JP2005041707A - Method of regenerating arsenic-containing mineral acid - Google Patents
Method of regenerating arsenic-containing mineral acid Download PDFInfo
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- JP2005041707A JP2005041707A JP2003200218A JP2003200218A JP2005041707A JP 2005041707 A JP2005041707 A JP 2005041707A JP 2003200218 A JP2003200218 A JP 2003200218A JP 2003200218 A JP2003200218 A JP 2003200218A JP 2005041707 A JP2005041707 A JP 2005041707A
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- 239000002253 acid Substances 0.000 title claims abstract description 105
- 229910052500 inorganic mineral Inorganic materials 0.000 title claims abstract description 101
- 239000011707 mineral Substances 0.000 title claims abstract description 101
- 229910052785 arsenic Inorganic materials 0.000 title claims abstract description 97
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 title claims abstract description 97
- 238000000034 method Methods 0.000 title claims abstract description 34
- 230000001172 regenerating effect Effects 0.000 title claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 51
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims abstract description 41
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 38
- 239000007787 solid Substances 0.000 claims abstract description 35
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 22
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 20
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 20
- 239000011593 sulfur Substances 0.000 claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 15
- CUGMJFZCCDSABL-UHFFFAOYSA-N arsenic(3+);trisulfide Chemical compound [S-2].[S-2].[S-2].[As+3].[As+3] CUGMJFZCCDSABL-UHFFFAOYSA-N 0.000 claims abstract 8
- 238000011282 treatment Methods 0.000 claims description 28
- 238000005273 aeration Methods 0.000 claims description 9
- OMZSGWSJDCOLKM-UHFFFAOYSA-N copper(II) sulfide Chemical compound [S-2].[Cu+2] OMZSGWSJDCOLKM-UHFFFAOYSA-N 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 3
- 238000007254 oxidation reaction Methods 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 34
- XPDICGYEJXYUDW-UHFFFAOYSA-N tetraarsenic tetrasulfide Chemical compound S1[As]2S[As]3[As]1S[As]2S3 XPDICGYEJXYUDW-UHFFFAOYSA-N 0.000 description 20
- 239000000706 filtrate Substances 0.000 description 8
- 239000002699 waste material Substances 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 239000002002 slurry Substances 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 150000007513 acids Chemical class 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 238000005259 measurement Methods 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- RPAJSBKBKSSMLJ-DFWYDOINSA-N (2s)-2-aminopentanedioic acid;hydrochloride Chemical class Cl.OC(=O)[C@@H](N)CCC(O)=O RPAJSBKBKSSMLJ-DFWYDOINSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- -1 iron salt compound Chemical class 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 2
- 229910052979 sodium sulfide Inorganic materials 0.000 description 2
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- DJHGAFSJWGLOIV-UHFFFAOYSA-N Arsenic acid Chemical compound O[As](O)(O)=O DJHGAFSJWGLOIV-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 229940000488 arsenic acid Drugs 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle 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
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
Abstract
Description
【０００１】
【発明の属する技術分野】
本発明は、ヒ素含有鉱酸の再生方法に関し、詳しくは、１０００ｐｐｍ以下、特に、５００ｐｐｍ以下の希薄濃度のヒ素を含有する鉱酸からヒ素を固形化して除去し、鉱酸を再利用可能な状態に再生する方法に関する。
【０００２】
【従来の技術】
数千〜数万ｐｐｍのヒ素を含有する鉱酸、例えば硫酸からヒ素を１０ｐｐｍ以下に除去して鉱酸を再生する方法として、ヒ素含有硫酸に水溶性硫化物や硫化水素ガスを添加し、硫酸中のヒ素を硫化ヒ素として不溶化させた後、これを硫酸中から固液分離する方法が一般的に行われている。
【０００３】
しかし、ヒ素濃度が１０００ｐｐｍ以下の希薄ヒ素を含有する鉱酸の場合は、硫化ヒ素の結晶生成が極めて遅くなり、鉱酸中のヒ素を一定濃度以下に除去するために数日間という比較的長時間を要し、実用性に難点がある。また、鉱酸中のヒ素を一定濃度以下にまで除去した後も、鉱酸中に残存するヒ素と硫化物とが反応し、沈降しにくい微細な硫化ヒ素が析出し続けるため、鉱酸の再利用に支障をきたすことがある。さらに、硫化剤として、硫化ナトリウムや水硫化ナトリウムを用いると、鉱酸中にナトリウム等の不要なイオンが残存するため、これが鉱酸との塩、例えば硫酸塩を生じて鉱酸の濃度を低下させ、鉱酸の再利用にとっては好ましくないものとなる。
【０００４】
このため、希薄なヒ素を含有する鉱酸廃液は、従来は再利用せずに廃液処理して排出しているのが実情である。廃液処理の方法として、例えば、希薄ヒ素含有鉱酸廃液のｐＨを７以上に調整して硫化ヒ素を形成させた後、鉄塩化合物を加えて凝集沈殿させる方法が知られている（例えば、特許文献１参照。）。
【０００５】
【特許文献１】
特開平１１−２７７０７５号公報
【０００６】
【発明が解決しようとする課題】
しかしながら、希薄ヒ素含有鉱酸廃液のｐＨを７以上にするためには、多大なアルカリ性物質が必要であり、また、ヒ素を含有した沈殿物の量が鉄塩等の凝集剤の添加によって大きく増加するため、ヒ素含有沈殿物の最終処分コストが大きくなるなどの問題を抱えていた。
【０００７】
そこで本発明は、ヒ素濃度が１０００ｐｐｍ以下の希薄ヒ素を含有した鉱酸からヒ素を効率よく除去することができ、鉱酸を再生して有効に再利用することができるヒ素含有鉱酸の再生方法を提供することを目的としている。
【０００８】
【課題を解決するための手段】
上記目的を達成するため、本発明のヒ素含有鉱酸の再生方法は、第１の方法として、希薄ヒ素を含有する鉱酸からヒ素を除去して鉱酸を再生する方法であって、固形硫化物及び／又は硫黄の存在下で前記ヒ素含有鉱酸を硫化水素ガスと接触させることによりヒ素を固形硫化ヒ素に変換し、次いで固液分離手段により前記固形硫化ヒ素を除去して再生鉱酸を得ることを特徴としている。
【０００９】
本発明の処理対象となるヒ素含有鉱酸は、希薄濃度のヒ酸を含有する鉱酸溶液であり、具体的には、ヒ素濃度が１０００ｐｐｍ以下、特に５００ｐｐｍ以下の鉱酸溶液である。前記鉱酸は、硫酸、塩酸、硝酸のいずれか又はこれらの混合物であり、酸濃度は特に限定されない。また、ヒ素以外の不純物を含有している鉱酸であっても、その不純物が硫化ヒ素の形成を阻害するものでなければよい。
【００１０】
このようなヒ素含有鉱酸としては、例えば、鉱山排水、精錬工場のプロセス排水、化学工業、電子工業の排水等を挙げることができる。また、水に含まれるヒ素をヒ素吸着材に吸着させることによって水中からヒ素を除去する水処理において、ヒ素を吸着したヒ素吸着材を鉱酸で再生したときに発生するヒ素含有鉱酸廃液も本発明の処理対象となる。この場合、鉱酸廃液中のヒ素を除去することにより、再生した鉱酸をヒ素吸着材の再生用として繰り返し使用できる。
【００１１】
処理対象のヒ素含有鉱酸は、そのｐＨが４以下、特に、ｐＨ３以下であることが望ましい。ヒ素含有鉱酸のｐＨが４を超えている場合は、適当な酸、通常は同種の鉱酸を使用してｐＨを調整すべきである。
【００１２】
このようなヒ素含有鉱酸を再生するにあたり、該ヒ素含有鉱酸を、固形硫化物及び／又は硫黄の存在下で硫化水素ガスと接触させることにより、硫化ヒ素の析出を促進することができるとともに、後段の固液分離も容易となる。前記固形硫化物や硫黄は、固形であれば形状は問わないが、後段の固液分離を考慮すると、平均粒径が０．１ｍｍ以上のものが好ましい。固形硫化物や硫黄の添加方法は、粉末状の形でそのまま添加してもよいし、加水してスラリー状で添加してもよい。また、前記固形硫化物としては、硫化ヒ素や硫化銅を用いることが好ましい。固形硫化物や硫黄の添加量は、ヒ素含有鉱酸の処理量に比例し、１Ｌ／ｈｒのヒ素含有鉱酸処理量に対して、固形硫化物及び／又は硫黄は、１５０ｍｇ以上、好ましくは３００ｍｇ以上、特に５００ｍｇ以上であることが好ましい。
【００１３】
硫化剤として用いられる前記硫化水素ガスは、市販の硫化水素ガス、あるいは、水硫化ソーダ又は硫化ソーダの酸分解により発生した硫化水素ガスを使用することができる。硫化水素ガスを用いることにより、硫酸等の鉱酸中には、硫化ヒ素及び硫黄が生成されるが、後段の固液分離装置で除去可能であり、アルカリ金属等の不要なイオンが混入せず、塩が生じたりしないため、鉱酸としての再利用に問題は生じない。硫化水素ガスの注入量は、少なくとも生成される硫化ヒ素に必要な硫黄当量以上であることが必要であるが、硫化ヒ素の生成速度に比べて硫酸等の鉱酸への硫化水素ガスの溶解速度が律速になると考えられるため、通常は、硫化水素ガスを過剰気味に使用することが好ましい。
【００１４】
ヒ素含有鉱酸と硫化水素ガスとを接触させる気液接触処理の時間は１０分以上、好ましくは１５分以上である。両者の接触時間が１０分未満の場合は、ヒ素除去率が不十分になることがある。また、両者を３時間を超えて長時間接触させてもヒ素除去率はほとんど向上しないので、接触時間は３時間以下が適当である。硫化水素ガスと接触させる際のヒ素含有鉱酸の温度は、２０〜９０℃の範囲が適当であり、特に、３０〜６０℃の範囲が好ましい。温度が高いほど反応速度が速くなり、除去率が向上して短時間で処理を終えることができるが、温度を高くし過ぎると加熱のために多くのエネルギーを必要とするため、コスト的に問題となることがある。
【００１５】
固形硫化物及び／又は硫黄の存在下でヒ素含有鉱酸と硫化水素ガスとを接触させるための気液接触装置には、従来から用いられている公知の装置を使用できる。固形硫化物及び／又は硫黄は、気液接触装置内に滞留して固定床あるいは流動床を形成するようにしてもよく、原液に必要量を添加し、完全混合気液接触装置を経て後段の固液分離装置で分離するようにしてもよい。
【００１６】
生成した硫化ヒ素の結晶は、気液接触装置に固液分離機能を付加して分離してもよいが、結晶が小さくて沈降性が悪いため、気液接触装置の後段に固液分離装置を設け、この固液分離装置で確実に分離除去することが望ましい。固液分離装置としては、通常用いられている重力沈降やろ過等を含む公知の物理的固液分離装置を利用することができる。
【００１７】
また、本発明方法の別の手順（第２の方法）として、前記ヒ素含有鉱酸を硫化水素ガスと接触させる気液接触処理を行った後、固形硫化物及び／又は硫黄と接触させる固液接触処理を行うことによりヒ素を固形硫化ヒ素に変換し、次いで固液分離手段により前記固形硫化ヒ素を除去して再生鉱酸を得ることもできる。
【００１８】
この第２の方法では、ヒ素含有鉱酸と硫化水素ガスとの接触によって生成した硫化ヒ素が、次の固液接触処理で固形硫化物や硫黄と接触することにより、これらの表面で結晶化して析出が促進されるとともに、後段での固液分離も容易に行える状態となる。
【００１９】
ヒ素含有鉱酸と硫化水素ガスとを接触させる気液接触処理の時間は、１０分以上、好ましくは３０分以上である。接触時間が１０分未満では硫化ヒ素の生成率が不十分になる。また、気液接触処理を終了した液を固形硫化物及び／又は硫黄と接触させる固液接触処理の時間は、１０分以上、好ましくは１５分以上である。１０分未満では、硫化ヒ素の結晶化を十分に行えないときがあり、除去率が低下することになる。
【００２０】
ヒ素含有鉱酸と硫化水素ガスとを接触させる気液接触装置は公知のものを使用でき、固形硫化物及び／又は硫黄と液とを接触させる固液接触装置は、固形硫化物及び／又は硫黄が固定床となっていても、流動床となっていてもよく、固液接触装置の流入液に必要量を添加し、完全混合させた状態で後段の固液分離装置により分離するようにしてもよい。
【００２１】
なお、この第２の方法は、基本的に前記第１の方法と同様の条件であり、上記気液接触処理及び固液接触処理以外は第１の方法と同じようにすればよい。
【００２２】
このようにしてヒ素含有鉱酸中からヒ素を効率よく除去できるが、ヒ素除去処理後の再生鉱酸中に過剰分の硫化水素ガスが溶存していると、再生鉱酸中に残留しているヒ素と反応して硫化ヒ素を生成したり、分解して硫黄を生成することがあるため、再生鉱酸の利用先によっては不都合なことがある。
【００２３】
このように、再生鉱酸中の硫化水素ガスの溶存が問題となる場合は、再生鉱酸中から硫化水素ガスを除去する必要がある。再生鉱酸からの硫化水素ガスの除去処理は、曝気処理、加熱処理、酸化処理及び減圧吸引処理のいずれか、あるいは、これらを適当に組み合わせて行うことができる。
【００２４】
曝気処理は、空気や窒素等の気体を用いた通常の曝気処理でよく、従来から用いられている種々の散気装置を用いて行うことができる。この曝気処理を行うことにより、再生鉱酸中に溶存している硫化水素ガスは、散気空気等に同伴されて再生鉱酸から除去され、あるいは、空気中の酸素によって酸化されて硫酸となる。この曝気処理の時間や散気量は、再生鉱酸中の硫化水素溶存量や液温に応じて設定すればよい。
【００２５】
加熱処理は、前記気液接触処理の温度より高い温度に再生鉱酸を保持し、硫化水素ガスの溶解度を低減することによって再生鉱酸中から硫化水素ガスを放出させるものであり、加熱温度や処理時間は再生鉱酸中の硫化水素ガスの溶存量や液温に応じて設定することができるが、加熱温度は、通常は、５０℃以上が好ましい。
【００２６】
酸化処理は、酸素や過酸化水素等の酸化剤を再生鉱酸に添加し、再生鉱酸中の硫化水素ガスを酸化剤で酸化して硫酸とすることにより、再生鉱酸中から硫化水素ガスを除去するものであり、酸化剤の使用量は、再生鉱酸中の硫化水素ガスの溶存量に応じて設定すればよい。
【００２７】
減圧吸引処理は、真空ポンプ等を使用して再生鉱酸を減圧環境に保持し、硫化水素ガスの溶解度を低減させることによって再生鉱酸中から硫化水素ガスを放出させるものである。このときの圧力や処理時間は、再生鉱酸中の硫化水素ガスの溶存量や液温に応じて設定することができる。
【００２８】
【実施例】
実施例１，２及び比較例１
ヒ素（Ａｓ５＋）濃度１００ｍｇ／Ｌの２Ｎ硫酸２００ｍＬに、Ａｓ２Ｓ５スラリーを５０００ｐｐｍ（実施例１）、ＣｕＳスラリーを２０００ｐｐｍ（実施例２）それぞれ添加し、５０℃に加温しながら硫化水素（Ｈ２Ｓ）ガスを３０分間吹き込んだ。その後、ろ紙で固液分離し、ろ液の硫酸中の残存Ａｓ濃度を測定した。比較例１として、同じ条件で何も添加せずに実験を行い、残存Ａｓ濃度を測定した。実験条件と測定結果とを表１にまとめて示す。
【００２９】
この結果から、硫化ヒ素や硫化銅のような固形硫化物を添加することにより、硫酸中の９５％以上のヒ素が除去された。一方、固形硫化物を添加しなかった比較例１では、ヒ素はほとんど除去されなかった。
【００３１】
実施例３
ヒ素（Ａｓ５＋）濃度１００ｍｇ／Ｌの２Ｎ硫酸２００ｍＬに、ＣｕＳスラリーを表２の条件で添加し、室温で硫化水素（Ｈ２Ｓ）ガスを１０分又は３０分吹き込んだ。その後、ろ紙で固液分離し、ろ液の硫酸中の残存Ａｓ濃度を測定した。実験条件と測定結果とを表２にまとめて示す。
【００３２】
この結果から、１Ｌ／ｈｒ処理量換算添加量が１６７ｍｇであれば、５０％以上のＡｓを除去できることがわかる（実験番号１）。また、１０分程度の反応時間でも、十分にヒ素を除去することができる。しかし、反応時間が５分間だと（実験番号４）、ヒ素除去率が低下した。一方、Ａｓ除去率を７５％以上にしたい場合は、１Ｌ／ｈｒ処理量換算添加量を約３００ｍｇ以上、Ａｓ除去率を９０％以上にしたい場合は、１Ｌ／ｈｒ処理量換算添加量を約１０００ｍｇ以上とすればよいことがわかる。また、実施例２と実施例３の実験番号３とを比較すればわかるように、反応温度が室温のときよりも５０℃の方がＡｓ除去率が高くなっている。
【００３４】
実施例４
ヒ素（Ａｓ５＋）濃度１００ｍｇ／Ｌの２Ｎ硫酸２００ｍＬを５０℃に加温しながら、硫化水素（Ｈ２Ｓ）ガスを３０分間吹き込んだ後、ＣｕＳスラリー１５００ｐｐｍを添加して１０分間攪拌した。次いで、ろ紙で固液分離し、ろ液の硫酸中の残存Ａｓ濃度を測定した。実験条件と測定結果とを表３にまとめて示す。
【００３５】
表３
ＣｕＳ濃度 １５００ｐｐｍ
１Ｌ／ｈｒ処理量換算添加量 ２５０ｍｇ
ヒ素除去率 ６１．７％
【００３６】
この結果から、硫化水素ガスと接触させた後にＣｕＳを添加しても、５０％以上のＡｓを除去できることがわかる。
【００３７】
実施例５及び比較例２
ヒ素（Ａｓ５＋）濃度１００ｍｇ／Ｌの２Ｎ硫酸２００ｍＬにＣｕＳスラリー２０００ｐｐｍを添加し、５０℃に加温しながら硫化水素（Ｈ２Ｓ）ガスを１０分間吹き込んだ後、ろ紙で固液分離した。ろ液を空気で１０分間曝気処理してから３日間保存した（実施例５）。比較例２として、曝気処理しないろ液を同様にして３日間保存した。３日後、両ろ液を目視観察したところ、実施例５のろ液は無色透明で懸濁物は認められなかった。しかし、比較例２のろ液には懸濁物の発生が観測され、液全体が黄色く変色していた。
【００３８】
【発明の効果】
以上説明したように、本発明のヒ素含有鉱酸の再生方法によれば、鉱酸中に溶存しているヒ素を効率よく除去することができる。特にヒ素濃度が１０００ｐｐｍ以下、さらには５００ｐｐｍ以下の希薄ヒ素も簡単な操作で効率よく除去することができる。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a method for regenerating arsenic-containing mineral acid, and more specifically, arsenic is solidified and removed from mineral acid containing arsenic at a dilute concentration of 1000 ppm or less, particularly 500 ppm or less, and the mineral acid can be reused. On how to play.
[0002]
[Prior art]
Mineral acid containing thousands to tens of thousands of ppm of arsenic, for example, as a method of regenerating mineral acid by removing arsenic from sulfuric acid to 10 ppm or less, water-soluble sulfide or hydrogen sulfide gas is added to sulfuric acid containing arsenic, sulfuric acid In general, a method in which arsenic contained therein is insolubilized as arsenic sulfide and then separated from sulfuric acid by solid-liquid separation.
[0003]
However, in the case of a mineral acid containing dilute arsenic with an arsenic concentration of 1000 ppm or less, arsenic sulfide crystal formation becomes extremely slow, and it takes a relatively long time of several days to remove arsenic in the mineral acid below a certain concentration. It is difficult to use. In addition, even after arsenic in the mineral acid is removed to a certain concentration or less, the arsenic remaining in the mineral acid reacts with the sulfide, and fine arsenic sulfide that does not easily settle out continues to precipitate, so that the mineral acid is recycled. May interfere with use. Furthermore, when sodium sulfide or sodium hydrosulfide is used as a sulfiding agent, unnecessary ions such as sodium remain in the mineral acid, which generates a salt with the mineral acid, for example, sulfate, thereby reducing the concentration of the mineral acid. Therefore, it is not preferable for the reuse of the mineral acid.
[0004]
For this reason, the mineral acid waste liquid containing a dilute arsenic is the fact that the waste liquid treatment and discharge | emission were not carried out conventionally, but recycling. As a waste liquid treatment method, for example, a method is known in which the pH of a dilute arsenic-containing mineral acid waste liquid is adjusted to 7 or more to form arsenic sulfide, and then an iron salt compound is added to cause aggregation precipitation (for example, patents). Reference 1).
[0005]
[Patent Document 1]
JP-A-11-277075 [0006]
[Problems to be solved by the invention]
However, in order to increase the pH of the dilute arsenic-containing mineral acid waste solution to 7 or more, a large amount of alkaline substance is required, and the amount of the arsenic-containing precipitate is greatly increased by the addition of a flocculant such as iron salt. As a result, the final disposal cost of the arsenic-containing precipitate is increased.
[0007]
Accordingly, the present invention provides a method for regenerating an arsenic-containing mineral acid that can efficiently remove arsenic from a mineral acid containing dilute arsenic having an arsenic concentration of 1000 ppm or less, and that can regenerate and effectively reuse the mineral acid. The purpose is to provide.
[0008]
[Means for Solving the Problems]
In order to achieve the above object, a method for regenerating an arsenic-containing mineral acid according to the present invention is a method for regenerating a mineral acid by removing arsenic from a mineral acid containing dilute arsenic as a first method. Arsenic is converted to solid arsenic sulfide by contacting the arsenic-containing mineral acid with hydrogen sulfide gas in the presence of product and / or sulfur, and then the solid arsenic sulfide is removed by solid-liquid separation means to obtain regenerated mineral acid. It is characterized by obtaining.
[0009]
The arsenic-containing mineral acid to be treated according to the present invention is a mineral acid solution containing a dilute concentration of arsenic acid. Specifically, the mineral acid solution has an arsenic concentration of 1000 ppm or less, particularly 500 ppm or less. The mineral acid is any one of sulfuric acid, hydrochloric acid, nitric acid, or a mixture thereof, and the acid concentration is not particularly limited. Further, even a mineral acid containing impurities other than arsenic may be used as long as the impurities do not inhibit the formation of arsenic sulfide.
[0010]
Examples of such arsenic-containing mineral acids include mine drainage, smelting factory process wastewater, chemical industry, electronic industry wastewater, and the like. Also, arsenic-containing mineral acid waste liquid generated when arsenic adsorbent adsorbed with arsenic is regenerated with mineral acid in water treatment that removes arsenic from water by adsorbing arsenic contained in water to the arsenic adsorbent. It becomes the processing object of the invention. In this case, by removing arsenic from the mineral acid waste liquid, the regenerated mineral acid can be repeatedly used for regenerating the arsenic adsorbent.
[0011]
It is desirable that the arsenic-containing mineral acid to be treated has a pH of 4 or less, particularly pH 3 or less. If the pH of the arsenic-containing mineral acid exceeds 4, a suitable acid, usually the same type of mineral acid, should be used to adjust the pH.
[0012]
In regenerating such an arsenic-containing mineral acid, the precipitation of arsenic sulfide can be promoted by bringing the arsenic-containing mineral acid into contact with hydrogen sulfide gas in the presence of solid sulfide and / or sulfur. Also, the subsequent solid-liquid separation is facilitated. The shape of the solid sulfide or sulfur is not particularly limited as long as it is solid, but in view of subsequent solid-liquid separation, those having an average particle size of 0.1 mm or more are preferable. The solid sulfide or sulfur may be added as it is in the form of a powder, or may be added in the form of a slurry after adding water. Further, as the solid sulfide, it is preferable to use arsenic sulfide or copper sulfide. The amount of solid sulfide and sulfur added is proportional to the amount of arsenic-containing mineral acid treated, and the amount of solid sulfide and / or sulfur is 150 mg or more, preferably 300 mg, relative to the amount of arsenic-containing mineral acid treated of 1 L / hr. As mentioned above, it is especially preferable that it is 500 mg or more.
[0013]
As the hydrogen sulfide gas used as the sulfiding agent, commercially available hydrogen sulfide gas, or hydrogen sulfide gas generated by acid decomposition of sodium hydrosulfide or sodium sulfide can be used. By using hydrogen sulfide gas, arsenic sulfide and sulfur are produced in mineral acids such as sulfuric acid, but they can be removed by a solid-liquid separator at a later stage, and unnecessary ions such as alkali metals are not mixed. Since no salt is produced, there is no problem in reuse as a mineral acid. The amount of hydrogen sulfide gas injected must be at least as high as the sulfur equivalent required for the produced arsenic sulfide, but the dissolution rate of hydrogen sulfide gas in mineral acids such as sulfuric acid compared to the production rate of arsenic sulfide. In general, it is preferable to use hydrogen sulfide gas in an excess manner.
[0014]
The time for the gas-liquid contact treatment for bringing the arsenic-containing mineral acid into contact with the hydrogen sulfide gas is 10 minutes or longer, preferably 15 minutes or longer. If the contact time between the two is less than 10 minutes, the arsenic removal rate may be insufficient. Further, even if the two are left in contact for more than 3 hours, the arsenic removal rate is hardly improved, so the contact time is suitably 3 hours or less. The temperature of the arsenic-containing mineral acid in contact with the hydrogen sulfide gas is suitably in the range of 20 to 90 ° C, and particularly preferably in the range of 30 to 60 ° C. The higher the temperature, the faster the reaction rate and the higher the removal rate, so that the treatment can be completed in a short time. However, if the temperature is too high, a large amount of energy is required for heating, which is a problem in terms of cost. It may become.
[0015]
As a gas-liquid contact apparatus for contacting the arsenic-containing mineral acid and hydrogen sulfide gas in the presence of solid sulfide and / or sulfur, a conventionally known apparatus can be used. The solid sulfide and / or sulfur may stay in the gas-liquid contact device to form a fixed bed or a fluidized bed, and a necessary amount is added to the stock solution, and then passed through the complete mixed gas-liquid contact device. You may make it isolate | separate with a solid-liquid separator.
[0016]
The produced arsenic sulfide crystals may be separated by adding a solid-liquid separation function to the gas-liquid contact device. However, since the crystals are small and sedimentation is poor, a solid-liquid separation device is placed downstream of the gas-liquid contact device. It is desirable to provide and reliably remove with this solid-liquid separator. As the solid-liquid separation device, known physical solid-liquid separation devices including commonly used gravity sedimentation and filtration can be used.
[0017]
Further, as another procedure (second method) of the method of the present invention, after performing a gas-liquid contact treatment in which the arsenic-containing mineral acid is brought into contact with hydrogen sulfide gas, a solid-liquid to be brought into contact with solid sulfide and / or sulfur. It is also possible to convert the arsenic to solid arsenic sulfide by performing a contact treatment, and then remove the solid arsenic sulfide by solid-liquid separation means to obtain a regenerated mineral acid.
[0018]
In this second method, the arsenic sulfide produced by the contact between the arsenic-containing mineral acid and hydrogen sulfide gas is crystallized on these surfaces by contacting with solid sulfide or sulfur in the subsequent solid-liquid contact treatment. Precipitation is promoted, and solid-liquid separation at a later stage can be easily performed.
[0019]
The time for the gas-liquid contact treatment for bringing the arsenic-containing mineral acid into contact with the hydrogen sulfide gas is 10 minutes or longer, preferably 30 minutes or longer. If the contact time is less than 10 minutes, the generation rate of arsenic sulfide is insufficient. Moreover, the time of the solid-liquid contact process which contacts the liquid which complete | finished the gas-liquid contact process with a solid sulfide and / or sulfur is 10 minutes or more, Preferably it is 15 minutes or more. If it is less than 10 minutes, arsenic sulfide may not be sufficiently crystallized, and the removal rate will decrease.
[0020]
A known gas-liquid contact device for contacting arsenic-containing mineral acid with hydrogen sulfide gas can be used, and a solid-liquid contact device for contacting solid sulfide and / or sulfur with liquid can be used for solid sulfide and / or sulfur. It can be a fixed bed or a fluidized bed, and the required amount is added to the influent of the solid-liquid contact device and separated by a subsequent solid-liquid separation device in a completely mixed state. Also good.
[0021]
The second method has basically the same conditions as the first method, and may be the same as the first method except for the gas-liquid contact treatment and the solid-liquid contact treatment.
[0022]
In this way, arsenic can be efficiently removed from the arsenic-containing mineral acid, but if excessive hydrogen sulfide gas is dissolved in the regenerated mineral acid after the arsenic removal treatment, it remains in the regenerated mineral acid. Since it may react with arsenic to produce arsenic sulfide or decompose to produce sulfur, it may be inconvenient depending on the use of regenerated mineral acid.
[0023]
Thus, when dissolution of hydrogen sulfide gas in the regenerated mineral acid becomes a problem, it is necessary to remove the hydrogen sulfide gas from the regenerated mineral acid. The removal treatment of hydrogen sulfide gas from the regenerated mineral acid can be carried out by any one of aeration treatment, heat treatment, oxidation treatment, and vacuum suction treatment, or an appropriate combination thereof.
[0024]
The aeration process may be a normal aeration process using a gas such as air or nitrogen, and can be performed using various conventionally used aeration devices. By performing this aeration treatment, the hydrogen sulfide gas dissolved in the regenerated mineral acid is removed from the regenerated mineral acid accompanied by air diffused or the like, or oxidized by oxygen in the air to become sulfuric acid. . What is necessary is just to set the time and the amount of aeration of this aeration process according to the amount of hydrogen sulfide dissolved in the regenerated mineral acid and the liquid temperature.
[0025]
The heat treatment is to release the hydrogen sulfide gas from the regenerated mineral acid by holding the regenerated mineral acid at a temperature higher than the temperature of the gas-liquid contact treatment and reducing the solubility of the hydrogen sulfide gas. The treatment time can be set according to the dissolved amount of hydrogen sulfide gas in the regenerated mineral acid and the liquid temperature, but the heating temperature is usually preferably 50 ° C. or higher.
[0026]
Oxidation treatment is performed by adding an oxidizing agent such as oxygen or hydrogen peroxide to the regenerated mineral acid, and oxidizing the hydrogen sulfide gas in the regenerated mineral acid with the oxidant to produce sulfuric acid, thereby producing hydrogen sulfide gas from the regenerated mineral acid. The amount of oxidizing agent used may be set according to the dissolved amount of hydrogen sulfide gas in the regenerated mineral acid.
[0027]
The vacuum suction treatment is to release hydrogen sulfide gas from the regenerated mineral acid by maintaining the regenerated mineral acid in a reduced pressure environment using a vacuum pump or the like and reducing the solubility of the hydrogen sulfide gas. The pressure and treatment time at this time can be set according to the dissolved amount of hydrogen sulfide gas in the regenerated mineral acid and the liquid temperature.
[0028]
【Example】
Examples 1 and 2 and Comparative Example 1
To 200 mL of 2N sulfuric acid having an arsenic (As 5+ ) concentration of 100 mg / L, 5000 ppm (Example 1) of As 2 S 5 slurry and 2000 ppm (Example 2) of CuS slurry were added, and hydrogen sulfide was heated to 50 ° C. (H 2 S) gas was blown in for 30 minutes. Then, it separated into solid and liquid with the filter paper, and the residual As density | concentration in the sulfuric acid of a filtrate was measured. As Comparative Example 1, an experiment was performed without adding anything under the same conditions, and the residual As concentration was measured. Experimental conditions and measurement results are summarized in Table 1.
[0029]
From this result, 95% or more of arsenic in sulfuric acid was removed by adding a solid sulfide such as arsenic sulfide or copper sulfide. On the other hand, in Comparative Example 1 in which no solid sulfide was added, arsenic was hardly removed.
[0031]
Example 3
CuS slurry was added to 200 mL of 2N sulfuric acid having an arsenic (As 5+ ) concentration of 100 mg / L under the conditions shown in Table 2, and hydrogen sulfide (H 2 S) gas was blown in at room temperature for 10 minutes or 30 minutes. Then, it separated into solid and liquid with the filter paper, and the residual As density | concentration in the sulfuric acid of a filtrate was measured. Table 2 summarizes the experimental conditions and the measurement results.
[0032]
From this result, it can be seen that 50% or more of As can be removed when the 1 L / hr treated amount conversion addition amount is 167 mg (Experiment No. 1). Further, arsenic can be sufficiently removed even with a reaction time of about 10 minutes. However, when the reaction time was 5 minutes (Experiment No. 4), the arsenic removal rate decreased. On the other hand, when the As removal rate is desired to be 75% or more, the 1L / hr treatment amount equivalent addition amount is about 300 mg or more, and when the As removal rate is 90% or more, the 1 L / hr treatment amount equivalent addition amount is about 1000 mg. It turns out that it should just be above. Further, as can be seen by comparing the experiment number 3 of Example 2 and Example 3, the As removal rate is higher at 50 ° C. than when the reaction temperature is room temperature.
[0034]
Example 4
While 200 mL of 2N sulfuric acid having an arsenic (As 5+ ) concentration of 100 mg / L was heated to 50 ° C., hydrogen sulfide (H 2 S) gas was blown for 30 minutes, and then 1500 ppm of CuS slurry was added and stirred for 10 minutes. Subsequently, it separated into solid and liquid with the filter paper, and the residual As density | concentration in the sulfuric acid of a filtrate was measured. The experimental conditions and measurement results are summarized in Table 3.
[0035]
Table 3
CuS concentration 1500ppm
1L / hr treatment amount equivalent addition amount 250mg
Arsenic removal rate 61.7%
[0036]
From this result, it can be seen that 50% or more of As can be removed even if CuS is added after contact with hydrogen sulfide gas.
[0037]
Example 5 and Comparative Example 2
After adding 2000 ppm of CuS slurry to 200 mL of 2N sulfuric acid with an arsenic (As 5+ ) concentration of 100 mg / L, hydrogen sulfide (H 2 S) gas was blown in for 10 minutes while heating to 50 ° C., and solid-liquid separation was performed with filter paper. The filtrate was aerated with air for 10 minutes and then stored for 3 days (Example 5). As Comparative Example 2, the filtrate not subjected to aeration treatment was stored in the same manner for 3 days. Three days later, both filtrates were visually observed. As a result, the filtrate of Example 5 was colorless and transparent, and no suspension was observed. However, in the filtrate of Comparative Example 2, the generation of a suspension was observed, and the entire liquid was discolored yellow.
[0038]
【The invention's effect】
As described above, according to the method for regenerating arsenic-containing mineral acid of the present invention, arsenic dissolved in mineral acid can be efficiently removed. In particular, dilute arsenic having an arsenic concentration of 1000 ppm or less and even 500 ppm or less can be efficiently removed by a simple operation.
Claims (7)
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005040656A (en) * | 2003-07-23 | 2005-02-17 | Maezawa Ind Inc | Treatment method for arsenic-containing mineral acid |
| JP2005224686A (en) * | 2004-02-12 | 2005-08-25 | Maezawa Ind Inc | Arsenic removal method |
| CN101857203A (en) * | 2010-05-24 | 2010-10-13 | 东营方圆有色金属有限公司 | Process for comprehensively recycling heavy metal-polluted acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005040656A (en) * | 2003-07-23 | 2005-02-17 | Maezawa Ind Inc | Treatment method for arsenic-containing mineral acid |
| JP4567303B2 (en) * | 2003-07-23 | 2010-10-20 | 前澤工業株式会社 | Method for treating arsenic-containing sulfuric acid |
| JP2005224686A (en) * | 2004-02-12 | 2005-08-25 | Maezawa Ind Inc | Arsenic removal method |
| JP4567344B2 (en) * | 2004-02-12 | 2010-10-20 | 前澤工業株式会社 | How to remove arsenic |
| CN101857203A (en) * | 2010-05-24 | 2010-10-13 | 东营方圆有色金属有限公司 | Process for comprehensively recycling heavy metal-polluted acid |
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