CN1608978A - Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization - Google Patents
Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization Download PDFInfo
- Publication number
- CN1608978A CN1608978A CN 200310110769 CN200310110769A CN1608978A CN 1608978 A CN1608978 A CN 1608978A CN 200310110769 CN200310110769 CN 200310110769 CN 200310110769 A CN200310110769 A CN 200310110769A CN 1608978 A CN1608978 A CN 1608978A
- Authority
- CN
- China
- Prior art keywords
- waste gas
- gas
- phosphoric acid
- ammonia
- flash
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
The present invention is the method of reusing industrial waste gas from ammonium phosphate and diammonium phosphate production and reducing exhaust. The heat in waste gas from final evaporator, pre-neutralizing reactor and pelletizer is utilized in heating dilute phosphoric acid or its neutralized solution with ammonia gas to make the dilute solution flash evaporate to concentrate at 58-65 deg.c, and utilizing the vapor at 52-61 deg.c in gasifying liquid ammonia at 5 deg.c for neutralizing. All the heat and mass transferring processes from the waste gas heat source at 75-85 deg.c to the low temperature cold source at 5 deg.c are wattful process without wattless consumption. The present invention his high resource utilization and high environment protection index.
Description
Technical field the present invention relates to a kind ofly make the utilization process of the industrial gaseous waste of monoammonium phosphate and diammonium phosphate by phosphoric acid by wet process and ammonia, can reduce product processing exhaust gas discharged amount, reduces the steam consumption of process simultaneously.Present method be applicable to adopt Phosphoric Acid Concentration or in and slip concentrate the factory that produces monoammonium phosphate or diammonium phosphate, need to use the occasion of gas ammonia neutralising phosphoric acid and enriching slurry, be particularly useful for diammonium phosphate/monoammonium phosphate joint process.
The existing industrial technology of background technology from phosphoric acid by wet process and ammonia manufacturing monoammonium phosphate and diammonium phosphate; by reactor, tablets press, in and slip concentrate equipment such as last evaporator to produce temperature be waste gas about 75～85 ℃, wherein contain a certain amount of water vapor.Prior art be make waste gas by chimney more than a certain height to airborne release, perhaps adopt recirculated cooling water to make wherein water vapor condensation discharging.A MAP Plant or a diammonium phosphate device of producing 600000 tons per year of producing 240000 tons per year, the water vapor amount about 75～85 ℃ of per hour discharging has been brought two aspect disadvantageous effects of resource and environment all more than 20 tons.And from the arts demand that phosphoric acid by wet process and ammonia are made monoammonium phosphate and diammonium phosphate use water vapor concentrate dilute phosphoric acid and and slip, also need to use the thermal source liquid ammonia that under 5 ℃ or lower temperature, gasifies.
Summary of the invention the present invention discloses a kind of by the recycle method of making the industrial gaseous waste of monoammonium phosphate and diammonium phosphate in the gas ammonia with phosphoric acid by wet process.Present method utilize 75～85 ℃ phosphoric acid pre-neutralization reactor exhaust, tablets press waste gas and in and slip concentrate last evaporator waste gas and be thermal source, high moisture content character according to waste gas, under being lower than the temperature of dew point, mainly utilize its heat of condensation heat dilute phosphoric acid or in and slip to 58～65 ℃, and flash distillation under the pressure about 9～15kPa (cutting off); 52～61 ℃ flash steam is utilized for 5 ℃ or low temperature liquefied ammonia gasification institute heat requirement down more again, thus realized utilizing waste gas thermal source pre-concentration dilute phosphoric acid or in and slip, carry out two of liquefied ammonia gasification simultaneously and imitate and process.The liquefied ammonia gasification makes 52～61 ℃ flash steam condensation easily as low temperature cold source, help to reduce flashing pressure, strengthen dilute phosphoric acid or in and slip pre-concentration process.And saved the required water coolant of common last evaporator exhaust steam condensation.
Main invention thought of the present invention is according to the second law of thermodynamics, between the liquefied ammonia gasification low temperature cold source of 75～85 ℃ waste gas thermals source and 5 ℃, insert one dexterously and can be lower than the dilute solution flash concentration process that 10～15 ℃ are carried out below the waste gas dew-point temperature, thereby flash steam is easy to be helped creating the required condition of vacuum flashing by the condensation of liquefied ammonia gasification heat dissipation institute, and rearmounted vacuum system only need be taken non-condensable gas away.From between the low temperature cold source of 75～85 ℃ waste gas thermals source to 5 ℃ all heat and mass transfer processes all are meritorious processes, avoided the reactive power consumption of common vacuum-evaporation secondary steam condensation.
Compare with the existing technology of handling monoammonium phosphate and diammonium phosphate industrial gaseous waste; present method difference is at least; utilize the slip of 75～85 ℃ high moisture content to concentrate last evaporator waste gas, pre-neutralization reactor exhaust and tablets press waste gas thermal source; the neutralization solution of heating dilute phosphoric acid or itself and gas ammonia under the temperature that is lower than the waste gas dew point; and the liquefied ammonia gasification that makes dilute solution flash concentration under 58～65 ℃ temperature, 52～61 ℃ flash steam be used further to 5 ℃ supplies neutralization reaction required.From between the low temperature cold source of 75～85 ℃ waste gas thermals source to 5 ℃ all heat and mass transfer processes all are meritorious processes, avoided the reactive power consumption of common vacuum-evaporation secondary steam condensation.
With a MAP Plant or a diammonium phosphate device of producing 600000 tons per year of producing 240000 tons per year is example, adopt present method per hour to reduce water vapor quantity discharged in the waste gas more than at least 15 tons, reduce and give birth to steam consumption more than at least 18 tons, and need not to consume recirculated cooling water.The resource utilization and the environment protection index of production process are improved significantly.
Shown in the appended drawings 1, be by spent air heat exchanger 1, dilute solution flasher 2, recycle pump 3, mist eliminator 4 and liquefied ammonia vaporizer 5 for major equipment constitutes pump circulation heating flash evaporation flow process of the present invention, further specify below with reference to specific embodiment 1.Shown in the accompanying drawing 2, be by waste gas heat exchange falling liquid film flasher 1, mist eliminator 2 and liquefied ammonia vaporizer 3 for major equipment constitutes one way falling film heating flash distillation flow process of the present invention, further specify below with reference to specific embodiment 2.
Embodiment embodiment 1 is the embodiment of 1 explanation pump circulation heating flash evaporation flow process of the present invention in conjunction with the accompanying drawings
Production equipment: produce 600000 tons of diammonium phosphate/240,000 ton monoammonium phosphate combination preparing device per year
Exhaust gas parameters: the diammonium phosphate pre-neutralization reactor exhaust behind chemical washing and the gas mixture of tablets press waste gas (hereinafter to be referred as " two ammonium waste gas "), about 80 ℃ of temperature, about 22 tons/hour of vapour content
Adopt phosphorus ammonium plant gas two of the present invention shown in the accompanying drawing 1 to imitate the pump circulation heating flash evaporation flow process of utilizing the pre-concentration dilute phosphoric acid and the liquefied ammonia that gasifies, make " the two ammonium waste gas " dilute phosphoric acid solution of heating cycle in spent air heat exchanger 1 about 80 ℃, the waste gas cooling condensation is cooled to discharge system behind about 18 tons/hour of 68 ℃, water vapor decrement.Dilute solution by recycle pump 3 pump circulation is replenished 25～28P
2O
568 tons/hour of % dilute phosphoric acids enter flasher 2 be heated to 58 ℃ in spent air heat exchanger 1 after, and evaporation concentration is to P under 10kPa (cutting off) pressure
2O
5Content about 29～33% is sent to subsequent handling and continues processing.By about 16～17 tons/hour of about 52 ℃ flash steam of flasher 2, enter ammonia evaporator 5 after in mist eliminator 4, separating entrainment, heating liquefied ammonia makes its evaporation under the heat transfer temperature difference about 40 ℃, the about 500kPa of gas ammonia pressure (cutting off) that produces can satisfy 600,000 tons of diammonium phosphate of annual output and 240,000 tons of monoammonium phosphate combination preparing device processing requirements simultaneously as raw material.Non-condensable gas and uncooled steam are taken away by vacuum system in the lump.
Embodiment 2 is the embodiment of 2 explanations one way falling film heating flash distillation flow process of the present invention in conjunction with the accompanying drawings
Production equipment: produce 60000 tons of MAP Plant per year
Exhaust gas parameters: slip concentrates last evaporator combustion gas (hereinafter to be referred as " an ammonium waste gas "), about 85 ℃ of temperature, about 6 tons/hour of water vapor amount
Adopt phosphorus ammonium plant gas two of the present invention shown in the accompanying drawing 2 to imitate the one way falling film heating flash distillation flow process of utilizing the pre-concentration dilute phosphoric acid and the liquefied ammonia that gasifies, " an ammonium waste gas " about 85 ℃ is heated along inside pipe wall falling liquid film mobile dilute phosphoric acid solution at waste gas heat exchange falling liquid film flasher 1 midfeather, the waste gas cooling condensation does not coagulate gas on a small quantity and is discharged to vacuum system.About 18 tons of/hour 22～25P
2O
5When the dilute phosphoric acid solution of % content is heated to about 62 ℃ in waste gas heat exchange falling liquid film flasher 1 under the pressure of 15kPa (cutting off) left and right sides evaporation concentration to P
2O
5Content about 29～33% is sent to subsequent handling and continues processing.By about 4～6 tons/hour of about 56 ℃ flash steam of waste gas heat exchange falling liquid film flasher 1, enter liquefied ammonia vaporizer 3 after in mist eliminator 2, separating entrainment, heating liquefied ammonia makes its evaporation under the heat transfer temperature difference about 44 ℃, the about 550kPa of gas ammonia pressure (cutting off) that produces can satisfy 60,000 tons of MAP Plant processing requirements of annual output as raw material.Non-condensable gas and uncooled steam are taken away by vacuum system in the lump.
Claims (1)
- A kind of by in the gas ammonia and phosphoric acid by wet process make the industrial gaseous waste recycle of monoammonium phosphate and diammonium phosphate and reduce the method for discharge amount of exhaust gas and implement the pump circulation heating flash evaporation flow process and the one way falling film heating flash distillation flow process of this method.It is characterized in that utilizing the slip of 75～85 ℃ high moisture content to concentrate last evaporator waste gas, pre-neutralization reactor exhaust and tablets press waste gas thermal source; the neutralization solution of heating dilute phosphoric acid or itself and gas ammonia under the temperature that is lower than the waste gas dew point; and making it flash concentration under 58～65 ℃ temperature, it is required for neutralization reaction that 52～61 ℃ flash steam is used further to 5 ℃ liquefied ammonia gasification.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101107690A CN1309658C (en) | 2003-10-24 | 2003-10-24 | Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101107690A CN1309658C (en) | 2003-10-24 | 2003-10-24 | Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1608978A true CN1608978A (en) | 2005-04-27 |
| CN1309658C CN1309658C (en) | 2007-04-11 |
Family
ID=34759228
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2003101107690A Expired - Fee Related CN1309658C (en) | 2003-10-24 | 2003-10-24 | Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1309658C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100396601C (en) * | 2006-10-09 | 2008-06-25 | 四川大学 | Ammonium phosphate preparation method without tail gas |
| CN103663398A (en) * | 2013-11-29 | 2014-03-26 | 安徽六国化工股份有限公司 | Method and device for utilizing heat energy of diammonium phosphate neutralization tail gas |
| CN108926962A (en) * | 2018-08-10 | 2018-12-04 | 重庆天原化工有限公司 | Ammonia-containing exhaust recovery and treatment method |
| CN114715865A (en) * | 2022-03-17 | 2022-07-08 | 四川龙蟒磷化工有限公司 | Production method of industrial grade diammonium hydrogen phosphate |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1042216C (en) * | 1992-07-17 | 1999-02-24 | 莱西市磷肥厂 | Enriching slurry process for production of diammonium phosphate |
| CN1235794C (en) * | 2002-03-06 | 2006-01-11 | 四川大学 | Coproduction method of diammonium phosphate and monoammonium phosphate and equipment for neutralizing washing liquid |
-
2003
- 2003-10-24 CN CNB2003101107690A patent/CN1309658C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100396601C (en) * | 2006-10-09 | 2008-06-25 | 四川大学 | Ammonium phosphate preparation method without tail gas |
| CN103663398A (en) * | 2013-11-29 | 2014-03-26 | 安徽六国化工股份有限公司 | Method and device for utilizing heat energy of diammonium phosphate neutralization tail gas |
| CN103663398B (en) * | 2013-11-29 | 2015-07-15 | 安徽六国化工股份有限公司 | Method and device for utilizing heat energy of diammonium phosphate neutralization tail gas |
| CN108926962A (en) * | 2018-08-10 | 2018-12-04 | 重庆天原化工有限公司 | Ammonia-containing exhaust recovery and treatment method |
| CN114715865A (en) * | 2022-03-17 | 2022-07-08 | 四川龙蟒磷化工有限公司 | Production method of industrial grade diammonium hydrogen phosphate |
| CN114715865B (en) * | 2022-03-17 | 2023-08-29 | 四川龙蟒磷化工有限公司 | Production method of industrial-grade diammonium hydrogen phosphate |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1309658C (en) | 2007-04-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102616973B (en) | Method and device for processing high-saline organic wastewater | |
| CN100480176C (en) | Wet-process two-stage phosphoric acid concentration method | |
| CN100595136C (en) | Method for producing feed-grade calcium phosphate | |
| CN101704539B (en) | Method and device for evaporating mother liquid in aluminium oxide plant | |
| CN105502307B (en) | The method and special purpose device of waste acid concentration defluorinating chlorine | |
| CN107029446A (en) | Double caloics couple solution condensing crystallizing system and method | |
| CN106829899B (en) | The Wet Processes of Phosphoric Acid and fluosilicic acid processing method of no fluorinated tail gas discharge | |
| CN1309658C (en) | Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization | |
| CN1306942A (en) | Method and apparatus for preparing fresh water from sea water | |
| CN101357755B (en) | Production process of potassium dihydrogen phosphate | |
| CN101837963B (en) | Stepped utilization method of steam in ammonium phosphate production | |
| CN102249474A (en) | Treatment method for thiamine waste water produced in production process of phosethyl-Al bulk chemical | |
| CN1125773C (en) | Production method of feed-level calcium hydrogen phosphate | |
| CN100396601C (en) | Ammonium phosphate preparation method without tail gas | |
| CN106967114B (en) | Recycling comprehensive treatment method and system for fosetyl-aluminum wastewater | |
| CN109205901A (en) | The device and method of agricultural calcium nitrate is produced using dense nitration mixture waste water | |
| CN102167301B (en) | Production method for co-production of high-water-solubility feed grade calcium phosphate and purified phosphoric acid | |
| CN106871468A (en) | Gas alternating temperature transformation reclaims low level used heat and the round-robin method for utilizing that heats up | |
| CN206915766U (en) | A kind of medium temperature carbonizatin method handles the device of high COD sulfuric acid | |
| CN220034363U (en) | Liquid ammonium polyphosphate fertilizer apparatus for producing | |
| CN110294503A (en) | The processing system of air compression-expansion circulating and evaporating separation electroplating wastewater | |
| CN101288440B (en) | Production method of feed grade calcium phosphate acidity agent | |
| CN214344476U (en) | MVR evaporation concentration equipment used in potassium chloride evaporation industry | |
| CN104478514B (en) | A kind of utilization gas cleaning accessory substance prepares the thermo-compression evaporation technique of chemical fertilizer | |
| CN102491295A (en) | Method for producing monoammonium phosphate by utilizing sludge acid as raw material through slurry concentration process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| 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: 20070411 Termination date: 20091124 |