphoric acid, and during 2. phosphorus ammonium reaction heat concentrates and slip, 3. the phosphor ammonium slurry hot-air dry dewaters.Present every 1t ammonium phosphate product heat dissipation ability 3.4GJ, electric energy 65kW.h enter atmosphere with waste gas after the disposable use of great amount of heat energy.In existing and in the slurry concentrated process technology; Giving birth to steam is used for phosphor ammonium slurry is carried out once concentration; The secondary steam that produces in concentrating is used for phosphor ammonium slurry is carried out secondary concentration; 80 ℃～90 ℃ the end that produces in concentrating is imitated steam and is entered atmosphere, and its low level heat energy does not obtain transforming and utilizes, and causes the waste of the energy.
At present, the patented claim part of steam utilization during still without phosphorus ammonium is produced.
Summary of the invention
The object of the present invention is to provide a kind of " in and slurry concentrated process " system phosphorus ammonium produce in the cascade utilization method of steam, more can utilize reaction heat and the Lowlevel thermal energy that adds steam fully, realize the energy-saving and emission-reduction that the phosphorus ammonium is produced.
The inventive method is to be based upon on the basis of thermodynamic optimization and process intensification, is utilized in a large amount of reaction heat that discharge in the chemical process of raw material phosphoric acid and ammonia react and secondary and concentrates the Lowlevel thermal energy that three steam producing bring.Comprise:
1. secondary is concentrated three steam that produce and introduce interchanger to raw material dilute phosphoric acid heating pre-concentration, the terminal steam that temperature after heating reduces is discharged, condensation;
2. still be used for phosphor ammonium slurry is carried out secondary concentration with the thermogenetic part of reaction that discharges in raw material phosphoric acid and the ammonia, another part steam continues heating raw phosphoric acid through the one way falling film evaporation, makes it further pre-concentration.
In the aforesaid method, the temperature of said three steam is 80 ℃～90 ℃, and described terminal vapor temperature is 50 ℃～60 ℃, absolute pressure 10～20kPa.
In the aforesaid method, in phosphoric acid and the ammonia with about 120 ℃ of the thermogenetic vapor temperature of reaction that discharges.
Compare with traditional technology; Present method has following advantage: (1) is reduced to 50～60 ℃ with terminal vaporization temperature from 80～90 ℃, realizes phosphoric acid low temperature pre-concentration, promptly utilizes the tail gas Lowlevel thermal energy to accomplish the pre-concentration task more than 30%; Practice thrift primary steam consumption, reduce the used heat exhaust gas emission simultaneously.(2) pump circulation of recovery waste heat and one way falling liquid film low temperature phosphoric acid pre-concentration technology and relevant equipment are stable, and the forced circulation evaporation intensity of calculating by heat transfer area reaches 29kg/h.m
2, circulation power consumption rate conventional art reduces by 50%, and equipment and line size are corresponding dwindles; One way falling film evaporation intensity reaches 20kg/h.m
2, do not need circulation power equipment.(3) service temperature reduces than traditional Phosphoric Acid Concentration Faxian work, and reaction has improved corrosion and the fouling of concentrated medium to hot face with the coupling of concentration process, and the hot face material is used the 316L stainless steel, do not have obviously corrosion, and scale formation slows down.(4) concentration operation is expanded to cold zone, has improved the original device function.
Description of drawings
Fig. 1 is in having now and the slurry concentrated process process flow diagram, and Fig. 2 is the process flow diagram of the inventive method.
Embodiment
Urn good fortune phosphate fertilizer plant of embodiment Wengfu Group Co., Ltd. 2005 adopts that should technology 240kt/a " in and slurry concentrated process " powdery monoammonium phosphate (being abbreviated as MAP) device be expanded can the consumption-reducing technological transformation, drops in July, 2006 and trys out.Realized that successfully the recovery slip concentrates the low temperature phosphoric acid pre-concentration MAP energy-saving technique of tail gas (about 80 ℃) waste heat, comprehensive energy consumption reduces by 39% on year-on-year basis, and makes original device slip throughput bring up to 360kt/a (original design 240kt/a Powder MAP) ability.Running condition after the employing low temperature phosphoric acid pre-concentration power saving function technology is following:
Visible by data in the table, through the peroxophosphoric acid pre-concentration, phosphoric acid P
2O
5Content raising value minimum is 3.12%, and peak is 5.89%.Phosphoric acid behind the use pre-concentration and ammonia neutralization, the phosphor ammonium slurry water cut that obtains will reduce, and the steam consumption when the minimizing phosphor ammonium slurry concentrates reaches energy-saving effect.Through calculating P in phosphoric acid
2O
5Content brings up to 27% by 23%, and under device full load (48t/h) running condition, the saving quantity of steam is 17.56t/h, the energy-conservation 0.3658t steam of promptly every 1t product, annual energy efficient signature coal 10536t.
Claims (3)
1. the cascade utilization method of steam during ammonium phosphate is produced, its characteristic comprises:
1. secondary is concentrated three steam that produce and introduce interchanger to raw material dilute phosphoric acid heating pre-concentration, the terminal steam that temperature after heating reduces is discharged, condensation;
2. still be used for phosphor ammonium slurry is carried out secondary concentration with the thermogenetic part of reaction that discharges in raw material phosphoric acid and the ammonia, another part steam continues heating raw phosphoric acid through the one way falling film evaporation, makes it further pre-concentration;
Said steam is the steam that produces during " in and slurry concentrated process " system ammonium phosphate is produced.
2. the method for claim 1, the temperature that it is characterized in that said three steam is 80 ℃～90 ℃, described terminal vapor temperature is 50 ℃～60 ℃, absolute pressure 10～20kPa.
3. the method for claim 1 is characterized in that in said phosphoric acid and the ammonia and 120 ℃ of the thermogenetic vapor temperatures of reaction that discharges.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101029148A CN101837963B (en) | 2009-12-01 | 2009-12-01 | Stepped utilization method of steam in ammonium phosphate production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2009101029148A CN101837963B (en) | 2009-12-01 | 2009-12-01 | Stepped utilization method of steam in ammonium phosphate production |
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| Publication Number | Publication Date |
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| CN101837963A CN101837963A (en) | 2010-09-22 |
| CN101837963B true CN101837963B (en) | 2012-01-25 |
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| CN2009101029148A Active CN101837963B (en) | 2009-12-01 | 2009-12-01 | Stepped utilization method of steam in ammonium phosphate production |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102430250A (en) * | 2010-09-29 | 2012-05-02 | 江苏乐科热工程设备有限公司 | Evaporation and concentration method for corrosive liquid material |
| CN102277633B (en) * | 2011-07-07 | 2013-01-02 | 唐山三友集团兴达化纤有限公司 | Method for achieving cascade utilization of steam in viscose staple fiber production process |
| CN102515923B (en) * | 2011-12-28 | 2013-09-25 | 四川宏达股份有限公司 | Drip irrigation-grade ammonium phosphate sulfate composite fertilizer and preparation process thereof |
| CN113262624B (en) * | 2021-05-20 | 2023-03-24 | 四川金象赛瑞化工股份有限公司 | Pressurization neutralization method for treating melamine tail gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3005696A (en) * | 1957-12-06 | 1961-10-24 | Tennessee Valley Authority | Process for production of ammonium phosphate fertilizers |
| CN1033261A (en) * | 1987-11-25 | 1989-06-07 | 沈阳化工综合利用研究所 | A kind of method of producing ammonium phosphate |
| CN1064858A (en) * | 1992-04-11 | 1992-09-30 | 四川省德阳市什邡化肥总厂 | With phosphoric acid by wet process coproduction fertilizer grade and pure phosphoric acid one ammonium |
| CN101343051A (en) * | 2008-09-02 | 2009-01-14 | 武汉凌派化工科技有限公司 | Method for decomposing phosphorus ore and phosphorus ore containing article with hydrochloric acid to produce phosphoric acid and ammonium phosphate salt |
-
2009
- 2009-12-01 CN CN2009101029148A patent/CN101837963B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3005696A (en) * | 1957-12-06 | 1961-10-24 | Tennessee Valley Authority | Process for production of ammonium phosphate fertilizers |
| CN1033261A (en) * | 1987-11-25 | 1989-06-07 | 沈阳化工综合利用研究所 | A kind of method of producing ammonium phosphate |
| CN1064858A (en) * | 1992-04-11 | 1992-09-30 | 四川省德阳市什邡化肥总厂 | With phosphoric acid by wet process coproduction fertilizer grade and pure phosphoric acid one ammonium |
| CN101343051A (en) * | 2008-09-02 | 2009-01-14 | 武汉凌派化工科技有限公司 | Method for decomposing phosphorus ore and phosphorus ore containing article with hydrochloric acid to produce phosphoric acid and ammonium phosphate salt |
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| CN101837963A (en) | 2010-09-22 |
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Address after: 550500 Guizhou Province, Qiannan Buyei and Miao Autonomous Prefecture Fuquan Racecourse town Yingbin Road No. 1 Wengfu group Patentee after: WENGFU GROUP Co.,Ltd. Address before: 23, 550002 floor, International Building, No. 57, South City Road, Nanming District, Guiyang, Guizhou Patentee before: WENGFU GROUP Co.,Ltd. |