CN101177251A - Method for producing technical grade ribose phosphate, food grade ribose phosphate and industry ammonium diacid phosphate using wet-process ribose phosphate - Google Patents
Method for producing technical grade ribose phosphate, food grade ribose phosphate and industry ammonium diacid phosphate using wet-process ribose phosphate Download PDFInfo
- Publication number
- CN101177251A CN101177251A CNA2007100929041A CN200710092904A CN101177251A CN 101177251 A CN101177251 A CN 101177251A CN A2007100929041 A CNA2007100929041 A CN A2007100929041A CN 200710092904 A CN200710092904 A CN 200710092904A CN 101177251 A CN101177251 A CN 101177251A
- Authority
- CN
- China
- Prior art keywords
- phosphoric acid
- grade
- extraction
- phosphate
- agent
- 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
Images
Abstract
The invention discloses a method of using wet phosphoric acid to prepare industrial grade phosphoric acid, food grade phosphoric acid and industrial ammonium diacid phosphate, which is characterized in using wet phosphoric acid as the material, and preparing industrial grade phosphoric acid and food grade phosphoric acid respectively by using a series of compound purifying technologies such as chemical sedimentation and extracting by organic solvent and concentration and recrystallization and other technologies; meanwhile, the invention uses a part of purified diluted phosphoric acid to prepare industrial ammonium diacid phosphate. The invention has the advantages of reasonable cascade utilization of the wet phosphoric acid, high additional value of phosphorus, and further exploitation of the lower industrial and food grades phosphate.
Description
Technical field
The invention belongs to phosphorus chemistry industry, specifically, be a kind of be raw material with the phosphoric acid by wet process, the method that adopt chemical precipitation, organic solvent extraction, concentrate, composite purification technology such as recrystallization prepares industrial monoammonium phosphate, PHOSPHORIC ACID TECH.GRADE and food grade phosphoric acid.
Background technology
Phosphorus chemistry industry (abbreviation phosphorous chemical industry) is to be that processing makes the industry of (mainly comprising element phosphor, phosphide, phosphoric acid and salt thereof, phosphoric acid ester, organophosphorus pesticide, phosphate fertilizer etc.) of various phosphorous goods to raw material through physical chemistry with the Rock Phosphate (72Min BPL).Since nearly half a century, owing to the widespread use of product in fields such as chemical industry, light industry, food, pharmacy, fire-fightings, phosphorous chemical industry has kept stable development.Because the specification of quality of fine phosphate adopts thermal phosphoric acid technology to satisfy its requirement for a long time.But variation along with the market requirement, and the restriction of factor such as resource, environment, the energy, phosphoric acid and inorganic phosphate production technology based on the wet phosphoric acid purifying technology replace traditional thermal phosphoric acid and phosphate production technical development very fast, become the focus of Modern Phosphating worker hi-tech development.
The operational path that with sulfuric acid is raw material is fundamental method in the Wet-process Phosphoric Acid Production.Phosphoric acid by wet process comes down to the nitration mixture of phosphoric acid, sulfuric acid and silicofluoric acid, contain plurality of impurities (as calcium, magnesium, fluorine, iron, aluminium, sulfate radical plasma), it is multiple fertile generally to be used to produce phosphorus, be used for process industry level, feed grade even food grade phosphoric acid product salt, must be with thick wet phosphoric acid purifying to remove impurity.At present, the purification of phosphoric acid by wet process mainly contains following several method: organic solvent extractionprocess; Ion exchange method; Ion exchange method and electroosmose process; Phosphoric Acid Concentration crystallization process or complex salt crystal method; Chemical precipitation method etc.
Organic solvent extractionprocess must adopt multi-stage solvent extraction, because therefore organic solvent high volatility, inflammable, explosive need take various security measuress; Organic solvent costs an arm and a leg, and the higher recovery system of yield etc. must be set, thereby increase the facility investment expense.In addition, negatively charged ion SO in the acid
4 2-, F
-, SiF
6 2-Remove Deng being difficult for; Gained purification of phosphoric acid concentration is lower; Generation contains residue (account for raw material 30%～50%) of a large amount of impurity etc.The advantage of this method is that phosphoric acid contacts with solvent and can be once removes various impurity in the disacidify, but and operate continuously, so be the main method of present wet phosphoric acid purifying.The development trend of this method is to develop into two-phase method by one-stage process; Develop into multiple solvent by single solvent.To the research of solvent itself, then more pay attention to the selectivity of phosphoric acid and impurity and at the partition ratio of solvent phase and aqueous phase.The phosphoric acid by wet process that solvent extration purifies can satisfy the requirement of PHOSPHORIC ACID TECH.GRADE or manufacturing feed-grade phosphate mostly, can reach the standard of food grade and even pharmaceutical grade after special the processing.The difference of various Technologies is that mainly solvent types is different with auxiliary treatment process.At present, solvent extration has become and has been used for one of most effectual way of refining phosphoric acid by wet process abroad.
Ion exchange method is because of can only making raw material with rarer phosphoric acid, thereby resin demand is big, and the acid of gained needs further to concentrate, and ion exchange resin need carry out manipulation of regeneration.
Recrystallization method is phosphoric acid by wet process to be concentrated or add other Synergist S-421 95s and phosphoric acid to form complex salt crystal, and after filtration, impurity is stayed in the aqueous solution and is removed.Because crystallization is carried secretly, this method is difficult to obtain highly purified acid, and the crystalline product yield is low, and concentration process easily causes corrosion to equipment and materials.
Chemical precipitation method can be removed partial cation or negatively charged ion, but it is not high to purify the degree of depth, and introduces another kind of ion again.Unless the compound solubility product that generates is very little, and can more fully remove foreign ion, as the sulfide of heavy metal, generally all need cooperate methods such as organic solvent extraction or ion exchange resin.
Single can not be comprehensively and the deeply purifying and removing decon with a kind of method, can not inside a technical process, obtain PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate simultaneously.
Summary of the invention
The invention provides a kind of low cost, high percentage extraction, high P
2O
5Utilization ratio makes the composite purification method of PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate simultaneously.
Technical scheme of the present invention is as follows: a kind ofly prepare the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process, it is characterized in that carrying out as follows:
Step 2, supernatant liquid in the clarifying tank enters the washing tower from the bottom inlet, washing tower middle and lower part inlet adds purifying phosphoric acid and the described supernatant liquid thorough mixing and the layering of 5～15 times of volumes of described supernatant liquid, lower floor extracting phase washing acid adds liquefied ammonia modulation degree of neutralization and is controlled to be 1.0～1.05 and reacts at neutralizing well, force the vacuum concentration system to concentrate with being pumped into, put into crystallisation by cooling groove growing the grain, stiff, obtain wet monoammonium phosphate through centrifugation, send into fluidizing fluid-bedly again with rotary conveyor, make high-quality crystalloid industrial monoammonium phosphate (total nutrient N+P with behind the hot-air dry
2O
5〉=72%), the mother liquor of centrifugation generation returns neutralizing well;
Step 3, described purifying phosphoric acid and described supernatant liquid thorough mixing and stratified upper organic phase, flow into washing organic phase groove from washing tower top, squeeze into back extraction tower middle and lower part inlet with pump, after adding the de-salted water thorough mixing and layering of 4～10 times of volumes of described upper organic phase from back extraction tower middle and upper part inlet simultaneously, extraction agent flows out from extraction tower top, recycles after the interchanger heat exchange, and the back extraction dilute phosphoric acid flows into the finished acid medial launder from the extraction tower bottom;
Step 4, the back extraction dilute phosphoric acid is sent into the abundant stirring reaction of sweetening agent of smart desulfurizer and 1.05～1.1 times of the energy neutralisation of sulphuric acid radical ions that adds simultaneously with pump, it is temporary to enter medial launder from the top overflow of smart desulfurizer, after with pump it being sent into the vertical type full automatic pressure filter filtration again, it is temporary that clear liquid enters medial launder, squeezes into pump and force the vacuum concentration system to concentrate and further obtain industrial phosphoric acid after the defluorinate (to contain P
2O
585%), again industrial phosphoric acid is carried out recrystallization and separate and to make food grade phosphoric acid;
In order to reach better effect, the barium carbonate of sweetening agent described in the step 1, ground phosphate rock or both mixing; Described defluorinating agent soda ash; Described regenerator caustic soda.The barium carbonate of sweetening agent described in the step 4.
Above-mentioned steps 1, step 2 adopts the multistage coupled wet phosphoric acid purifying of chemical precipitation, organic solvent extraction and recrystallization technology described in the step 3, step 4.The regeneration of extraction agent described in the step 3 and recycle, the online decolouring of the described charcoal non activated of step 1, described discoloring agent is a hydrogen peroxide, does not need special decoloring equipment.The sludge that vertical type full automatic pressure filter produces in the above-mentioned technology is with after raffinate mixes, with being pumped into composting system production fertilizer grade monoammonium phosphate.
Beneficial effect of the present invention is:
(1) realizes the combination of phosphoric acid purification and slag acid composting.In the production process of large phosphate fertilizer, extract part phosphoric acid production purifying phosphoric acid, raffinate that produces in the scavenging process and sludge are then delivered to the fertilizer device and are produced the fertilizer grade monoammonium phosphate.Raffinate is produced phosphate fertilizer and is not reduced its value, realizes the economic utilization of fertilizer-salt binding, the waste gas qualified discharge after administering that produces in the while production process, and waste water and waste residue produce all and fully utilize, and belong to environmentally friendly friendly process.
(2) realize PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate coproduction, made phosphoric acid by wet process obtain rational classification utilization, improved the added value of phosphorus, can further develop the technical grade and the food-grade phosphate in its downstream.
(3) directly utilize dilute phosphoric acid manufacture level phosphoric acid and food grade phosphoric acid ,-wet phosphoric acid purifying-reconcentration concentrated with the diluted acid of present concentrated acid purification techniques both domestic and external compared, cut down the consumption of energy greatly.Purifying technology has the ability that impurity level is big, class is many of removing.Multistage coupling separation technology successful Application in phosphoric acid purification has solved the task that traditional phosphoric acid impurity isolation technique is difficult to finish.
(4) adopt chemical precipitation method, solvent extration and recrystallization method process combined, realize having complementary advantages, improve project technico-economical comparison level, make Industry Promotion have better adaptive faculty and application prospect.Utilize the phosphoric acid extraction process of finding not to be subjected to the rule that influences of sulfate ion, optimize sweetening process, greatly simplify technical process.
(5) screen a kind of organic solvent (comprising thinner) that adapts to the extraction of wet method dilute phosphoric acid, and realized the regeneration and the recycle of extraction agent.
(6) adopt the charcoal non activated decoloring method.Colourity is an important indicator of industrial phosphoric acid, requires water white transparency or slightly yellow.Traditional extraction technology mostly adopts gac or hydrogen peroxide decolouring, and is equipped with special decoloring equipment.The present invention adds the charcoal non activated discoloring agent in extraction agent and thinner, can thoroughly remove the pigment in the phosphoric acid in extraction process, does not need special decolouring flow process and equipment, has shortened technical process, saves investment and running cost.
(7) in the defluorinate process, add the extractant regeneration agent, do not need special extractant regeneration equipment, shortened technical process, save investment and running cost, improved driving rate.Extraction agent in use can progressively wear out, so that finally loses the extraction function, must regenerate to extraction agent.Traditional extraction technology generally all is equipped with special extractant regeneration flow process and equipment.
(8) adopt the high-efficiency vertical full automatic pressure filter, intensity filter improves more than 6 times than conventional panels basket pressure filter.Conventional panels basket pressure filter throughput is low, level of automation is low, floor space is big, labour intensity is big.The vertical type full automatic pressure filter that the present invention adopts integrates filtration, extruding, washing, secondary extrusion, air-dry, slag dumping, adopts the PLC full automatic control, it is big to have throughput, filter residue liquid holdup low (below 1.6%), the self-cleaning regeneration of filter cloth, compact construction takes up an area of advantages such as few.
(9) in extraction procedure, add interchanger and remove the heat in the extraction agent after the back extraction, realize low-temperature extraction and high temperature back extraction, further improve percentage extraction, make back extraction more thorough.The phosphoric acid by wet process extraction is an exothermic process, and traditional extraction technology extracts high temperature, back extraction low temperature often, causes percentage extraction low.
Description of drawings
Fig. 1 is a process flow sheet of the present invention;
Embodiment
The invention will be further described below in conjunction with drawings and Examples:
As shown in Figure 1, the present invention is a kind of to prepare the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process, it is characterized in that carrying out as follows:
Step 2, supernatant liquid in the clarifying tank enters the washing tower from the bottom inlet, washing tower middle and lower part inlet adds purifying phosphoric acid and the described supernatant liquid thorough mixing and the layering of 10 times of volumes of described supernatant liquid, liquefied ammonia with 1.02 times of washing acids in lower floor's extracting phase washing acid adding energy reacts at neutralizing well, force the vacuum concentration system to concentrate with being pumped into, put into crystallisation by cooling groove growing the grain, stiff, obtain wet monoammonium phosphate through centrifugation, send into fluidizing fluid-bedly again with rotary conveyor, make high-quality crystalloid industrial monoammonium phosphate (total nutrient N+P with behind the hot-air dry
2O
5〉=72%), the mother liquor of centrifugation generation returns neutralizing well;
Step 3, described purifying phosphoric acid and described supernatant liquid thorough mixing and stratified upper organic phase, flow into washing organic phase groove from washing tower top, squeeze into back extraction tower middle and lower part inlet with pump, after adding the de-salted water thorough mixing and layering of 7 times of volumes of described upper organic phase from back extraction tower middle and upper part inlet simultaneously, extraction agent flows out from extraction tower top, recycles after the interchanger heat exchange, and the back extraction dilute phosphoric acid flows into the finished acid medial launder from the extraction tower bottom;
Step 4, with pump with the back extraction dilute phosphoric acid send into smart desulfurizer with add simultaneously can the neutralisation of sulphuric acid radical ion 1.05 times the abundant stirring reaction of sweetening agent barium carbonate, it is temporary to enter medial launder from the top overflow of smart desulfurizer, after with pump it being sent into the vertical type full automatic pressure filter filtration again, it is temporary that clear liquid enters medial launder, squeezes into pump and force the vacuum concentration system to concentrate and further obtain industrial phosphoric acid after the defluorinate (to contain P
2O
585%), again industrial phosphoric acid is carried out recrystallization and separate and to make food grade phosphoric acid;
The sludge that vertical type full automatic pressure filter produces in the above-mentioned technology is with after raffinate mixes, with being pumped into composting system production fertilizer grade monoammonium phosphate.
Claims (6)
1. one kind prepares the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process, it is characterized in that carrying out as follows:
Step 1, phosphoric acid by wet process is removed solid substance with being pumped into pressure filter, the clear liquid that obtains enters extraction tower top, the extraction tower bottom adds the extraction agent of 3～9 times of volumes of clear liquid simultaneously, described extraction agent is a tbp, thinner, discoloring agent, proportion relation is 2: 1: 0.00005, under 45～55 ℃, carry out hybrid extraction, form organic phase and extracting phase, organic phase enters desulfurization defluorinate groove and the sweetening agent that adds 1.05～1.1 times of energy neutralisation of sulphuric acid radical ion and fluorions, behind the abundant stirring reaction of defluorinating agent and regenerator, overflow enters clarifying tank and carries out sedimentation, layering, the bottom slurry is discharged after pressure filter filters, and filtrate is returned clarifying tank;
Step 2, supernatant liquid in the clarifying tank enters the washing tower from the bottom inlet, washing tower middle and lower part inlet adds purifying phosphoric acid and the described supernatant liquid thorough mixing and the layering of described supernatant liquid 5～1 5 times of volumes, lower floor's extracting phase washing acid adds in the energy and 1.0～1.05 times of liquefied ammonia of washing acid react at neutralizing well, force the vacuum concentration system to concentrate with being pumped into, put into crystallisation by cooling groove growing the grain, stiff, obtain wet monoammonium phosphate through centrifugation, send into fluidizing fluid-bed again with behind the hot-air dry with rotary conveyor, make high-quality crystalloid industrial monoammonium phosphate, the mother liquor that centrifugation produces returns neutralizing well;
Step 3, described purifying phosphoric acid and described supernatant liquid thorough mixing and stratified upper organic phase, flow into washing organic phase groove from washing tower top, squeeze into back extraction tower middle and lower part inlet with pump, after adding the de-salted water thorough mixing and layering of 4～10 times of volumes of described upper organic phase from back extraction tower middle and upper part inlet simultaneously, extraction agent flows out from extraction tower top, recycles after the interchanger heat exchange, and the back extraction dilute phosphoric acid flows into the finished acid medial launder from the extraction tower bottom;
Step 4, the back extraction dilute phosphoric acid is sent into the abundant stirring reaction of sweetening agent of smart desulfurizer and 1.05～1.1 times of the energy neutralisation of sulphuric acid radical ions that adds simultaneously with pump, it is temporary to enter medial launder from the top overflow of smart desulfurizer, after with pump it being sent into the pressure filter filtration again, it is temporary that clear liquid enters medial launder, squeeze into pump and to force the vacuum concentration system to concentrate and further obtain industrial phosphoric acid after the defluorinate, again industrial phosphoric acid is carried out multistage crystallization and separate making food grade phosphoric acid.
2. prepare the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate according to claim 1 is described with phosphoric acid by wet process, it is characterized in that: sweetening agent described in the step 1 is that barium carbonate or ground phosphate rock or both mix; Described defluorinating agent is a soda ash; Described regenerator is a caustic soda.
3. prepare the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate according to claim 1 is described with phosphoric acid by wet process, it is characterized in that: sweetening agent described in the step 4 is a barium carbonate.
4. prepare the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate according to claim 1 is described with phosphoric acid by wet process, it is characterized in that: the regeneration of extraction agent described in the step 3 and recycle, regenerator are caustic soda.
5. prepare the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate according to claim 1 is described with phosphoric acid by wet process, it is characterized in that: the described discoloring agent of step 1 is a hydrogen peroxide.
6. prepare the method for PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate according to claim 1 is described with phosphoric acid by wet process, it is characterized in that: described pressure filter is a vertical type full automatic pressure filter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100929041A CN100558633C (en) | 2007-10-26 | 2007-10-26 | The method for preparing PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100929041A CN100558633C (en) | 2007-10-26 | 2007-10-26 | The method for preparing PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101177251A true CN101177251A (en) | 2008-05-14 |
| CN100558633C CN100558633C (en) | 2009-11-11 |
Family
ID=39403703
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2007100929041A Active CN100558633C (en) | 2007-10-26 | 2007-10-26 | The method for preparing PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100558633C (en) |
Cited By (26)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101857212A (en) * | 2010-06-04 | 2010-10-13 | 广西明利集团有限公司 | Method for preparing food-grade monoammonium phosphate from wet-process phosphoric acid |
| CN101857216A (en) * | 2010-06-29 | 2010-10-13 | 贵州川恒化工有限责任公司 | Method for extracting and purifying wet-process phosphorous acid to produce industrial-grade phosphorous acid |
| CN101654235B (en) * | 2009-09-19 | 2011-01-19 | 宜昌瑞特精细化工有限公司 | Method for producing food grade monoammonium phosphate by using agricultural monoammonium phosphate |
| CN101824536B (en) * | 2009-03-03 | 2011-12-14 | 北京有色金属研究总院 | Process for extracting rare-earth from sulfuric acid treating phosphorite process |
| CN102431983A (en) * | 2011-09-30 | 2012-05-02 | 华东理工大学 | Phosphate preparation method |
| CN102442657A (en) * | 2011-10-14 | 2012-05-09 | 吴杰 | Washing technology for refinement of wet-process phosphoric acid by solvent extraction method |
| CN102502547A (en) * | 2011-10-10 | 2012-06-20 | 浙江兴达活性炭有限公司 | Process for removing impurity in phosphoric acid from activated carbon production by phosphoric acid method |
| CN102583284A (en) * | 2012-02-09 | 2012-07-18 | 昆明川金诺化工股份有限公司 | Method for removing slag before solvent extraction in process of producing industrial-grade phosphoric acid by wet-process phosphoric acid |
| CN102602904A (en) * | 2012-04-16 | 2012-07-25 | 瓮福（集团）有限责任公司 | Method for producing monoammonium phosphate from raffinate acid |
| CN102701167A (en) * | 2012-06-13 | 2012-10-03 | 中化化肥有限公司重庆磷复肥工程技术研究中心 | Method for producing industrial ammonium dihydrogen phosphate |
| CN104069646A (en) * | 2014-06-11 | 2014-10-01 | 陈锂 | Extracting agent for purifying wet-process phosphoric acid and method of extracting wet-process phosphoric acid by extracting agent |
| CN104495770A (en) * | 2014-12-24 | 2015-04-08 | 金正大诺泰尔化学有限公司 | Method for purifying wet process phosphoric acid by crystallization in extraction process |
| CN104986746A (en) * | 2015-08-07 | 2015-10-21 | 中化重庆涪陵化工有限公司 | Method for increasing extraction rate of purification of wet process phosphoric acid |
| CN105776169A (en) * | 2016-04-05 | 2016-07-20 | 瓮福（集团）有限责任公司 | Method for washing phosphoric acid loaded organic solvent with compound washing agent |
| CN106629644A (en) * | 2017-01-14 | 2017-05-10 | 湖南省正源储能材料与器件研究所 | Method for producing industrial first-stage and battery-stage monoammonium phosphate by using fertilizer-stage monoammonium phosphate |
| CN107739026A (en) * | 2017-11-13 | 2018-02-27 | 贵阳开磷化肥有限公司 | A kind of method of the micro- reaction production PHOSPHORIC ACID TECH.GRADE ammonium dihydrogen of phosphoric acid by wet process |
| CN108609592A (en) * | 2018-07-04 | 2018-10-02 | 中化重庆涪陵化工有限公司 | The method of Purification of Wet process Phosphoric Acid by Solvent Extraction coproduction potassium dihydrogen phosphate |
| CN108715441A (en) * | 2018-06-01 | 2018-10-30 | 四川省雷波明信化工有限公司 | A kind of fluidized bed process phosphoric acid production technique and system |
| CN109437144A (en) * | 2018-12-21 | 2019-03-08 | 广西川金诺化工有限公司 | A kind of washing methods for wet phosphoric acid purifying |
| CN110817819A (en) * | 2019-09-27 | 2020-02-21 | 瓮福达州化工有限责任公司 | Wet-process phosphoric acid purification system and preparation process thereof |
| CN110917717A (en) * | 2019-12-16 | 2020-03-27 | 瓮福达州化工有限责任公司 | Raffinate acid purification process |
| CN112551497A (en) * | 2020-12-26 | 2021-03-26 | 贵州川恒化工股份有限公司 | Method for preparing industrial phosphoric acid by double salt crystallization method |
| CN113548651A (en) * | 2021-09-09 | 2021-10-26 | 中国石油化工股份有限公司 | Method for purifying wet-process phosphoric acid by solvent extraction |
| CN114436230A (en) * | 2022-01-29 | 2022-05-06 | 贵州芭田生态工程有限公司 | Process for preparing ammonium phosphate to improve quality of lithium iron phosphate by denitrifying phosphoric acid |
| CN115092899A (en) * | 2022-06-27 | 2022-09-23 | 佛山市德方纳米科技有限公司 | Preparation method of diammonium hydrogen phosphate and battery positive electrode material |
| CN116425132A (en) * | 2023-04-21 | 2023-07-14 | 新洋丰农业科技股份有限公司 | Preparation method of high-quality industrial grade monoammonium phosphate |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1204044C (en) * | 2003-05-12 | 2005-06-01 | 四川大学 | Method for preparing industrial grade and food grade phosphoric acid by wet method phosphoric acid |
-
2007
- 2007-10-26 CN CNB2007100929041A patent/CN100558633C/en active Active
Cited By (33)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101824536B (en) * | 2009-03-03 | 2011-12-14 | 北京有色金属研究总院 | Process for extracting rare-earth from sulfuric acid treating phosphorite process |
| CN101654235B (en) * | 2009-09-19 | 2011-01-19 | 宜昌瑞特精细化工有限公司 | Method for producing food grade monoammonium phosphate by using agricultural monoammonium phosphate |
| CN101857212B (en) * | 2010-06-04 | 2012-05-09 | 广西钦州桂金诺磷化工有限公司 | Method for preparing food-grade monoammonium phosphate from wet-process phosphoric acid |
| CN101857212A (en) * | 2010-06-04 | 2010-10-13 | 广西明利集团有限公司 | Method for preparing food-grade monoammonium phosphate from wet-process phosphoric acid |
| CN101857216A (en) * | 2010-06-29 | 2010-10-13 | 贵州川恒化工有限责任公司 | Method for extracting and purifying wet-process phosphorous acid to produce industrial-grade phosphorous acid |
| CN101857216B (en) * | 2010-06-29 | 2012-04-25 | 贵州川恒化工有限责任公司 | Method for extracting and purifying wet-process phosphorous acid to produce industrial-grade phosphorous acid |
| CN102431983A (en) * | 2011-09-30 | 2012-05-02 | 华东理工大学 | Phosphate preparation method |
| CN102502547A (en) * | 2011-10-10 | 2012-06-20 | 浙江兴达活性炭有限公司 | Process for removing impurity in phosphoric acid from activated carbon production by phosphoric acid method |
| CN102442657A (en) * | 2011-10-14 | 2012-05-09 | 吴杰 | Washing technology for refinement of wet-process phosphoric acid by solvent extraction method |
| CN102442657B (en) * | 2011-10-14 | 2014-02-26 | 吴杰 | Washing technology for refinement of wet-process phosphoric acid by solvent extraction method |
| CN102583284A (en) * | 2012-02-09 | 2012-07-18 | 昆明川金诺化工股份有限公司 | Method for removing slag before solvent extraction in process of producing industrial-grade phosphoric acid by wet-process phosphoric acid |
| CN102602904A (en) * | 2012-04-16 | 2012-07-25 | 瓮福（集团）有限责任公司 | Method for producing monoammonium phosphate from raffinate acid |
| CN102701167A (en) * | 2012-06-13 | 2012-10-03 | 中化化肥有限公司重庆磷复肥工程技术研究中心 | Method for producing industrial ammonium dihydrogen phosphate |
| CN104069646B (en) * | 2014-06-11 | 2016-01-06 | 陈锂 | A kind of extractant of purification of wet process phosphoric acid and the method with its extraction phosphoric acid by wet process |
| CN104069646A (en) * | 2014-06-11 | 2014-10-01 | 陈锂 | Extracting agent for purifying wet-process phosphoric acid and method of extracting wet-process phosphoric acid by extracting agent |
| CN104495770A (en) * | 2014-12-24 | 2015-04-08 | 金正大诺泰尔化学有限公司 | Method for purifying wet process phosphoric acid by crystallization in extraction process |
| CN104495770B (en) * | 2014-12-24 | 2017-12-29 | 金正大诺泰尔化学有限公司 | A kind of method of purging by crystallization phosphoric acid by wet process in extraction process |
| CN104986746A (en) * | 2015-08-07 | 2015-10-21 | 中化重庆涪陵化工有限公司 | Method for increasing extraction rate of purification of wet process phosphoric acid |
| CN105776169A (en) * | 2016-04-05 | 2016-07-20 | 瓮福（集团）有限责任公司 | Method for washing phosphoric acid loaded organic solvent with compound washing agent |
| CN106629644A (en) * | 2017-01-14 | 2017-05-10 | 湖南省正源储能材料与器件研究所 | Method for producing industrial first-stage and battery-stage monoammonium phosphate by using fertilizer-stage monoammonium phosphate |
| CN106629644B (en) * | 2017-01-14 | 2018-11-09 | 湖南省正源储能材料与器件研究所 | A method of producing industrial level-one and LITHIUM BATTERY monoammonium phosphate with chemical fertilizer grade monoammonium phosphate |
| CN107739026A (en) * | 2017-11-13 | 2018-02-27 | 贵阳开磷化肥有限公司 | A kind of method of the micro- reaction production PHOSPHORIC ACID TECH.GRADE ammonium dihydrogen of phosphoric acid by wet process |
| CN108715441A (en) * | 2018-06-01 | 2018-10-30 | 四川省雷波明信化工有限公司 | A kind of fluidized bed process phosphoric acid production technique and system |
| CN108715441B (en) * | 2018-06-01 | 2022-01-28 | 雷波明信实业发展有限公司 | Fluidized bed method phosphoric acid production process and system |
| CN108609592A (en) * | 2018-07-04 | 2018-10-02 | 中化重庆涪陵化工有限公司 | The method of Purification of Wet process Phosphoric Acid by Solvent Extraction coproduction potassium dihydrogen phosphate |
| CN109437144A (en) * | 2018-12-21 | 2019-03-08 | 广西川金诺化工有限公司 | A kind of washing methods for wet phosphoric acid purifying |
| CN110817819A (en) * | 2019-09-27 | 2020-02-21 | 瓮福达州化工有限责任公司 | Wet-process phosphoric acid purification system and preparation process thereof |
| CN110917717A (en) * | 2019-12-16 | 2020-03-27 | 瓮福达州化工有限责任公司 | Raffinate acid purification process |
| CN112551497A (en) * | 2020-12-26 | 2021-03-26 | 贵州川恒化工股份有限公司 | Method for preparing industrial phosphoric acid by double salt crystallization method |
| CN113548651A (en) * | 2021-09-09 | 2021-10-26 | 中国石油化工股份有限公司 | Method for purifying wet-process phosphoric acid by solvent extraction |
| CN114436230A (en) * | 2022-01-29 | 2022-05-06 | 贵州芭田生态工程有限公司 | Process for preparing ammonium phosphate to improve quality of lithium iron phosphate by denitrifying phosphoric acid |
| CN115092899A (en) * | 2022-06-27 | 2022-09-23 | 佛山市德方纳米科技有限公司 | Preparation method of diammonium hydrogen phosphate and battery positive electrode material |
| CN116425132A (en) * | 2023-04-21 | 2023-07-14 | 新洋丰农业科技股份有限公司 | Preparation method of high-quality industrial grade monoammonium phosphate |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100558633C (en) | 2009-11-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100558633C (en) | The method for preparing PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process | |
| CN101857216B (en) | Method for extracting and purifying wet-process phosphorous acid to produce industrial-grade phosphorous acid | |
| CN100392124C (en) | Method of retrieving magnesium from high magnesium phosphorus ore | |
| CN104058378B (en) | The method of monoammonium phosphate and magnesium ammonium phosphate is produced with the acid of wet method concentrated phosphoric acid slag | |
| CN103172074A (en) | Process for decomposing potassium feldspar by adopting low-temperature semidry method for comprehensive utilization | |
| CN101993256B (en) | Method for preparing agricultural potassium sulfate from potassium-rich rock | |
| CN104628206A (en) | Recycling technique of lithium iron phosphate production wastewater | |
| CN101186284B (en) | Method for preparing phosphoric acid from phosphorus block ore by wet method and extracting rare earth from phosphorus block ore | |
| CN104495927B (en) | Prepare the method for Vanadium Pentoxide in FLAKES | |
| CN103303886B (en) | Novel method for producing industrial phosphoric acid by purification with wet process phosphoric acid | |
| CN102863267A (en) | Method for producing monoammonium phosphate and coproducing N-P binary compound fertilizer by using wet-process phosphoric acid | |
| CN102701167A (en) | Method for producing industrial ammonium dihydrogen phosphate | |
| CN101386909A (en) | Method for extracting rare-earth from ardealite | |
| CN105197905A (en) | Production method for extracting phosphorite cogeneration feed grade monocalcium phosphate and industrial grade monoammonium phosphate | |
| CN104411626A (en) | Production of ammonium phosphates | |
| CN100503440C (en) | Process of preparing potassium sulfate with potassium containing bittern of magnesium sulfate subtype | |
| CN101434386A (en) | Method for producing fine phosphate by using dilute acid to decompose middle and low grade phosphate ore using | |
| CN103466579A (en) | Method for producing full-water-soluble monoammonium phosphate by phosphoric acid by wet process | |
| CN101186967A (en) | Technique for comprehensive utilization clean production of phosphorus block ore and extracting rare earth form the phosphorus block ore | |
| CN100396600C (en) | Technology of preparing ammonium phosphide using solid liquid reextraction method | |
| CN101633584B (en) | A method for producing nitrogen phosphorus potassium compound fertilizer with water-insoluble potassium-containing rock | |
| CN108569812B (en) | Treatment system and treatment method for wastewater containing low-concentration sulfuric acid | |
| CN100441502C (en) | Method of classification utilizing wet-process phosphoric acid | |
| CN102515114A (en) | High-value and high-efficiency titanium white waste acid utilization method | |
| CN103241720B (en) | Method for preparing amorphous iron phosphate by using phosphate sludge |
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 | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20080514 Assignee: Zhong Hua Yunlong company limited Assignor: Zhonghua Chongqing Fulin Chemical Co., Ltd. Contract record no.: 2012530000059 Denomination of invention: Method for producing technical grade ribose phosphate, food grade ribose phosphate and industry ammonium diacid phosphate using wet-process ribose phosphate Granted publication date: 20091111 License type: Exclusive License Record date: 20120905 |