JPS6018606B2 - Wet phosphoric acid manufacturing method - Google Patents
Wet phosphoric acid manufacturing methodInfo
- Publication number
- JPS6018606B2 JPS6018606B2 JP5210481A JP5210481A JPS6018606B2 JP S6018606 B2 JPS6018606 B2 JP S6018606B2 JP 5210481 A JP5210481 A JP 5210481A JP 5210481 A JP5210481 A JP 5210481A JP S6018606 B2 JPS6018606 B2 JP S6018606B2
- Authority
- JP
- Japan
- Prior art keywords
- phosphoric acid
- solution
- ore
- dilute phosphoric
- acid solution
- 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.)
- Expired
Links
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 title claims description 88
- 229910000147 aluminium phosphate Inorganic materials 0.000 title claims description 44
- 238000004519 manufacturing process Methods 0.000 title claims description 13
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims description 15
- 238000004140 cleaning Methods 0.000 claims description 13
- 239000002244 precipitate Substances 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 7
- 238000005406 washing Methods 0.000 claims description 5
- 229910019142 PO4 Inorganic materials 0.000 claims description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 3
- 239000010452 phosphate Substances 0.000 claims description 3
- 239000000243 solution Substances 0.000 description 25
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 13
- 239000007788 liquid Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000003456 ion exchange resin Substances 0.000 description 6
- 229920003303 ion-exchange polymer Polymers 0.000 description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 5
- 229910001635 magnesium fluoride Inorganic materials 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 4
- 229910001634 calcium fluoride Inorganic materials 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000002367 phosphate rock Substances 0.000 description 4
- 239000011347 resin Substances 0.000 description 4
- 229920005989 resin Polymers 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 150000007513 acids Chemical class 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 235000011116 calcium hydroxide Nutrition 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 229910052925 anhydrite Inorganic materials 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 241000252233 Cyprinus carpio Species 0.000 description 1
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- 101100182219 Homo sapiens ALOX12 gene Proteins 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 102100031949 Polyunsaturated fatty acid lipoxygenase ALOX12 Human genes 0.000 description 1
- 229910004014 SiF4 Inorganic materials 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 150000002222 fluorine compounds Chemical class 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 239000013072 incoming material Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- ABTOQLMXBSRXSM-UHFFFAOYSA-N silicon tetrafluoride Chemical compound F[Si](F)(F)F ABTOQLMXBSRXSM-UHFFFAOYSA-N 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 229910000391 tricalcium phosphate Inorganic materials 0.000 description 1
Landscapes
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Description
【発明の詳細な説明】
本発明は、湿式リン酸製造方法に関し、特にリン鉱石中
に不純物として含まれるＭｇ分を除去して、高品質のリ
ン酸をを得る方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a wet method for producing phosphoric acid, and particularly to a method for obtaining high-quality phosphoric acid by removing Mg contained as an impurity in phosphate rock.
本発明者らは、先に、不純物が多く含まれるリン鉱石を
稀リン酸液で予備洗浄した後、通常の湿式リン酸製造工
程によってリン酸を製造し、Ｍｇ含有量の少ないリン酸
を得る方法を提案した（椿関昭５７−１００９０９号公
報参照）。本発明は上記の方法の延長上にある。上記の
方法で用いた使用済み稀リン酸液には、鉱石から溶出し
たＭｇ分が含まれている。よってこれを除去すれば同液
を再び鉱石洗浄用に使用できる。Ｍｇ分の除去方法とし
ては、強酸型イオン交換樹脂を用いる方法がある。しか
しこれにはつぎのような問題がある。１） 鉱石の洗浄
に伴って鉱石中の有機物に由釆したスラィムや微細な浮
遊物が発生し、これらがイオン交予期樹脂の層内に沈着
し、交去勢塔の閉塞をきたすことがある。The present inventors first pre-cleaned phosphate rock containing many impurities with a dilute phosphoric acid solution, and then produced phosphoric acid using a normal wet phosphoric acid production process to obtain phosphoric acid with a low Mg content. proposed a method (see Tsubaki Seki Publication No. 57-100909). The present invention is an extension of the method described above. The used dilute phosphoric acid solution used in the above method contains Mg eluted from the ore. Therefore, if this is removed, the same liquid can be used again for ore cleaning. As a method for removing Mg, there is a method using a strong acid type ion exchange resin. However, this has the following problems. 1) As the ore is washed, slime and fine suspended matter are generated due to the organic matter in the ore, and these may settle in the layer of ion exchange resin and cause blockage of the exchange tower.
２） 一般にＭｇの溶雛は、塩酸、硫酸、硝酸等の鉱酸
によってなされるが、このうち硫酸以外の酸は湿式リン
酸製造プラントにおいて入手容易でなく、コスト的には
合わない。2) Generally, melting of Mg is carried out using mineral acids such as hydrochloric acid, sulfuric acid, and nitric acid, but acids other than sulfuric acid are not easily available in wet phosphoric acid production plants and are not cost effective.
また硫酸以外の酸は、これが洗浄用の稀リン酸液の循環
に伴って、リン酸製造プラントにおける分解用酸に混入
すると、装置の腐食をきたすおそれがあるので、この点
からも使用を避けるべきである。さらに硫酸の場合には
つぎのような問題がある。鉱石の洗浄の結果、Ｍｇ分以
外にＣａ分も溶出し、これらは共にイオン交モ数樹脂に
吸着される。こうして両イオンを吸着したイオン交換樹
脂を硫酸で処理すると、ＭｇはＭが０４の形態で、Ｃａ
はＣａＳ０４の形態でそれぞれ樹脂から溶離される。こ
れら硫酸塩のうち、前者は溶解度が大きいので問題ない
が、後者は溶解度が４・さいために、樹脂の表面ないし
層内に一部析出し、そのため樹脂の吸着および溶鱗能力
の低下をきたす上に、交換塔の閉塞トラブルを生じる。
本発明者らは、上記のような点に鑑み、使用済み稀リン
酸液中に含まれるＭｇ分を、イオン交換樹脂によらない
で除去し、同液を鉱石洗浄用として循環使用し得る方法
につき研究を重ねたところ、同液中のＭｇを、少なくと
も酸性領域において汝災安するような溶解度の小さいＭ
ｇ化合物に変換すれば、同化合物を系外に取出すことに
よってＭｇを容易に除去することができるという知見を
得、またこのようなＭｇ化合物としてはＭず２が好適で
あるという知見を得て、本発明を完成した。Also, avoid using acids other than sulfuric acid as they may corrode the equipment if they mix with the decomposition acid in the phosphoric acid manufacturing plant as the dilute phosphoric acid solution for cleaning is circulated. Should. Furthermore, in the case of sulfuric acid, there are the following problems. As a result of washing the ore, in addition to Mg, Ca is also eluted, and both of these are adsorbed by the ion exchanger resin. When the ion exchange resin adsorbing both ions is treated with sulfuric acid, Mg is in the form of M04 and Ca
are respectively eluted from the resin in the form of CaS04. Among these sulfates, the former has a high solubility, so there is no problem, but the latter has a solubility of 4.5%, so it partially precipitates on the surface or within the layer of the resin, resulting in a decrease in the adsorption and scale ability of the resin. On top of that, problems with clogging of the exchange tower occur.
In view of the above points, the present inventors have developed a method in which the Mg content contained in the used dilute phosphoric acid solution can be removed without using an ion exchange resin, and the same solution can be reused for ore cleaning. After repeated research on Mg, it was found that Mg in the same solution has a low solubility, at least in the acidic region.
We obtained the knowledge that Mg can be easily removed by taking the same compound out of the system by converting it to a compound of Mg, and that Mz2 is suitable as such a Mg compound. , completed the invention.
なお、この明細書において割合を表わす「％はすべて重
量％を意味する。改行一字下げて本発明は、リン鉱石を
稀リン酸液で洗浄して鉱石中のＭｇ分を選択的に溶出さ
せ、洗浄後の鉱石を酸分解してＭｇ含有率の低いリン酸
を得るに当り、使用済み稀リン酸液にフッ化水素酸を加
えて液中のＭｇと反応させ、生成したＭが２の沈殿物を
液から分離除去し、得られたＭ熱除去後の稀リン酸液を
鉱石洗浄用に循環使用することを要旨とする湿式リン酸
製造法である。一般に、リン鉱石中にはフッ素が数％含
まれており、リン酸製造工程中にその約４０％がＨＦ、
ＳｉＦ４、日２ＳｊＦ６等の形態でガス状物質として放
散される。In addition, in this specification, all "%" which expresses a ratio means weight%. In order to obtain phosphoric acid with a low Mg content by acid decomposing the ore after washing, hydrofluoric acid is added to the used dilute phosphoric acid solution and reacted with the Mg in the solution. This is a wet phosphoric acid production method that involves separating and removing the precipitate from the liquid, and recycling the dilute phosphoric acid solution obtained after removing the M heat for cleaning ore.Generally, phosphate ore contains fluorine. It contains several percent of HF, and about 40% of it is converted into HF,
It is emitted as a gaseous substance in the form of SiF4, 2SjF6, etc.
そして、これら物質は作業環境保全、公害防止の点から
集気させて、アルカリ水溶液、消石灰水溶液等に吸収さ
れている。そのため湿式リン酸製造工程においては、フ
ッ素化合物の取扱いおよびその入手は特に問題とならな
い。本発明においてリン鉱石洗浄用の稀リン酸液の濃度
はＰ２４濃度で１〜２０％である。Ｐ２Ｑ濃度が上記範
囲に限定される理由は、１％未満では洗浄効果が低すぎ
て実用的でなく、また２０％を越えると、リン鉱石中の
Ｍｇ化合物○ａＭｇ（ＣＱ）２のみならず主成分である
Ｃａ３（Ｐ０４）２までも分解してしまうからある（上
記特開昭５７−１００９０９号公報２頁下右欄〜３頁上
左欄参照）。またフッ化水素酸の添加量は稀リン酸液中
に存在するＭｇおよびＣａの総量により決定され、好ま
しくはフッ化水素酸は化学量論量よりやや過剰に添加さ
れる。In order to preserve the working environment and prevent pollution, these substances are collected and absorbed into an aqueous alkaline solution, an aqueous slaked lime solution, and the like. Therefore, in the wet phosphoric acid production process, there are no particular problems in handling and obtaining fluorine compounds. In the present invention, the concentration of the dilute phosphoric acid solution for cleaning phosphate rock is 1 to 20% in terms of P24 concentration. The reason why the P2Q concentration is limited to the above range is that if it is less than 1%, the cleaning effect is too low to be practical, and if it exceeds 20%, not only the Mg compound ○aMg(CQ)2 in phosphate rock but also the main This is because even the component Ca3(P04)2 is decomposed (see the lower right column on page 2 to the upper left column on page 3 of the above-mentioned JP-A-57-100909). Further, the amount of hydrofluoric acid added is determined by the total amount of Mg and Ca present in the dilute phosphoric acid solution, and preferably the amount of hydrofluoric acid added is slightly in excess of the stoichiometric amount.
なお、本願発明者らが独自に測定したＭず２の溶解度曲
線を第１図に示す。Incidentally, the solubility curve of M22, which was independently measured by the inventors of the present application, is shown in FIG.
同図はＰ２０５２％の稀リン酸中に溶解状に存在するＭ
ｇＦ２の土を稀リン酸に対する重量％で示したものであ
って、同図からわかるようにＰ２０５２％の稀リン酸に
対するＭｇＦ２の溶解度は極めて低い。もっともこの溶
解度はＰ２Ｑ濃度により異なる。つぎに本発明の実施例
を示す。The figure shows M dissolved in P2052% dilute phosphoric acid.
The figure shows the soil of gF2 in weight percent relative to dilute phosphoric acid, and as can be seen from the figure, the solubility of MgF2 in dilute phosphoric acid with P2052% is extremely low. However, this solubility varies depending on the P2Q concentration. Next, examples of the present invention will be shown.
実施例
第２図に示す原料燐鉱石処理量５山／ｈの燐酸製造プラ
ントにおいて、Ｐ２Ｑ３０％とＭｇ１．０％を含む原料
鉱石がホッパ１に供給され、ついで、ホツパ１の底部か
ら一定流量でその下の洗浄槽２に流下する。Example In a phosphoric acid production plant with a throughput of raw phosphate ore of 5 piles/h as shown in FIG. It flows down into the cleaning tank 2 below.
同糟２にはＰ２０５３．０％とＭｇ０．０６％を含み稀
リン酸液が流量１４８ノｈで流入している。そして鉱石
は縄梓下に温度７０午０にて３時間稀リン酸液で洗浄さ
れて、スラリーとなされる。洗浄槽２の底部から出たス
ラリーは、固液分離装置３に導かれ、洗浄後の鉱石と使
用済み稀リン酸液に分離される。こうして洗浄された鉱
石にはＰ２０５１６．６５ｔ／ｈとＭ知．１４ｔ／ｈが
含まれており、洗浄前の鉱石中のＭｇ分の７２％が除去
されている。洗浄後の鉱石は、ついで通常の湿式燐酸製
造工程に送られる。A dilute phosphoric acid solution containing 3.0% P205 and 0.06% Mg was flowing into the same tank 2 at a flow rate of 148 h. The ore is then washed with a dilute phosphoric acid solution for 3 hours at a temperature of 70:00 under a rope to form a slurry. The slurry discharged from the bottom of the cleaning tank 2 is led to the solid-liquid separator 3, where it is separated into the cleaned ore and the used dilute phosphoric acid solution. The ore thus washed contains P20,516.65t/h and M. 14t/h was included, and 72% of the Mg content in the ore before cleaning was removed. The cleaned ore is then sent to a conventional wet phosphoric acid manufacturing process.
すなわち硫酸による分解工程４、晶析工程５、石こう炉
過工程６および濃縮工程７を経て、Ｍｇ含有率の低い高
品質燐酸（Ｐ２０５５４％）が製造される。他方、使用
済み稀リン酸液は、３時間の洗浄期間中に水分蒸発をき
たし、液量１２４ｔ／ｈ、Ｐ２Ｑ２．２％およびＭ鮒．
３６％の液となされ、間液分離装置３からその下の受器
８に流下する。That is, through a decomposition step 4 using sulfuric acid, a crystallization step 5, a gypsum furnace filtration step 6, and a concentration step 7, high quality phosphoric acid (P20554%) with a low Mg content is produced. On the other hand, the used dilute phosphoric acid solution caused water evaporation during the 3-hour washing period, and the liquid volume was 124 t/h, P2Q 2.2%, and M carp.
The liquid is reduced to 36% and flows down from the interliquid separator 3 to the receiver 8 below.
この液はついでＭｇ回収工程に送られる。すなわち、同
液は、４６％フッ化水素液１．６の／ｈが送入されてい
る第１反応槽９に送入される。そして両送入物が温度７
０ｑｏにて渡梓下に混合され、フッ化水素酸と使用済み
稀リン酸液中のＭｇ分とが次式（１）に示す如く反応す
る。ＭｇＨＰ０４十班Ｆ→Ｍず２十日３Ｐ０４ ・・・
・・・（１）この反応により使用済み稀リン酸液中のＭ
ｇ分の８０％がＭｇＦ２として沈殿する。This liquid is then sent to the Mg recovery step. That is, the same liquid is sent to the first reaction tank 9 into which 1.6/h of 46% hydrogen fluoride solution is fed. And both incoming materials have a temperature of 7.
They are mixed together at 0 qo under pressure, and the hydrofluoric acid and the Mg content in the used dilute phosphoric acid solution react as shown in the following formula (1). MgHP04 10th group F → Mzu 20th 3P04...
...(1) Through this reaction, M in the used dilute phosphoric acid solution
80% of the g fraction precipitates as MgF2.
反応混合物よりなるスラリ‐は反応槽９から第１炉過機
１０に導かれて、ここでＭｇＦ２の沈殿物０．９２／ｈ
が分離される。そして得られた炉過液にはＰ２Ｑ２．７
３、Ｍｇ０．０軌およびＨＦＯ．１５ｔが含まれている
。この液はついで第２反応糟１ １‘こ送られる。同糟
１ １には消石灰の粉末ないしはスラリーが投入されて
おり、これと炉液中のＨＦが次式（０）により反応し、
ＣａＦ２が沈殿する。Ｃａ（ＯＨ）２十がＦ→ＣａＦ２
十２ＬＯ ……（０）消石灰の投入量はＨＦに当量で
よい。The slurry consisting of the reaction mixture is led from the reaction tank 9 to the first filter 10, where a precipitate of MgF2 of 0.92/h is removed.
are separated. The obtained filtrate contains P2Q2.7
3, Mg0.0 orbital and HFO. Contains 15t. This liquid is then sent to the second reaction vessel 11'. Slaked lime powder or slurry is added to 1, and this reacts with HF in the furnace liquid according to the following formula (0).
CaF2 precipitates. Ca(OH)20 is F → CaF2
12LO... (0) The amount of slaked lime to be added may be equivalent to HF.
あまり過剰になると、炉液中の隣分を沈殿するので、好
ましくない。反応混合物よりなるスラリーは第２炉過磯
１２に導かれて、ここでＣａＦ２の沈殿物０．２軌／ｈ
が分離される。そして得られた炉液には、前記緑式燐酸
製造工程において得られた製品燐酸の一部３０３／ｈが
加えられ、さらに全量が１４８／ｈとなるように水が加
えられる。こうして得られた稀リン酸液は前記洗浄槽２
に送られ、洗浄液として循環使用せられる。第１および
第２炉過機１０，１２において分離されたＭｇＦ２およ
びＣａＦ２の各沈殿物は、そのまま創生物として取得し
てもよいが、これらを混合してＨＦ回収装置１３に装入
し、これに濃硫酸を加えて加熱することにより、次式（
ｍ）（Ｗ）で示す如く、ＨＦを回収することもできる。Too much excess is not preferable because it precipitates the neighboring fraction in the furnace solution. The slurry consisting of the reaction mixture is led to the second furnace sieve 12, where it is deposited with a precipitate of CaF2 of 0.2 km/h.
are separated. A portion of the product phosphoric acid obtained in the green phosphoric acid manufacturing process, 303/h, is added to the obtained furnace liquid, and water is further added so that the total amount becomes 148/h. The dilute phosphoric acid solution thus obtained is then used in the cleaning tank 2.
The water is sent to the water tank and recycled as a cleaning solution. The MgF2 and CaF2 precipitates separated in the first and second furnace filtration machines 10, 12 may be obtained as they are as created substances, but they are mixed and charged into the HF recovery device 13. By adding concentrated sulfuric acid to and heating it, the following formula (
m) HF can also be recovered as shown in (W).
ＮねＦ２十日２Ｓ０４一Ｍ史０４十がＦ ・・・・・
・（ｍ）ＣａＦ２十ＱＳ０４→ＣａＳ０４十２ＨＦ
・・・・・・（Ｗ）こうして発生させたＨＦを水に吸
収させてフツ化水素酸を得、これを前記第１反応槽９に
供給することができる。Nne F2 10th 2S04-M history 040 is F...
・(m)CaF20QS04→CaS0412HF
(W) The HF thus generated can be absorbed into water to obtain hydrofluoric acid, which can be supplied to the first reaction tank 9.
また式（ｍ）（Ｗ）の反応により副生したＭｇＳ０４と
ＣａＳ０４は、前者の水に対する溶解度が後者のそれに
比べて大きいので、混合物に水を添加することにより、
容易に分離することができる。本発明による湿式リン酸
製造法は以上のとおり構成されており、鉱石の洗浄に用
いた使用済み稀リン酸液にフッ化水素酸を加えて液中の
Ｍｇと反応させ、生成したＭが２の沈殿物を分離除去す
るので、イオン交換樹脂を使用しなくても液中のＭｇを
容易に除去することができ、したがってイオン交換樹脂
の使用に伴う多くの問題は全く生じる余地がない。また
本発明による方法は、通常の湿式リン酸製造工程で使用
する薬品以外に特に薬品を必要とせず、操作を連続的に
行なうことができる。Furthermore, since the solubility of the former in water is greater than that of the latter, MgS04 and CaS04, which are by-produced by the reaction of formulas (m) and (W), can be obtained by adding water to the mixture.
Can be easily separated. The wet phosphoric acid manufacturing method according to the present invention is configured as described above, in which hydrofluoric acid is added to a used dilute phosphoric acid solution used for cleaning ores and reacted with Mg in the solution, and the generated M is Since the precipitate is separated and removed, Mg in the liquid can be easily removed without using an ion exchange resin, and therefore many problems associated with the use of ion exchange resins do not arise at all. Further, the method according to the present invention does not require any particular chemicals other than those used in the normal wet phosphoric acid production process, and can be operated continuously.
第１図はＭｇＦ２の稀リン酸液に対する熔解度を示すグ
ラフ、第２図は本発明の実施例を示す工程図である。
第１図
第２図FIG. 1 is a graph showing the solubility of MgF2 in dilute phosphoric acid solution, and FIG. 2 is a process diagram showing an example of the present invention. Figure 1 Figure 2
Claims (1)
液で洗浄して鉱石中のＭｇ分を選択的に溶出させ、洗浄
後の鉱石を酸分解してＭｇ含有率の低いリン酸を得るに
当り、使用済み稀リン酸液にフツ化水素酸を加えて液中
のＭｇと反応させ、生成したＭｇＦ＿２の沈殿物を液か
ら分離除去し、得られたＭｇ除去後の稀リン酸液を鉱石
洗浄用に循環使用することを特徴とする湿式リン酸製造
法。1. To selectively elute the Mg content in the ore by washing phosphate ore with a dilute phosphoric acid solution with a P_2O_5 concentration of 1 to 20%, and then acid decomposing the ore after washing to obtain phosphoric acid with a low Mg content. Hydrofluoric acid is added to the used dilute phosphoric acid solution to react with Mg in the solution, and the generated MgF_2 precipitate is separated and removed from the solution.The resulting dilute phosphoric acid solution after Mg removal is used as ore. A wet phosphoric acid production method characterized by circulating phosphoric acid for cleaning.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5210481A JPS6018606B2 (en) | 1981-04-06 | 1981-04-06 | Wet phosphoric acid manufacturing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5210481A JPS6018606B2 (en) | 1981-04-06 | 1981-04-06 | Wet phosphoric acid manufacturing method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57166302A JPS57166302A (en) | 1982-10-13 |
| JPS6018606B2 true JPS6018606B2 (en) | 1985-05-11 |
Family
ID=12905536
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5210481A Expired JPS6018606B2 (en) | 1981-04-06 | 1981-04-06 | Wet phosphoric acid manufacturing method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6018606B2 (en) |
-
1981
- 1981-04-06 JP JP5210481A patent/JPS6018606B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57166302A (en) | 1982-10-13 |
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