JPH02233503A - Purification of hydrochloric acid - Google Patents
Purification of hydrochloric acidInfo
- Publication number
- JPH02233503A JPH02233503A JP5444689A JP5444689A JPH02233503A JP H02233503 A JPH02233503 A JP H02233503A JP 5444689 A JP5444689 A JP 5444689A JP 5444689 A JP5444689 A JP 5444689A JP H02233503 A JPH02233503 A JP H02233503A
- Authority
- JP
- Japan
- Prior art keywords
- hydrochloric acid
- activated carbon
- reducing agent
- anion exchange
- free
- 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
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000000746 purification Methods 0.000 title abstract 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 62
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 28
- 229910052742 iron Inorganic materials 0.000 claims abstract description 25
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 18
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 15
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 claims abstract description 8
- WTDHULULXKLSOZ-UHFFFAOYSA-N Hydroxylamine hydrochloride Chemical compound Cl.ON WTDHULULXKLSOZ-UHFFFAOYSA-N 0.000 claims abstract description 6
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000004202 carbamide Substances 0.000 claims abstract description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 45
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 26
- 239000000460 chlorine Substances 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 12
- 230000004913 activation Effects 0.000 claims description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 4
- 238000006298 dechlorination reaction Methods 0.000 claims description 4
- 239000011347 resin Substances 0.000 claims description 3
- 229920005989 resin Polymers 0.000 claims description 3
- 238000005349 anion exchange Methods 0.000 claims 1
- 150000002500 ions Chemical class 0.000 abstract description 2
- 239000000203 mixture Substances 0.000 abstract description 2
- 239000002253 acid Substances 0.000 abstract 2
- 230000003247 decreasing effect Effects 0.000 abstract 2
- 230000000382 dechlorinating effect Effects 0.000 abstract 1
- 238000001914 filtration Methods 0.000 abstract 1
- 150000003839 salts Chemical class 0.000 description 7
- 235000013162 Cocos nucifera Nutrition 0.000 description 2
- 244000060011 Cocos nucifera Species 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical class [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical group [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 1
- 241000700159 Rattus Species 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 229920001429 chelating resin Polymers 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004040 coloring Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229960002089 ferrous chloride Drugs 0.000 description 1
- 229910052733 gallium Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 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
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0718—Purification ; Separation of hydrogen chloride by adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0718—Purification ; Separation of hydrogen chloride by adsorption
- C01B7/0725—Purification ; Separation of hydrogen chloride by adsorption by active carbon
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は遊離塩素及び鉄分を含何する塩酸の精製方法に
関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Field of Application] The present invention relates to a method for purifying hydrochloric acid containing free chlorine and iron.
［従来の技術とその課題］
金属の洗浄液に使用ざれた塩酸廃液は大部分塩化第一鉄
として鉄分を含有している。このような塩鼠を精製する
場合、まず塩素ガスで第一鉄塩を第二鉄塩に酸化する。[Prior art and its problems] Hydrochloric acid waste used as a metal cleaning solution contains iron mostly as ferrous chloride. When refining such salt rats, first ferrous salts are oxidized to ferric salts using chlorine gas.
また有機化合物製造時に副生ずる塩酸中にも遊離塩素及
び第二鉄塩を含む場合が多い。第二銖塩でおれば強塩基
性陰イオン交換樹脂例えばα型陰イオン交換樹脂で除去
できるので、陰イオン交換樹脂保護のために、活性炭で
′ｔ１離塩素を除去した後に樹脂塔に送る方法が行われ
ている。すなわち活性炭による遊離塩素除去の目的は、
陰イオン交換樹脂が遊離塩素により酸化され交換容量が
低下するのを防ぐことや塩酸の着色を防ぐことであるが
、このような活性炭による脱塩素処理を行った塩酸は鉄
分が十分除去できないという問題点がめった。Furthermore, hydrochloric acid produced as a by-product during the production of organic compounds often contains free chlorine and ferric salts. If it is a secondary salt, it can be removed with a strongly basic anion exchange resin, such as an α-type anion exchange resin, so in order to protect the anion exchange resin, 't1 free chlorine is removed with activated carbon and then sent to the resin column. is being carried out. In other words, the purpose of free chlorine removal using activated carbon is
The aim is to prevent the anion exchange resin from being oxidized by free chlorine and reduce its exchange capacity, and to prevent the coloring of hydrochloric acid, but the problem is that iron cannot be removed sufficiently from hydrochloric acid that has been dechlorinated using activated carbon. I scored very few points.
（課題を解決するための手段〕
本発明者らは以上の問題点を解決するため、鋭意検討を
行った結果、濃度１５重母％以上の塩酸に含まれる鉄分
は第二鉄であればＦｅ（Ｊａ″″イオンとして存在する
ので強塩基性陰イオン交換樹脂に吸着するが、通常の活
性炭と接触すると活性炭の還元力で一部が第一鉄となり
、陰イオン交換樹脂で鉄分を完全に除去できなくなるこ
とが判明した。(Means for Solving the Problems) In order to solve the above problems, the present inventors conducted intensive studies and found that if the iron contained in hydrochloric acid with a concentration of 15% or more is ferric iron, Fe (Since it exists as Ja″″ ions, it is adsorbed by the strongly basic anion exchange resin, but when it comes into contact with ordinary activated carbon, some of it becomes ferrous iron due to the reducing power of the activated carbon, and the iron content is completely removed by the anion exchange resin. It turned out that it would not be possible.
本発明は以上の知見に基いて完成ざれたものであってす
なわち、遊離塩素及び鉄分を含有する塩敢に、還元剤を
添加するか又は比表面積５００尻／Ｑ以下の低賦活活性
炭を接触させて脱塩素処理を行った後、強塩基性陰イオ
ン交換樹脂と接触させることを特徴とする塩薗の精製方
法である。また還元剤を添加後、上記低試活活性炭を接
触させてもよい。The present invention has been completed based on the above findings, namely, by adding a reducing agent or contacting low-activation activated carbon with a specific surface area of 500 sides/Q or less to a salt containing free chlorine and iron. This is a method for purifying shiokon, which is characterized by carrying out dechlorination treatment using chlorine and then contacting it with a strongly basic anion exchange resin. Further, after adding the reducing agent, the low test activated carbon may be brought into contact with the reducing agent.
本発明において用いられる活性炭は比表面積ＳＯＯボ／
ｇ以下２好ましくは３００尻／ｇ以下の低斌活活性炭で
あり、通常の平均約１０００ＴＩｉ／ｇの比表面積を有
する活性炭とは異なるものである。このような低賦活活
性炭は炭化温度５００〜６００℃，水蒸気による賦活温
度８５０〜１０００℃にて通常の活性炭より例えば賦活
時間を短縮する等の方法により比表面積の増加を加減し
て製造することができる。また水蒸気賦活法に特に限定
ざれず例えば亜鉛を使用する方法等他の斌活法によって
も製造し得る。The activated carbon used in the present invention has a specific surface area of SOO/
The activated carbon has a low density of less than 2 g, preferably less than 300 TIi/g, and is different from ordinary activated carbon having a specific surface area of about 1000 TIi/g on average. Such low-activation activated carbon can be produced at a carbonization temperature of 500 to 600°C and an activation temperature of 850 to 1000°C with steam, by adjusting the increase in specific surface area by, for example, shortening the activation time compared to ordinary activated carbon. can. Further, it is not particularly limited to the steam activation method, and can also be produced by other activation methods such as a method using zinc.
この低賦活活性炭と塩酸との接触方法は特に限定される
ことなく、例えば低賦活活性炭の充填層に塩酸を通過さ
せてもよく、塩酸と低賦活活性炭とを十分混合した後枦
過してもよい。通常、塩酸中の遊離塩素が約１０ｐｐｍ
程度であれば、このような低賦活活性炭により１ ｐｐ
ｍ以下にまで脱塩素することができ、強塩基性陰イオン
交換樹脂を損傷することがない。The method of contacting the low-activation activated carbon with hydrochloric acid is not particularly limited; for example, the hydrochloric acid may be passed through a packed bed of low-activation activated carbon, or the hydrochloric acid and the low-activation activated carbon may be sufficiently mixed and then passed through. good. Usually, free chlorine in hydrochloric acid is about 10 ppm
If the level of
It can be dechlorinated to less than m and does not damage the strongly basic anion exchange resin.
また塩酸中の鉄分は第一鉄塩にまで遠元されず第二鉄塩
の形態を保っているので強塩基性陰イオン交換樹脂によ
り効率のよい脱鉄を行うことができる。Furthermore, since the iron content in hydrochloric acid is not dissipated into ferrous salt and remains in the form of ferric salt, it is possible to efficiently remove iron using a strongly basic anion exchange resin.
本発明において使用ざれる還元剤はヒドラジン、塩酸ヒ
ドロキシルアミン，尿素，過酸化水素の少なくとも１種
が好ましく、このような還元剤を用いることにより塩酸
中への不純物の混入を避けることができる。還元剤の添
加母は遊離塩素に対し化学量論的量もしくはそれ以下で
よく、還元剤が過剰にならないよう注意する。還元剤の
添加母は遊離塩素自動分析計で測定しながら調節すれば
よい。The reducing agent used in the present invention is preferably at least one of hydrazine, hydroxylamine hydrochloride, urea, and hydrogen peroxide, and by using such a reducing agent, it is possible to avoid contamination of the hydrochloric acid with impurities. The reducing agent may be added in a stoichiometric amount or less relative to free chlorine, and care must be taken not to add too much reducing agent. The amount of reducing agent added may be adjusted while measuring with an automatic free chlorine analyzer.
脱塩ｌＡ処理は還元剤の添加又は低賦活活性炭のみによ
って行うことも可能であるが、被精製塩酸中の遊ｍ塩素
濃度が１０ｐｐｍを越える場合は、必らかじめ還元剤を
添加して１０ｐｐｍ程度にまで遊離塩素を除去した後、
ざらに低賦活活性炭により脱塩素処理を行う方法が工業
的に好ましい。このように還元剤の添加により大部分の
遊離塩素を還元し、残存する少量の遊離塩素を低賦活活
性炭により除去すれば、活性炭の負荷を小にしその寿命
を長くすることができる。Desalination 1A treatment can be carried out by adding a reducing agent or by using only low activated carbon, but if the free m chlorine concentration in the hydrochloric acid to be purified exceeds 10 ppm, be sure to add a reducing agent in advance to reduce the concentration to 10 ppm. After removing free chlorine to a certain extent,
A method in which dechlorination is carried out using low-activation activated carbon is industrially preferred. In this way, by reducing most of the free chlorine by adding a reducing agent and removing the small amount of remaining free chlorine using low activation activated carbon, it is possible to reduce the load on the activated carbon and extend its life.
実施例１
直径２５ｍｍ，高さ５００ｍｍのガラムカラムに、あら
かじめ塩酸で洗浄した低賦活活性炭（ヤシ殻炭を水蒸気
試活，比表面積１３０Ｍ／（Ｊ ．粒度１２〜４０メッ
シュ》を１５０威充填したく第１塔）。また同形のカラ
ムに強塩基性陰イオン交換樹脂（商品名アンバーライト
Ｉ ＲＡ−４００ ，ロームアンドハース社製＞ １
５０ｄを充填した（第２塔）。遊離塩素３２ｐｐｍ，鉄
分４２ｐｐｍを含む濃度２７％の塩酸を２８℃にて第１
塔，第２塔の順にそれぞれ空間速度（ Ｓ Ｖ ）
８ｈｒｌで下向流で通過させたところ、第２塔出口の塩
酸中の遊離塩素０． ３ｐｐｍ，鉄分は０．２ｐｐｍで
あった。Example 1 A gallium column with a diameter of 25 mm and a height of 500 mm was filled with 150 pieces of low activation activated carbon (coconut shell charcoal, steam tested, specific surface area: 130 M/(J. particle size: 12 to 40 mesh)) which had been washed with hydrochloric acid in advance. 1 column).In addition, a strongly basic anion exchange resin (trade name Amberlite I RA-400, manufactured by Rohm and Haas Co., Ltd.> 1 column) was used in the same column.
50d (second column). Hydrochloric acid with a concentration of 27% containing 32 ppm of free chlorine and 42 ppm of iron was first added at 28°C.
space velocity (SV) in the order of the column and the second column, respectively.
When it was passed in a downward flow at 8 hrl, free chlorine in the hydrochloric acid at the outlet of the second column was 0. The iron content was 3 ppm, and the iron content was 0.2 ppm.
比較例１
実施例１の低賦活活性炭の代りに、あらかじめ塩酸で洗
浄した粒状ヤシ殻活性炭（商品名 白鷺Ｗ：武田薬品工
業（株）！！！）を使用し他は同様にして、同じ塩酸の
精製を行ったところ、第２塔出口の塩酸中の遊離塩素０
． ２ｐＩ）ｍ，鉄分４．５ｐｐｍであった。この活性
炭の比表面積を自動ボロシメーターオートポア９２００
（ （株）島津製作所製）にて測定したところ１１０
０ＴＩｉ／ｆｊであった。Comparative Example 1 In place of the low activation activated carbon of Example 1, granular coconut shell activated carbon (trade name: Shirasagi W: Takeda Pharmaceutical Company Ltd.!!!) which had been washed with hydrochloric acid in advance was used, and the other conditions were the same, and the same hydrochloric acid was used. When purified, 0 free chlorine was found in the hydrochloric acid at the outlet of the second column.
．． The iron content was 2pI)m, and the iron content was 4.5ppm. The specific surface area of this activated carbon was measured using an automatic borosimeter Autopore 9200.
(Manufactured by Shimadzu Corporation): 110
It was 0TIi/fj.
実施例２
遊離塩素８５ｐｐｍ，鉄分３６ｐｐｍを含む濃度３２％
の塩酸１ｇに１５℃の室温にて濃度１％のヒドラジン水
溶液６ｄを添加し同温度にて１０分間放置した。Example 2 Concentration 32% including free chlorine 85 ppm and iron 36 ppm
To 1 g of hydrochloric acid was added 6 d of a 1% aqueous hydrazine solution at a room temperature of 15° C., and the mixture was left at the same temperature for 10 minutes.
この塩酸の遊離塩素濃度は０． ８ｐｐｍでおった。次
いでこの塩酸を実施例１と同様の強塩基性陰イオン交換
樹脂充填力ラムに空間速度（ＳＶ）１０ｈｒ″″１で下
向流で通過させたところ樹脂筒出口の塩酸中の遊離塩素
０． ｌｉ）ｐｍ，鉄分０． ８１）ｐｍテあった。The free chlorine concentration of this hydrochloric acid is 0. It was 8 ppm. Next, this hydrochloric acid was passed through a strongly basic anion exchange resin packing force ram similar to that in Example 1 in a downward flow at a space velocity (SV) of 10 hr''1, and free chlorine in the hydrochloric acid at the outlet of the resin cylinder was 0.0. li) pm, iron content 0. 81) There was a pm te.
実施例３
遊！Ｉｉ塩素１ｏａｐｐｍ．鉄分３０ｐｐｍを含む濃度
３５％の塩酸りに、１５℃にて濃度１％の尿素水溶液５
ｄを添加し同温度にて１５分間放置した。この塩酸中の
遊離塩素は１３ｐｐｍとなった。次いであらかじめ塩薗
で洗浄した低賦活活性炭（比表面積２７０ｍ／０，粒度
１２Ｘ４０メッシュ）１５０威を充填した第１塔，及び
実施例１と同じ第２塔を空間速度（ＳＶ）７ｈｒ″″１
で下向流で通過させたところ、第２塔出口の塩酸中の遊
離塩素０．１ｐｐｌｎ，鉄分０．５ｐｐｍでおった。Example 3 Play! Ii Chlorine 1oappm. Add a 1% aqueous urea solution 5 to 35% hydrochloric acid containing 30 ppm iron at 15°C.
d was added and left at the same temperature for 15 minutes. Free chlorine in this hydrochloric acid was 13 ppm. Next, the first column filled with 150 liters of low-activation activated carbon (specific surface area 270 m/0, particle size 12 x 40 mesh) which had been washed with salt in advance, and the second column which was the same as in Example 1, were heated at a space velocity (SV) of 7 hr''1.
When the hydrochloric acid was passed through in a downward flow, the free chlorine and iron content in the hydrochloric acid at the outlet of the second column were 0.1 ppln and 0.5 ppm, respectively.
［発明の効果］
本発明方法によれば、塩酸中の遊離塩素及び鉄分を除去
する際、従来の活性炭にかえて、還元剤又は低試活活性
炭を使用し又はこれらを併用して脱塩素処理を行うこと
により、塩酸中の鉄分を第一鉄塩にまで還元することな
く強塩基性陰イオン交換樹脂による効率のよい脱鉄を行
うことができるので工業的に有用である。[Effects of the Invention] According to the method of the present invention, when removing free chlorine and iron from hydrochloric acid, dechlorination treatment is carried out by using a reducing agent or low-test activated carbon, or in combination with these, in place of conventional activated carbon. By carrying out this process, iron removal can be carried out efficiently using a strongly basic anion exchange resin without reducing the iron content in hydrochloric acid to ferrous salt, which is industrially useful.
Claims (3)
加するか又は比表面積５００ｍ＾２／ｇ以下の低賦活活
性炭を接触させて脱塩素処理を行つた後、強塩基性陰イ
オン交換樹脂と接触させることを特徴とする塩酸の精製
方法。(1) Hydrochloric acid containing free chlorine and iron is dechlorinated by adding a reducing agent or brought into contact with low activation activated carbon with a specific surface area of 500 m^2/g or less, followed by strong basic anion exchange. A method for purifying hydrochloric acid, which comprises bringing it into contact with a resin.
後、比表面積５００ｍ＾２／ｇ以下の低賦活活性炭と接
触させて脱塩素処理を行った後、強塩基性陰イオン交換
樹脂と接触させることを特徴とする塩酸の精製方法。(2) After adding a reducing agent to hydrochloric acid containing free chlorine and iron, it is brought into contact with low activation activated carbon with a specific surface area of 500 m^2/g or less for dechlorination treatment, and then treated with a strong basic anion exchange resin. A method for purifying hydrochloric acid, which comprises bringing it into contact.
尿素、過酸化水素より選ばれた少なくとも１種である請
求項１もしくは請求項２に記載の塩酸の精製方法。(3) The reducing agent is hydrazine, hydroxylamine hydrochloride,
The method for purifying hydrochloric acid according to claim 1 or 2, wherein at least one selected from urea and hydrogen peroxide is used.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5444689A JPH02233503A (en) | 1989-03-06 | 1989-03-06 | Purification of hydrochloric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5444689A JPH02233503A (en) | 1989-03-06 | 1989-03-06 | Purification of hydrochloric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02233503A true JPH02233503A (en) | 1990-09-17 |
| JPH0569761B2 JPH0569761B2 (en) | 1993-10-01 |
Family
ID=12970929
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5444689A Granted JPH02233503A (en) | 1989-03-06 | 1989-03-06 | Purification of hydrochloric acid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02233503A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5330735A (en) * | 1993-01-21 | 1994-07-19 | Dow Corning Corporation | Purification of hydrochloric acid |
| EP0618170A1 (en) * | 1993-03-31 | 1994-10-05 | Basf Corporation | Process for producing reagent grade hydrochloric acid from the manufacture of organic isocyanates |
| US5426944A (en) * | 1993-08-31 | 1995-06-27 | American Air Liquide, Inc. | Chemical purification for semiconductor processing by partial condensation |
| US6290927B1 (en) * | 1994-06-03 | 2001-09-18 | Norsk Hydro A/S | Method for the removal of unwanted color from hydrochloric acid |
| CN109553070A (en) * | 2018-12-17 | 2019-04-02 | 江苏诺斯特拉环保科技有限公司 | Waste hydrochloric acid recycles method of disposal |
| CN110436416A (en) * | 2019-08-19 | 2019-11-12 | 四川金山制药有限公司 | A kind of technique preparing electronic grade hydrochloric acid except free chlorine |
| CN110562922A (en) * | 2019-08-19 | 2019-12-13 | 四川金山制药有限公司 | Process for producing atomic fluorescent grade hydrochloric acid by gasification method |
| CN111960384A (en) * | 2020-08-26 | 2020-11-20 | 浙江凯圣氟化学有限公司 | Method for removing free chlorine in hydrochloric acid |
| CN114180525A (en) * | 2021-12-30 | 2022-03-15 | 南通醋酸化工股份有限公司 | Separation method of hydrogen chloride/dichloromethane in synthesis of 4-chloroacetoacetic acid ethyl ester |
-
1989
- 1989-03-06 JP JP5444689A patent/JPH02233503A/en active Granted
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5330735A (en) * | 1993-01-21 | 1994-07-19 | Dow Corning Corporation | Purification of hydrochloric acid |
| EP0618170A1 (en) * | 1993-03-31 | 1994-10-05 | Basf Corporation | Process for producing reagent grade hydrochloric acid from the manufacture of organic isocyanates |
| US5426944A (en) * | 1993-08-31 | 1995-06-27 | American Air Liquide, Inc. | Chemical purification for semiconductor processing by partial condensation |
| US6290927B1 (en) * | 1994-06-03 | 2001-09-18 | Norsk Hydro A/S | Method for the removal of unwanted color from hydrochloric acid |
| CN109553070A (en) * | 2018-12-17 | 2019-04-02 | 江苏诺斯特拉环保科技有限公司 | Waste hydrochloric acid recycles method of disposal |
| CN110436416A (en) * | 2019-08-19 | 2019-11-12 | 四川金山制药有限公司 | A kind of technique preparing electronic grade hydrochloric acid except free chlorine |
| CN110562922A (en) * | 2019-08-19 | 2019-12-13 | 四川金山制药有限公司 | Process for producing atomic fluorescent grade hydrochloric acid by gasification method |
| CN111960384A (en) * | 2020-08-26 | 2020-11-20 | 浙江凯圣氟化学有限公司 | Method for removing free chlorine in hydrochloric acid |
| CN111960384B (en) * | 2020-08-26 | 2022-04-12 | 浙江凯圣氟化学有限公司 | Method for removing free chlorine in hydrochloric acid |
| CN114180525A (en) * | 2021-12-30 | 2022-03-15 | 南通醋酸化工股份有限公司 | Separation method of hydrogen chloride/dichloromethane in synthesis of 4-chloroacetoacetic acid ethyl ester |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0569761B2 (en) | 1993-10-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR100195324B1 (en) | Heavy metal cation recovering agent including a silicate or aluminosilicate type compound and a carbonate type compound | |
| EP0196173B1 (en) | Removal of iodide compounds from non-aqueous organic media | |
| JPS605215A (en) | Filter material for purifying water | |
| JPH07308538A (en) | Cleaner for harmful gas | |
| JPH02233503A (en) | Purification of hydrochloric acid | |
| JP4247633B2 (en) | Adsorbent | |
| US2402959A (en) | Removal of boron from boron polluted substances | |
| JPH08109008A (en) | Purification of halogen gas | |
| JP3603701B2 (en) | Method and apparatus for treating peracetic acid-containing wastewater | |
| JPH0639277A (en) | Active paddy husk and water purifying method using same | |
| JPH0350114A (en) | Purification of aqueous solution of alkali metal chloride | |
| EP1181248A1 (en) | Non-caking sodium chloride crystals, a process to make them, and their use in an electrolysis process | |
| JP6719214B2 (en) | Oxo acid ion adsorbent | |
| JPH07155608A (en) | Production of high capacity carbon material | |
| US3262876A (en) | Cleaning ion exchange resins | |
| US4637922A (en) | Method for removing organic materials from a wet process phosphoric acid | |
| JP4041202B2 (en) | Sr ion adsorbent, method for producing the same, and method for treating Sr ion-containing water using the same | |
| JP2007237169A (en) | Adsorbent for treating liquid phase and its manufacturing method | |
| JP3680867B2 (en) | Method for purifying hydrogen peroxide water | |
| JP2006255628A (en) | Dephosphorizationagent and method for removing phosphoric acid ion | |
| JPH049598B2 (en) | ||
| JPH0218906B2 (en) | ||
| JP4392493B2 (en) | Method for removing and recovering phosphorus | |
| US3410659A (en) | Purification and stabilization of hydrogen peroxide | |
| JPH0455312A (en) | Method for removing metal in caustic alkali solution |