NO138526B - PROCEDURE FOR PURPOSE ACID PURIFICATION - Google Patents
PROCEDURE FOR PURPOSE ACID PURIFICATION Download PDFInfo
- Publication number
- NO138526B NO138526B NO750908A NO750908A NO138526B NO 138526 B NO138526 B NO 138526B NO 750908 A NO750908 A NO 750908A NO 750908 A NO750908 A NO 750908A NO 138526 B NO138526 B NO 138526B
- Authority
- NO
- Norway
- Prior art keywords
- phosphoric acid
- urea
- urea phosphate
- phosphate
- recycled
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims description 20
- 238000000746 purification Methods 0.000 title claims description 5
- 239000002253 acid Substances 0.000 title description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 70
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 35
- DZHMRSPXDUUJER-UHFFFAOYSA-N [amino(hydroxy)methylidene]azanium;dihydrogen phosphate Chemical compound NC(N)=O.OP(O)(O)=O DZHMRSPXDUUJER-UHFFFAOYSA-N 0.000 claims description 32
- QHDUJTCUPWHNPK-UHFFFAOYSA-N methyl 7-methoxy-2h-indazole-3-carboxylate Chemical compound COC1=CC=CC2=C(C(=O)OC)NN=C21 QHDUJTCUPWHNPK-UHFFFAOYSA-N 0.000 claims description 12
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 8
- 239000012452 mother liquor Substances 0.000 claims description 8
- 229910017604 nitric acid Inorganic materials 0.000 claims description 8
- 239000011541 reaction mixture Substances 0.000 claims description 8
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 5
- 239000004202 carbamide Substances 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 229910019142 PO4 Inorganic materials 0.000 description 5
- 235000021317 phosphate Nutrition 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000000356 contaminant Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 125000000129 anionic group Chemical group 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000013019 agitation Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- 159000000009 barium salts Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 239000001175 calcium sulphate Substances 0.000 description 1
- 235000011132 calcium sulphate Nutrition 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 229940075614 colloidal silicon dioxide Drugs 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052745 lead Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000002367 phosphate rock Substances 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 229910021653 sulphate ion Inorganic materials 0.000 description 1
- -1 sulphate ions Chemical class 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/18—Phosphoric acid
- C01B25/234—Purification; Stabilisation; Concentration
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Fertilizers (AREA)
- Removal Of Specific Substances (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Description
Foreliggende oppfinnelse angår en fremgangsmåte for The present invention relates to a method for
rensning av fosforsyre fra våtprosessen, ofte kaldt "råsyre". purification of phosphoric acid from the wet process, often cold "raw acid".
Fosforsyre fra våtprosessen fremstilles ved omsetning Phosphoric acid from the wet process is produced by conversion
av fosfatstein med svovelsyre og separering av kalsiunsulfat. of phosphate rock with sulfuric acid and separation of calcium sulphate.
Denne syre inneholder anioniske forurensninger, slik som SO^ og This acid contains anionic impurities, such as SO^ and
F, metalliske forurensninger slik som Ca, Mg, Fe, Al, As, Pb og F, metallic impurities such as Ca, Mg, Fe, Al, As, Pb and
Cu, og også kolloidalt siliciumoxyd. Metalliske forurensninger Cu, and also colloidal silicon oxide. Metallic contaminants
gir besværlige avleiringer under lagring. Ennvidere vil i alkali eller ammoniakkopplosninger metalliske forurensninger utfelles som gelatinose fosfater som gjor oppløsningen blakk og tetter igjen filtere. Ennvidere må anioniske og metalliske forurensninger fjernes ved fremstilling av fosfater for næringsmidler for mennesker eller dyr eller vaskemidler. produces troublesome deposits during storage. Furthermore, in alkali or ammonia solutions, metallic contaminants will precipitate as gelatinous phosphates, which make the solution cloudy and clog filters. Furthermore, anionic and metallic contaminants must be removed when producing phosphates for foodstuffs for humans or animals or detergents.
Mange rensemetoder er foreslått. Ifolge en av disse prosesser noytraliseres fosforsyre delvis med natriumhydroxyd, soda, kaliumhydroxyd, kaliumcarbonat eller ammoniakk for å ut-felle metalliske forurensninger som fosfater. Ifolge denne fremgangsmåte fjernes ikke fosfatdoner. Disse må utfelles ved en ytterligere behandling med ét bariumsalt, eller enkelte ganger med et kalsiumsalt. Many cleaning methods have been proposed. According to one of these processes, phosphoric acid is partially neutralized with sodium hydroxide, soda ash, potassium hydroxide, potassium carbonate or ammonia to precipitate metallic impurities such as phosphates. According to this method, phosphate donors are not removed. These must be precipitated by a further treatment with a barium salt, or sometimes with a calcium salt.
Fosforsyre er også blitt renset ved mot s t rom sek>; tråks jon med et organisk opplosningsmiddel. De store mengder av nodvendig opplosningsmiddel er kostbare. Videre vil ved denne fremgangstnå- Phosphoric acid has also been purified by mot s t rom sec>; trit ion with an organic solvent. The large quantities of solvent required are expensive. Furthermore, with this progress,
te sulfationer heller ikke fjernes, da svovelsyre ekstraheres sammen med fosforsyre. På den annen side må kolloidalt silicium-bxyd i enkelte tilfeller flokkuleres separat. sulphate ions are also not removed, as sulfuric acid is extracted together with phosphoric acid. On the other hand, colloidal silicon dioxide must in some cases be flocculated separately.
Foreliggende oppfinnelse angår en fremgangsmåte som mu-liggjor på en enkel måte å redusere forurensningkonsentrasjonen til ca. en tiendedel av den opprinnelige konsentrasjon. The present invention relates to a method which makes it possible in a simple way to reduce the pollution concentration to approx. one tenth of the original concentration.
Foreliggende oppfinnelse angår folgelig en fremgangsmåte The present invention therefore relates to a method
for rensning av fosforsyre fra våtprosessen ved hvilken fosforsyren omsettes med urea, og krystallisert ureafosfat utfelles og skilles fra modervæsken, hvilken fremgangsmåte gr kjemetegnet ved at ureafosfåtet omsettes med salpetersyre, og at ureanitrat skilles fra renset fosforsyre. for the purification of phosphoric acid from the wet process in which the phosphoric acid is reacted with urea, and crystallized urea phosphate is precipitated and separated from the mother liquor, which process is chemically characterized by the urea phosphate being reacted with nitric acid, and urea nitrate being separated from purified phosphoric acid.
Fremstilling av ureafosfat har vært kjent i lang tid, og er eksempelvis beskrevet i britisk patentskrift 1.149.924. The production of urea phosphate has been known for a long time, and is, for example, described in British patent document 1,149,924.
For fremstilling av ureafosfat omsettes fosforsyre fra våtprosessen med urea., og ureafosfat krystalliseres fra reak-sjon sblanding en. For the production of urea phosphate, phosphoric acid from the wet process is reacted with urea, and urea phosphate is crystallized from reaction mixture 1.
Reaksjonen ved dannelsen av ureafosfat The reaction in the formation of urea phosphate
er eksoterm. Eftersom opploseligheten av ureafosfat oker med temperaturen, forbedres krystallisasjonshastigheten for urea fosfat ved avkjoling av reaksjonsblandingen. Krystallisasjonen ut-fores fortrinnsvis ved temperaturer mellom 0 og 25°C, i særdeleshet mellom 15 og 20°C. Selv lavere temperaturer kan anvendes, men kjoleoperasjonen blir da mere kostbar. is exothermic. Since the solubility of urea phosphate increases with temperature, the rate of crystallization of urea phosphate is improved by cooling the reaction mixture. The crystallization is preferably carried out at temperatures between 0 and 25°C, in particular between 15 and 20°C. Even lower temperatures can be used, but the dressing operation then becomes more expensive.
Krystallisert ureafosfat fraskilles ved filtrering eller drenering. En del av modervæskene resirkuleres fortrinnsvis til reaksjonsblandingen for å opprettholde dens fluiditet ved en verdi som er forenelig med en effektiv omroring. Denne resirkulerte del av modervæskene er fortrinnsvis slik at vektforholdet mellom modervæsken og fosforsyre i reaksjonsblandingen er mellom 0,5 og 2,5, fortrinnsvis mellom 1,5 og 2,0. Krystallisert fraskilt ureafosfat vaskes, fortrinnsvis med en opplosning mettet med ureafosfat fra en tidligere operasjon. De erholdte md-dervæsker efter fraskillelse av ureafosfat inneholder hovedmeng-den av forurensningene (SO^, F, Fe, Al) fra den opprinnelige fosforsyre og en viss mengde ^2^*5 °9 ureaai trogen. For å unngå tap anvendes disse modervæsker fortrinnsvis for fremstilling av flytende eller faste gjodningsstoffer. Crystallized urea phosphate is separated by filtration or drainage. A portion of the mother liquors is preferably recycled to the reaction mixture to maintain its fluidity at a value compatible with effective agitation. This recycled part of the mother liquor is preferably such that the weight ratio between the mother liquor and phosphoric acid in the reaction mixture is between 0.5 and 2.5, preferably between 1.5 and 2.0. Crystallized separated urea phosphate is washed, preferably with a solution saturated with urea phosphate from a previous operation. The mud liquids obtained after separation of urea phosphate contain the main amount of the contaminants (SO^, F, Fe, Al) from the original phosphoric acid and a certain amount of ^2^*5 °9 ureaai trogen. To avoid losses, these mother liquors are preferably used for the production of liquid or solid fertilisers.
Det erholdte ureafosfat kan umiddelbart behandles ined salpetersyre under dannelse av renset fosforsyre.. Men da ureafosfat er lettere å lagre og transportere enn fosforsyre, kan det være fordelaktig i enkelte tilfelle å lagre og transportere ureafosfat og fremstille fosforsyre når og hvor den skal anvendes . Muligheten for lagring av ureafosfat gir prosessen The obtained urea phosphate can be immediately treated with nitric acid to form purified phosphoric acid. But as urea phosphate is easier to store and transport than phosphoric acid, it can be advantageous in some cases to store and transport urea phosphate and produce phosphoric acid when and where it is to be used. The possibility of storing urea phosphate provides the process
stor fleksibilitet. Dette fosfat har flere anvendelser: flytende gjodningsstoffer, dyrefor, brannslukningsmiddel, metall-fosfateringsmiddel. Alt efter behov kan derfor ureafosfat enten selges eller anvendes for å fremstille renset fosforsyre. great flexibility. This phosphate has several uses: liquid fertilizers, animal feed, fire extinguishing agent, metal phosphating agent. Depending on the need, urea phosphate can therefore either be sold or used to produce purified phosphoric acid.
I det annet trinn omsettes ureafosfat med salpetersyre for å gi renset fosforsyre og ureanitrat ifolge reaksjonslignin-gen: In the second step, urea phosphate is reacted with nitric acid to give purified phosphoric acid and urea nitrate according to the reaction equation:
Ureanitrat er et hvitt krystallisert fast materiale san fraskilles fra fosforsyre ved filtrering eller drenering. Resir-kulering til reaksjonsblandingen av en del av fosforsyren for-bedrer filtreringen eller dreneringen. Den resirkulerte del er fortrinnsvis slik at vektforholdet mellom resirkulert fosforsyre og ureafosfat er mellom 0,4 og 3, fortrinnsvis 1. Stokiometri-ske mengder av salpetersyre anvendes fortrinnsvis, men ikke de-sto mindre er i enkelte tilfelle et overskudd av salpetersyre fordelaktig da det nedsetter opploseligheten til ureanitrat i reaks jonsblandingen. Urea nitrate is a white crystallized solid material that can be separated from phosphoric acid by filtration or drainage. Recirculation to the reaction mixture of a portion of the phosphoric acid improves the filtration or drainage. The recycled part is preferably such that the weight ratio between recycled phosphoric acid and urea phosphate is between 0.4 and 3, preferably 1. Stoichiometric amounts of nitric acid are preferably used, but nevertheless in some cases an excess of nitric acid is advantageous as it reduces the solubility of urea nitrate in the react ion mixture.
Drenert ureanitrat vaskes med vann med en temperatur fortrinnsvis varierende mellom O og 5°C for å forhindre opplbs-ning av formeget ureanitrat. Mengden av anvendt vann er fortrinnsvis ca. 20 vekt% av ureanitratet. Det således erholdte ureanitrat kan lett anvendes som nitrogenopplosning for fremstilling av flytende gjodningsstoffer. Drained urea nitrate is washed with water at a temperature preferably varying between 0 and 5°C to prevent dissolution of formed urea nitrate. The amount of water used is preferably approx. 20% by weight of the urea nitrate. The urea nitrate thus obtained can easily be used as a nitrogen solution for the production of liquid fertilisers.
Som det fremgår av det ovenfor angitte er fremgangsmå-ten særlig fordelaktig, da alle biprodukter kan anvendes. Et ek-sempel er gitt i det efterf6lgende for å illustrere oppfinnelsen. As can be seen from the above, the method is particularly advantageous, as all by-products can be used. An example is given below to illustrate the invention.
I en blander ble innfort 1818 g fosforsyre inneholdende 54,4 % P2°5 °9 fSigende forurensninger (vekt%). In a mixer, 1818 g of phosphoric acid containing 54.4% P2°5°9 fSuggesting impurities (wt%) were introduced.
F 0,49 F 0.49
SC- 3,38 SC- 3.38
Ca 0,54 About 0.54
Mg 0,33 Mg 0.33
Fe 0,09 Fe 0.09
Al 0,17 Al 0.17
og 845 g urea med 46 % N såvel som 2540 g resirkulert modervæske og 500 g resirkulert vaskevann. Vektforholiet mellom modervæsker og fosforsyre er ca. 1,7. Blandingen fikk omsettes i lopet av en time og ble holdt ved en temperatur på 18°C. Den ble derefter sentrifugert for å fraskille 1980 g ureafosfat og 3732 modervæske inneholdende 316 g N og 815 g P2°5' nvorav 2540 g ble resirkulert til blanderen. Ureafosfat ble vasket i en trommel med en mettet opplosning av ureafosfat erholdt ved opplesning av 254 g renset ureafosfat i 229 g vann. Efter vasking ble der erholdt 1980 g renset ureafosfat, hvorav 254 g ble anvendt for fremstilling av vaskeoppldsningen. 1726 g renset ureafosfat og 1223 g 53 %'s salpetersyre ble innfort sammen med 1726 g resirkulert fosforsyre. Vektforholdet mellom resirkulert fosforsyre og ureafosfat var ca. 1. Blandingen fikk omsettes 1 time og ble derefter sentrifugert. and 845 g of urea with 46% N as well as 2540 g of recycled mother liquor and 500 g of recycled wash water. The weight ratio between mother liquors and phosphoric acid is approx. 1.7. The mixture was allowed to react over the course of one hour and was kept at a temperature of 18°C. It was then centrifuged to separate 1980 g of urea phosphate and 3732 of mother liquor containing 316 g of N and 815 g of P2°5' of which 2540 g was recycled to the mixer. Urea phosphate was washed in a drum with a saturated solution of urea phosphate obtained by dissolving 254 g of purified urea phosphate in 229 g of water. After washing, 1980 g of purified urea phosphate were obtained, of which 254 g were used to prepare the washing solution. 1726 g of purified urea phosphate and 1223 g of 53% nitric acid were introduced together with 1726 g of recycled phosphoric acid. The weight ratio between recycled phosphoric acid and urea phosphate was approx. 1. The mixture was allowed to react for 1 hour and was then centrifuged.
Der ble erholdt 2980 g fosforsyre inneholdende 43 % P^O^ og 1695 g ureanitrat. Ureanitrat ble vasket i en trommel med 420 g vann ved 0°C. 2980 g of phosphoric acid containing 43% P^O^ and 1695 g of urea nitrate were obtained. Urea nitrate was washed in a drum with 420 g of water at 0°C.
625 g av det erholdte vaskevann inneholdende 460 g 625 g of the obtained washing water containing 460 g
<p>^05 ble tilsatt til renset fosforsyre. Efter rensning ble der erholdt 1490 g ureanitrat og 1879 g fosforsyre inneholdende 39,5 % P205°3 met^ folgende sammensetning: F 0,03 <p>^05 was added to purified phosphoric acid. After purification, 1490 g of urea nitrate and 1879 g of phosphoric acid containing 39.5% P205°3 with the following composition were obtained: F 0.03
SO. 0,02 SO. 0.02
Ca 0,01 About 0.01
Mg 0,02 Mg 0.02
Fe 0,01 Fe 0.01
Al 0,01 Al 0.01
Claims (5)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR7409158A FR2264774B1 (en) | 1974-03-19 | 1974-03-19 |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| NO750908L NO750908L (en) | 1975-09-22 |
| NO138526B true NO138526B (en) | 1978-06-12 |
| NO138526C NO138526C (en) | 1978-09-20 |
Family
ID=9136486
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO750908A NO138526C (en) | 1974-03-19 | 1975-03-18 | PROCEDURE FOR PURPOSE ACID PURIFICATION. |
Country Status (14)
| Country | Link |
|---|---|
| JP (1) | JPS5440075B2 (en) |
| BE (1) | BE826810A (en) |
| ES (1) | ES435760A1 (en) |
| FI (1) | FI58767C (en) |
| FR (1) | FR2264774B1 (en) |
| GB (1) | GB1438269A (en) |
| IL (1) | IL46740A (en) |
| IT (1) | IT1036884B (en) |
| MX (1) | MX3087E (en) |
| NL (1) | NL167391C (en) |
| NO (1) | NO138526C (en) |
| SE (2) | SE7503010L (en) |
| YU (1) | YU36663B (en) |
| ZA (1) | ZA751297B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES482524A1 (en) * | 1979-07-17 | 1980-04-01 | Cros Sa | Food-pharmaceutical quality phosphoric acid preparation - by treating urea phosphate with nitric acid, then with nitrous acid, passing air and reducing nitrate with saccharide(s) or formic acid |
| TW421606B (en) * | 1995-06-21 | 2001-02-11 | Mohamed Takhim | Method of purifying substances by extraction from a liquid medium |
| WO2008046428A1 (en) * | 2006-10-18 | 2008-04-24 | Fekria Ahmed Fathi Kassem | New method for cheap production of urea phosphate |
| CN103170221A (en) * | 2013-04-18 | 2013-06-26 | 瓮福（集团）有限责任公司 | Method and device for exhaust gas treatment by wet-process phosphoric acid reaction |
| CN104311181B (en) * | 2014-09-19 | 2017-02-08 | 贵州大学 | Preparation method of special fertilizer for honey peaches |
| CN107473990A (en) * | 2017-07-24 | 2017-12-15 | 湖北三宁化工股份有限公司 | A kind of urea phosphate mother liquor water soluble fertilizer and preparation method |
| USD943707S1 (en) * | 2019-10-25 | 2022-02-15 | Tianjin Bright Sight Commerce Co., Ltd. | Filter |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE754920A (en) * | 1969-08-22 | 1971-02-01 | Hachez Pierre | PROCESS FOR PURIFYING PHOSPHORIC ACID PRODUCED BY WET METHODS AND A POTASSIUM-BASED PHOSPHATE BY-PRODUCT THAT CAN BE USED AS A FERTILIZER |
-
1974
- 1974-03-19 FR FR7409158A patent/FR2264774B1/fr not_active Expired
-
1975
- 1975-02-28 GB GB857375A patent/GB1438269A/en not_active Expired
- 1975-03-01 MX MX100043U patent/MX3087E/en unknown
- 1975-03-03 ZA ZA00751297A patent/ZA751297B/en unknown
- 1975-03-03 IL IL46740A patent/IL46740A/en unknown
- 1975-03-13 NL NL7503004.A patent/NL167391C/en not_active IP Right Cessation
- 1975-03-13 YU YU0606/75A patent/YU36663B/en unknown
- 1975-03-17 SE SE7503010D patent/SE7503010L/xx not_active Application Discontinuation
- 1975-03-17 SE SE7503010A patent/SE393361B/en not_active IP Right Cessation
- 1975-03-18 ES ES435760A patent/ES435760A1/en not_active Expired
- 1975-03-18 JP JP3286775A patent/JPS5440075B2/ja not_active Expired
- 1975-03-18 BE BE154441A patent/BE826810A/en not_active IP Right Cessation
- 1975-03-18 FI FI750803A patent/FI58767C/en not_active IP Right Cessation
- 1975-03-18 NO NO750908A patent/NO138526C/en unknown
- 1975-03-18 IT IT48663/75A patent/IT1036884B/en active
Also Published As
| Publication number | Publication date |
|---|---|
| GB1438269A (en) | 1976-06-03 |
| JPS5440075B2 (en) | 1979-12-01 |
| SE7503010L (en) | 1975-09-22 |
| NL167391B (en) | 1981-07-16 |
| FI58767B (en) | 1980-12-31 |
| IL46740A (en) | 1977-07-31 |
| FI750803A (en) | 1975-09-20 |
| DE2511345A1 (en) | 1975-09-25 |
| FI58767C (en) | 1981-04-10 |
| NO750908L (en) | 1975-09-22 |
| ES435760A1 (en) | 1976-12-16 |
| DE2511345B2 (en) | 1977-02-17 |
| MX3087E (en) | 1980-03-27 |
| SE393361B (en) | 1977-05-09 |
| NL7503004A (en) | 1975-09-23 |
| ZA751297B (en) | 1976-01-28 |
| YU60675A (en) | 1982-06-18 |
| YU36663B (en) | 1984-08-31 |
| IL46740A0 (en) | 1975-05-22 |
| NO138526C (en) | 1978-09-20 |
| IT1036884B (en) | 1979-10-30 |
| FR2264774B1 (en) | 1977-06-17 |
| JPS50131892A (en) | 1975-10-18 |
| BE826810A (en) | 1975-09-18 |
| NL167391C (en) | 1981-12-16 |
| FR2264774A1 (en) | 1975-10-17 |
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