CN1312030C - Method for purifying wet-process phosphoric acid by crystallization - Google Patents
Method for purifying wet-process phosphoric acid by crystallization Download PDFInfo
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- CN1312030C CN1312030C CNB2005100137147A CN200510013714A CN1312030C CN 1312030 C CN1312030 C CN 1312030C CN B2005100137147 A CNB2005100137147 A CN B2005100137147A CN 200510013714 A CN200510013714 A CN 200510013714A CN 1312030 C CN1312030 C CN 1312030C
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Abstract
The present invention relates to a method for purifying wet-process phosphoric acid by crystallization. After simple treatment, raw material acid is pre-purified via a solvent with the precipitation method; obtained phosphoric acid is concentrated to 85% to 90% and is crystallized at the temperature of 8 to 20 DEG C. Seed crystal taking 1 to 3% of the total acid liquor quality or a medium crystal agent is introduced and crystallized for 2 to 5h; separated, washed and diluted crystal products reach requirements for food-grade phosphoric acid. The obtained semiwater phosphoric acid crystals are melted and diluted to 85 to 90%, and then recrystallized, and crystallized for the third time respectively at the operating temperature of 5 to 15 DEG C and 0 to 9 DEG C; separated, washed and diluted crystal products respectively reach requirements for qualified electronic-grade and quality electronic-grade phosphoric acid. Compared with the foreign like techniques, the present invention has the advantages of high removal rate on impurity ions, low producing energy consumption, wide purity range of treated raw material acid, wide grade, high purity and good chromaticity of the obtained product, high comprehensive usage rate of P2O5 and favorable economic benefit.
Description
Technical field
The present invention relates to the crystallization technique field, particularly a kind of method of purifying wet-process phosphoric acid by crystallization.
Background technology
Foreign matter content is quite high in the phosphoric acid by wet process, mainly is the vitriol of different content, organic compound, arsenic and other metal ions.These impurity derive from the sulfuric acid that uses in Rock Phosphate (72Min BPL) and the production process.Phosphoric acid by wet process must reduce these foreign matter contents effectively just can be used in industry-by-industries such as industry, foodstuff additive, medicine, electronics later on.Present process for purification mainly contains extraction process, ion exchange method, crystallization process etc.
Compare with other several methods, the simple energy consumption of crystallization process equipment is low, and operating process is polluted little, the product purity height that obtains, and colourity is good.So since the eighties, it is quite active to utilize crystallization technique to carry out the research of wet phosphoric acid refining, main technological route has following four kinds: (i) go out H by crystallization in the phosphoric acid by wet process
3PO
41/2H
2O (29.32 ℃ of fusing points) or H
3PO
4(42.35 ℃ of fusing points); (ii) crystallization precipitation of phosphorus hydrochlorate is converted into phosphoric acid then; (iii) adding urea, melamine etc. separates out phosphoric acid formation complex salt crystal; (∏) solvent precipitation, this method adopts the solvent that dissolves each other fully with water, as methyl alcohol, ethanol, Virahol or propyl alcohol etc., makes phosphoric acid and water-soluble in solvent, and impurity formation insoluble salt precipitation is removed.
Once mainly contained with purifying wet-process phosphoric acid by crystallization and the research that reaches the above purity requirement of food grade:
Russian patent 2,059,570 adopt 4 one step crystallizings to reach the food grade requirement, German Patent 20,059,827 pairs of raw material phosphoric acid carry out the multistep pre-treatment, reach the food grade requirement with 3 one step crystallizings then.Korean Patent 2,003 in 2003, and 042,108 utilizes the fusion-crystallization method to reach the requirement of food grade phosphoric acid equally.Above patent all requires with chemical precipitation method or adds strong oxidizer raw material acid is carried out pre-treatment, purifies with crystallization process after removing partial impurities again.
Preparation as for electron-level phosphoric acid, owing in its standard plurality of impurity ions content is all had harsh restriction, higher when using crystallization process to used raw material acid purity requirement, so at present crystallization process is mainly used in the further purification of thermal phosphoric acid or other high purity rank phosphoric acid, it is few directly to do the report of feedstock production electron-level phosphoric acid with phosphoric acid by wet process.
For example russian patent 2,209, and 178 usefulness crystallization processs purify thermal phosphoric acid, and product reaches CooTB Ty electronic industry phosphoric acid standard; Japanese Patent 3,193,614 and 3,237,009 respectively with solution crystal process and the fusion-crystallization method electron-level phosphoric acid of further purifying, and obtains foreign matter content at other high-purity phosphoric acid of ppb level.
In the prior art, the direct solution crystallization of impure more phosphoric acid by wet process is difficulty quite, because the impurity in the phosphoric acid by wet process plays katalysis, ortho-phosphoric acid heating back generation polyphosphazene polymer phosphoric acid sharply increases viscosity and is difficult to separate out crystal.And if from the phosphoric acid by wet process direct crystallization be purified to food grade phosphoric acid must be more than 3 times recrystallization, the complex process yield is lower.So the direct crystallization method does not also realize industrialization so far.
The main raw material of electron-level phosphoric acid preparation at present is a thermal phosphoric acid, and the production process energy consumption of thermal phosphoric acid is big, and environmental pollution is also big, will be replaced by the production of phosphoric acid by wet process soon.Purify so be necessary to study the further refining of phosphoric acid by wet process, to satisfy the needs of following phosphoric acid production.
Summary of the invention
The present invention uses solvent precipitation and the refining phosphoric acid by wet process of solution crystal process coupling.
Processing step comprises successively that pre-treatment, solvent deposition purify, concentrate, crystallization, filtering separation, washing crystal, fusion dilution, recrystallization, three crystallizations.
Specifically may further comprise the steps:
(1). will carry out crystallization operation behind the Phosphoric Acid Concentration to 85% after the preliminary cleaning～90%: crystallization for the first time, temperature is 8 ℃～20 ℃, introduces crystal seed or medium crystallization agent, its amount is 1%～3% of total acid solution quality, crystallization time 2h～5h; Mother liquor with the next stage crystallization operation washs resulting crystal product at the corresponding levels; Used washings quality is 20%～30% of a filter cake quality;
(2). the half water phosphoric acid crystal that will obtain fusion, carry out recrystallization after being diluted to 85%～90%, 5 ℃～15 ℃ of service temperatures, operating time 3h～6h reaches qualified electron-level phosphoric acid requirement behind the crystal product separating, washing.
In order to obtain more other phosphoric acid of top grade, can carry out crystallization for the third time again, 0 ℃～10 ℃ of service temperatures, operating time 4h～8h reaches the requirement of high-quality electron-level phosphoric acid behind the crystal product separating, washing.
After phosphoric acid by wet process carries out simple sulphur removal, arsenic removal and decolouring processing, under agitation add the organic solvent that dissolves each other fully with water, carry out preliminary cleaning operation with solvent precipitation, after organic solvent was distilled mutually, still liquid was handled, is concentrated and be purified acid through activated carbon decolorizing.
The method that the present invention can adopt is:
(1) acid after the simple process and ammonia or an alkali metal salt reaction, ammonia or alkalimetal ion and P
2O
5Mol ratio be 0.05～0.30, under agitation add the organic solvent that dissolves each other fully with water then, solvent is 2.0～3.6: 1 with the mass ratio of acid, 35 ℃～60 ℃ of temperature of reaction, reaction times 10min～30min;
(2) adding mass concentration in the solution of step (1) is 20%～30% alkaline solution, the volume ratio of mother liquor and alkaline solution is 50～90: 1, stirring reaction 10min～30min, the organic solvent of separated salt water and phosphoric acid mutually after leaving standstill, organic solvent is distilled mutually, and still liquid obtains PHOSPHORIC ACID TECH.GRADE after activated carbon decolorizing is handled;
Alkaline solution can adopt NaOH solution or NaH
2PO
4Solution etc.
The mixture of one or more that the described organic solvent that dissolves each other fully with water is Virahol, methyl alcohol, propyl alcohol or acetone.
Below method of the present invention and principle are described in further detail.
Pre-treatment is sulphur removal, arsenic removal, decolouring to be placed on an operation carry out.Adopt conventional sweetening agent, dearsenification and heavy metal agent and discoloring agent.
The organic solvent of phosphoric acid is distilled mutually, recycle behind the solvent distillation, still liquid simmer down to technical grade behind activated carbon decolorizing purifies acid.After being concentrated to 85%～90%, the technical grade acid that obtains carries out crystallization operation.At first, adopt the mode of heat exchange that acid solution is cooled to FCTA temprature.Under the situation that has crystal seed to exist, Tc crosses when low that foreign ion causes that easily bringing out the formula nucleation makes soltion viscosity sharp increase filtration difficulty in the acid; P when temperature is too high
2O
5Yield reduces does not have economic benefit.For example to the crystallization first time, suitable operating temperature range is 8 ℃～20 ℃.After acid liquor temperature is stable, introduce good crystal seed or the medium crystallization agent that accounts for total acid solution quality 1～3%; The operation final stage can improve yield by cooling.
Another key factor that influences foreign ion removal efficient is the residence time.Because the crystalline form of As, Cr, compound that V forms is close with half water phosphoric acid crystalline form in the impurity, these impurity can not get effective separation when the phosphoric acid crystalline growth velocity is too fast; Iron also is easy to be incorporated in the lattice of phosphoric acid simultaneously.So the suggestion crystallization time surpasses 2h, by controlling suitable crystalline growth velocity, obtains higher purification efficiency.
Another important step is the washing of crystal product in the crystallization operation.The washings of using in the aforesaid method is the mother liquor of next stage crystallization operation; The last step washings is made with the finished product dilution.Used washings quality is that 20～30% of filter cake quality is advisable, and washings concentration can not be too big, otherwise viscosity is higher not easy to operate.Mother liquor in the crystallization operation process and washings can purify acid with upper level after treatment and mix sale.
Simple pretreated phosphoric acid by wet process is at first handled through additive methods such as solvent deposition or extractions, removes most of impurity metal ion and anionic part impurity such as Fe, Mg, Al, Ca.Viscosity reduced after the removal of these impurity made Phosphoric Acid Concentration, solution crystallization operation easy to implement.The method of purifying wet-process phosphoric acid by crystallization of the present invention is applicable to the purification of the thermal phosphoric acid that meets purity requirement or the technical grade behind the wet phosphoric acid refining, food grade phosphoric acid, also can be used for the further purification of qualified electron-level phosphoric acid.
In addition, the present invention also improves existing phosphoric acid crystallization processes, with typical operational condition russian patent 2 for example, 209,178 compare, and by suitable raising service temperature and control crystalline growth velocity, have reduced to bring out the probability of nucleation, when improving foreign ion removal efficient, shorten the operating time, reduced production energy consumption.The recrystallization product purity has surpassed the data of russian patent report, and three crystallizations reach high-quality electron-level phosphoric acid standard.
Embodiment
Embodiment 1:
600 gram phosphoric acid by wet processes, P
2O
5Concentration 39.8% adds 5.4 gram CaO, 3.8 gram Na
2S, 0.6 gram gac and 0.6 gram diatomite, sealed reaction 2h.The suction filtration separation obtains filtrate 560 grams, P
2O
5Concentration 38.7%.The filtrate heating is concentrated into 460 grams, stirs to add NH
35.3 gram, 60～80 ℃ of temperature of reaction in 0.5 hour reaction times, stir adding Virahol 1000ml down, reaction 10min fast.Cross filter residue and make fertilizer after washing drying, back separated salt water and organic phase are reacted, left standstill to the NaOH solution stirring that adds 20ml 20% in the mother liquor.Solvent in the organic phase distills to such an extent that acid solution 312 restrains P
2O
5Concentration 55.2%; Behind activated carbon decolorizing, be concentrated into P
2O
5Concentration 62% promptly obtains PHOSPHORIC ACID TECH.GRADE, forms to see Table 1.
Phosphoric acid 250 grams that aforesaid method obtains, P
2O
5Concentration is introduced medium crystallization agent 5 grams down for 63.9%, 19 ℃, keeps stirring velocity 200r.p.m, is cooled to 8 ℃, operation 3.0h, suction filtration separates, and filter cake is 80% next stage crystalline mother solution washing with 20 gram mass concentration, obtain product 102 gram, fusion dilute food grade phosphoric acid, form and list in table 1.This step crystallization operation P
2O
5Mass yield is 42.4%, and mother liquor and washings purify acid with aforementioned technical grade and mix use after decolouring is handled.
Table 1 streams is formed (%)
Embodiment 2:
Embodiment 1 gets phosphatase 11 00 gram, P
2O
5Concentration 63.9%, introduce medium crystallization agent 2.0 grams down for 15 ℃, keep stirring velocity 200r.p.m, be cooled to 5 ℃, operation 5.0h, suction filtration separates, filter cake is 80% next stage crystalline mother solution washing with 10 gram mass concentration, obtain product 47.6 grams, can be used for electron trade after the fusion dilution, form and list in table 2.This step crystallization operation P
2O
5Mass yield is 49.0%, and mother liquor and washings purify acid with aforementioned food grade and mix use.
Embodiment 3:
Embodiment 2 gets phosphatase 24 5 grams, P
2O
5Concentration is introduced medium crystallization agent 0.9 gram down for 63.9%, 10 ℃, keeps stirring velocity 160r.p.m, is cooled to 2 ℃, operation 6.0h, suction filtration separates, and filter cake is 80% high-purity phosphoric acid washing with 5 gram mass concentration, obtain product 21.0 gram, fusion dilute the high-quality electron-level phosphoric acid, form and also list in table 2.This step crystallization operation P
2O
5Mass yield is 48.6%, and mother liquor and washings purify acid with aforementioned qualified electronic-grade and mix use.
Table 2 streams is formed (%)
Embodiment 4
Commercially available PHOSPHORIC ACID TECH.GRADE 200 grams (composition sees Table 3), P
2O
5Concentration is introduced medium crystallization agent 4.0 grams down for 62.0%, 16 ℃, keeps stirring velocity 200r.p.m, is cooled to 5 ℃, operation 7.0h, suction filtration separates, and filter cake is with the 20 analytical pure phosphoric acid washings that restrain concentration 80%, obtain product 89.7 grams, can be used for electron trade after the fusion dilution, composition sees Table 3.This step crystallization operation P
2O
5Mass yield is 47.1%, and mother liquor and washings can be done PHOSPHORIC ACID TECH.GRADE and use.
Table 3 streams is formed (%)
The present invention open and the preparation method and the product that propose, those skilled in the art can be by using for reference this paper content, and links such as appropriate change raw material, processing parameter realize.Method of the present invention and product are described by preferred embodiment, person skilled obviously can be in not breaking away from content of the present invention, spirit and scope to method as herein described with product is changed or suitably change and combination, realize the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (7)
1. the method for a purifying wet-process phosphoric acid by crystallization may further comprise the steps:
(1). carry out crystallization operation after the phosphoric acid by wet process after the preliminary cleaning is concentrated to 85%～90%: crystallization for the first time, temperature is 8 ℃～20 ℃, introduces crystal seed or medium crystallization agent, its amount is 1%～3% of total acid solution quality, crystallization time 2h～5h; Mother liquor with the next stage crystallization operation washs resulting crystal product at the corresponding levels; Used washings quality is 20%～30% of a filter cake quality;
(2). the half water phosphoric acid crystal that will obtain fusion, carry out recrystallization after being diluted to 85%～90%, 5 ℃～15 ℃ of service temperatures, operating time 3h～6h reaches qualified electron-level phosphoric acid requirement behind the crystal product separating, washing.
2. the method for a kind of purifying wet-process phosphoric acid by crystallization as claimed in claim 1, it is characterized in that carrying out crystallization for the third time in described step (2) back, 0 ℃～10 ℃ of service temperatures, operating time 4h～8h, crystal product separating, washing reach the requirement of high-quality electron-level phosphoric acid.
3. the method for a kind of purifying wet-process phosphoric acid by crystallization as claimed in claim 1 or 2, it is characterized in that at described phosphoric acid by wet process through after the simple process, under agitation add the organic solvent that dissolves each other fully with water, carry out the preliminary cleaning operation with solvent precipitation, after organic solvent distilled mutually, still liquid was handled, is concentrated and be purified acid through activated carbon decolorizing.
4. the method for a kind of purifying wet-process phosphoric acid by crystallization as claimed in claim 3 is characterized in that may further comprise the steps in described method:
(1) acid after the simple process and ammonia or an alkali metal salt reaction, ammonia or alkalimetal ion and P
2O
5Mol ratio be 0.05～0.30, under agitation add the organic solvent that dissolves each other fully with water then, solvent is 2.0～3.6: 1 with the mass ratio of acid, 35 ℃～60 ℃ of temperature of reaction, reaction times 10min～30min;
(2) adding mass concentration in the solution of step (1) is 20%～30% alkaline solution, the volume ratio of mother liquor and alkaline solution is 40～90: 1, stirring reaction 10min～30min, the organic solvent of separated salt water and phosphoric acid mutually after leaving standstill, organic solvent is distilled mutually, and still liquid is purified phosphoric acid after activated carbon decolorizing is handled.
5. the method for a kind of purifying wet-process phosphoric acid by crystallization as claimed in claim 4 is characterized in that described alkaline solution is NaOH solution or NaH
2PO
4Solution.
6. the method for a kind of purifying wet-process phosphoric acid by crystallization as claimed in claim 4, the mixture of one or more that it is characterized in that the described organic solvent that dissolves each other fully with water is Virahol, methyl alcohol, propyl alcohol or acetone.
7. the method for a kind of purifying wet-process phosphoric acid by crystallization as claimed in claim 1 or 2 is characterized in that described method is applied to meet the further purification of the thermal phosphoric acid of purity requirement or the technical grade behind the wet phosphoric acid refining, food grade phosphoric acid.
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| JP2008247733A (en) * | 2007-03-14 | 2008-10-16 | Niro Process Technology Bv | Purification of phosphoric acid rich stream |
| CN101774555B (en) * | 2010-02-02 | 2011-08-31 | 天津大学 | Method for preparing electronic grade phosphoric acid through liquid membrane crystallization |
| CN102730656A (en) * | 2012-06-26 | 2012-10-17 | 瓮福（集团）有限责任公司 | Method for preparing phosphoric acid with high concentration by microwave heating of raffinate acid |
| CN103754847B (en) * | 2013-12-30 | 2016-01-20 | 广西明利化工有限公司 | The method of electron-level phosphoric acid is produced in a kind of U-tube crystallization |
| 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 |
| CN105253869B (en) * | 2015-09-27 | 2017-12-05 | 海南医学院 | A kind of wet method prepares the method that process phosphoric acid reduces Oil repellent in accessory substance |
| CN105366655B (en) * | 2015-12-10 | 2018-01-02 | 四川蓝海化工（集团）有限公司 | The preparation method of capacitor stage phosphoric acid crystal |
| CN106517122A (en) * | 2016-11-04 | 2017-03-22 | 秦皇岛天鼎化工有限公司 | Applications of a nitrogen-based oxidant in wet-process phosphoric acid decolouring, wet-process phosphoric acid decolouring method, and device |
| CN106809812B (en) * | 2017-03-14 | 2023-05-23 | 镇江江南化工有限公司 | Method and device for preprocessing crude sodium pyrophosphate |
| CN112551497B (en) * | 2020-12-26 | 2022-11-18 | 贵州川恒化工股份有限公司 | Method for preparing industrial phosphoric acid by double salt crystallization method |
| CN114408887A (en) * | 2022-01-28 | 2022-04-29 | 江苏电科环保有限公司 | Method for preparing electronic grade phosphoric acid |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03193614A (en) * | 1989-12-21 | 1991-08-23 | Nippon Chem Ind Co Ltd | High purity phosphoric acid and its production |
| RU2059570C1 (en) * | 1995-07-05 | 1996-05-10 | Николай Николаевич Бушуев | Extraction phosphoric acid purification from impurities method |
| CN1134914A (en) * | 1996-01-18 | 1996-11-06 | 昆明理工大学 | Solvent sedimentation method for purifying wet method phosphoric acid |
| CN1139072A (en) * | 1995-06-26 | 1997-01-01 | 广东湛化企业集团公司 | Wet phosphoric acid purifying techn eliminating fluorine and heavy metals |
| CN1217705A (en) * | 1997-02-03 | 1999-05-26 | 吉乌里尼化学两合公司 | Wet-process technique for refiining phosphoric acid |
| JP3193614B2 (en) * | 1996-02-15 | 2001-07-30 | 株式会社ピーエフユー | Customer display device |
| RU2209178C1 (en) * | 2002-02-22 | 2003-07-27 | Открытое акционерное общество "РЕАТЭКС" | Method of purification of dry-process phosphoric acid |
| CN1483666A (en) * | 2003-05-12 | 2004-03-24 | 四川大学 | Method for preparing industrial grade and food grade phosphoric acid by wet method phosphoric acid |
-
2005
- 2005-06-09 CN CNB2005100137147A patent/CN1312030C/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03193614A (en) * | 1989-12-21 | 1991-08-23 | Nippon Chem Ind Co Ltd | High purity phosphoric acid and its production |
| CN1139072A (en) * | 1995-06-26 | 1997-01-01 | 广东湛化企业集团公司 | Wet phosphoric acid purifying techn eliminating fluorine and heavy metals |
| RU2059570C1 (en) * | 1995-07-05 | 1996-05-10 | Николай Николаевич Бушуев | Extraction phosphoric acid purification from impurities method |
| CN1134914A (en) * | 1996-01-18 | 1996-11-06 | 昆明理工大学 | Solvent sedimentation method for purifying wet method phosphoric acid |
| JP3193614B2 (en) * | 1996-02-15 | 2001-07-30 | 株式会社ピーエフユー | Customer display device |
| CN1217705A (en) * | 1997-02-03 | 1999-05-26 | 吉乌里尼化学两合公司 | Wet-process technique for refiining phosphoric acid |
| RU2209178C1 (en) * | 2002-02-22 | 2003-07-27 | Открытое акционерное общество "РЕАТЭКС" | Method of purification of dry-process phosphoric acid |
| CN1483666A (en) * | 2003-05-12 | 2004-03-24 | 四川大学 | Method for preparing industrial grade and food grade phosphoric acid by wet method phosphoric acid |
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Assignee: Tianjin Tianda United Engineering & Technology Co., Ltd. Assignor: Beijing Hongyuandi Green Technology Co., Ltd. Contract fulfillment period: 2009.6.10 to 2014.6.9 Contract record no.: 2009120000145 Denomination of invention: Method for purifying wet-process phosphoric acid by crystallization Granted publication date: 20070425 License type: Exclusive license Record date: 20090731 |
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