JP7372069B2 - Formic acid recovery method - Google Patents
Formic acid recovery method Download PDFInfo
- Publication number
- JP7372069B2 JP7372069B2 JP2019138664A JP2019138664A JP7372069B2 JP 7372069 B2 JP7372069 B2 JP 7372069B2 JP 2019138664 A JP2019138664 A JP 2019138664A JP 2019138664 A JP2019138664 A JP 2019138664A JP 7372069 B2 JP7372069 B2 JP 7372069B2
- Authority
- JP
- Japan
- Prior art keywords
- formic acid
- solution
- exchange resin
- recovery method
- group
- 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.)
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- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 title claims description 304
- 235000019253 formic acid Nutrition 0.000 title claims description 152
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 title claims description 151
- 238000000034 method Methods 0.000 title claims description 45
- 238000011084 recovery Methods 0.000 title claims description 25
- 239000000243 solution Substances 0.000 claims description 57
- 150000001412 amines Chemical class 0.000 claims description 44
- 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 claims description 36
- 239000003729 cation exchange resin Substances 0.000 claims description 35
- 125000000217 alkyl group Chemical group 0.000 claims description 30
- -1 formate ions Chemical class 0.000 claims description 26
- 239000003929 acidic solution Substances 0.000 claims description 24
- 125000004432 carbon atom Chemical group C* 0.000 claims description 24
- 230000002378 acidificating effect Effects 0.000 claims description 21
- 239000003637 basic solution Substances 0.000 claims description 16
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 12
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 11
- 229910000028 potassium bicarbonate Inorganic materials 0.000 claims description 6
- 235000015497 potassium bicarbonate Nutrition 0.000 claims description 6
- 239000011736 potassium bicarbonate Substances 0.000 claims description 6
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 6
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 6
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 6
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 5
- 229940086066 potassium hydrogencarbonate Drugs 0.000 claims description 5
- 239000006185 dispersion Substances 0.000 claims description 4
- 238000000605 extraction Methods 0.000 description 39
- 239000002904 solvent Substances 0.000 description 26
- 238000004821 distillation Methods 0.000 description 23
- 229910052739 hydrogen Inorganic materials 0.000 description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 23
- 239000001257 hydrogen Substances 0.000 description 22
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 20
- 238000003860 storage Methods 0.000 description 15
- 230000000052 comparative effect Effects 0.000 description 11
- 238000000354 decomposition reaction Methods 0.000 description 11
- 150000007524 organic acids Chemical class 0.000 description 11
- UWHRNIXHZAWBMF-UHFFFAOYSA-N n-dodecyl-n-methyldodecan-1-amine Chemical compound CCCCCCCCCCCCN(C)CCCCCCCCCCCC UWHRNIXHZAWBMF-UHFFFAOYSA-N 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- 150000001298 alcohols Chemical class 0.000 description 9
- 239000007864 aqueous solution Substances 0.000 description 9
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 6
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 125000003438 dodecyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 6
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 6
- 125000001147 pentyl group Chemical group C(CCCC)* 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 239000003957 anion exchange resin Substances 0.000 description 5
- 150000001768 cations Chemical class 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 5
- 239000011347 resin Substances 0.000 description 5
- 229920005989 resin Polymers 0.000 description 5
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 description 4
- LEACJMVNYZDSKR-UHFFFAOYSA-N 2-octyldodecan-1-ol Chemical compound CCCCCCCCCCC(CO)CCCCCCCC LEACJMVNYZDSKR-UHFFFAOYSA-N 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 125000002704 decyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 4
- 125000003187 heptyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 4
- 125000004051 hexyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000003456 ion exchange resin Substances 0.000 description 4
- 229920003303 ion-exchange polymer Polymers 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 125000001400 nonyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 4
- 235000005985 organic acids Nutrition 0.000 description 4
- 239000012074 organic phase Substances 0.000 description 4
- 230000020477 pH reduction Effects 0.000 description 4
- 239000011232 storage material Substances 0.000 description 4
- SWZDQOUHBYYPJD-UHFFFAOYSA-N tridodecylamine Chemical compound CCCCCCCCCCCCN(CCCCCCCCCCCC)CCCCCCCCCCCC SWZDQOUHBYYPJD-UHFFFAOYSA-N 0.000 description 4
- 125000002948 undecyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 3
- YJLYANLCNIKXMG-UHFFFAOYSA-N N-Methyldioctylamine Chemical compound CCCCCCCCN(C)CCCCCCCC YJLYANLCNIKXMG-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 229920002125 Sokalan® Polymers 0.000 description 3
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 description 3
- 239000008346 aqueous phase Substances 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 229940023913 cation exchange resins Drugs 0.000 description 3
- 238000004128 high performance liquid chromatography Methods 0.000 description 3
- 150000004678 hydrides Chemical class 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 235000010755 mineral Nutrition 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- OOHAUGDGCWURIT-UHFFFAOYSA-N n,n-dipentylpentan-1-amine Chemical compound CCCCCN(CCCCC)CCCCC OOHAUGDGCWURIT-UHFFFAOYSA-N 0.000 description 3
- MJCJUDJQDGGKOX-UHFFFAOYSA-N n-dodecyldodecan-1-amine Chemical compound CCCCCCCCCCCCNCCCCCCCCCCCC MJCJUDJQDGGKOX-UHFFFAOYSA-N 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- XFRVVPUIAFSTFO-UHFFFAOYSA-N 1-Tridecanol Chemical compound CCCCCCCCCCCCCO XFRVVPUIAFSTFO-UHFFFAOYSA-N 0.000 description 2
- CFOQKXQWGLAKSK-UHFFFAOYSA-N 13-docosen-1-ol Natural products CCCCCCCCC=CCCCCCCCCCCCCO CFOQKXQWGLAKSK-UHFFFAOYSA-N 0.000 description 2
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 229910045601 alloy Inorganic materials 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- MWKFXSUHUHTGQN-UHFFFAOYSA-N decan-1-ol Chemical compound CCCCCCCCCCO MWKFXSUHUHTGQN-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 description 2
- NOPFSRXAKWQILS-UHFFFAOYSA-N docosan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCCCCCO NOPFSRXAKWQILS-UHFFFAOYSA-N 0.000 description 2
- LQZZUXJYWNFBMV-UHFFFAOYSA-N dodecan-1-ol Chemical compound CCCCCCCCCCCCO LQZZUXJYWNFBMV-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- FIPPFBHCBUDBRR-UHFFFAOYSA-N henicosan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCCCCO FIPPFBHCBUDBRR-UHFFFAOYSA-N 0.000 description 2
- GOQYKNQRPGWPLP-UHFFFAOYSA-N heptadecan-1-ol Chemical compound CCCCCCCCCCCCCCCCCO GOQYKNQRPGWPLP-UHFFFAOYSA-N 0.000 description 2
- IRHTZOCLLONTOC-UHFFFAOYSA-N hexacosan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCCCCCCCCCO IRHTZOCLLONTOC-UHFFFAOYSA-N 0.000 description 2
- BXWNKGSJHAJOGX-UHFFFAOYSA-N hexadecan-1-ol Chemical compound CCCCCCCCCCCCCCCCO BXWNKGSJHAJOGX-UHFFFAOYSA-N 0.000 description 2
- BTFJIXJJCSYFAL-UHFFFAOYSA-N icosan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCCCO BTFJIXJJCSYFAL-UHFFFAOYSA-N 0.000 description 2
- 230000003993 interaction Effects 0.000 description 2
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 2
- 125000002960 margaryl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- TZIHFWKZFHZASV-UHFFFAOYSA-N methyl formate Chemical compound COC=O TZIHFWKZFHZASV-UHFFFAOYSA-N 0.000 description 2
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 description 2
- 125000001421 myristyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 2
- XGFDHKJUZCCPKQ-UHFFFAOYSA-N nonadecan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCCO XGFDHKJUZCCPKQ-UHFFFAOYSA-N 0.000 description 2
- ZWRUINPWMLAQRD-UHFFFAOYSA-N nonan-1-ol Chemical compound CCCCCCCCCO ZWRUINPWMLAQRD-UHFFFAOYSA-N 0.000 description 2
- GLDOVTGHNKAZLK-UHFFFAOYSA-N octadecan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCO GLDOVTGHNKAZLK-UHFFFAOYSA-N 0.000 description 2
- 125000000913 palmityl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 2
- REIUXOLGHVXAEO-UHFFFAOYSA-N pentadecan-1-ol Chemical compound CCCCCCCCCCCCCCCO REIUXOLGHVXAEO-UHFFFAOYSA-N 0.000 description 2
- 125000002958 pentadecyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 125000004079 stearyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 2
- 150000003512 tertiary amines Chemical class 0.000 description 2
- TYWMIZZBOVGFOV-UHFFFAOYSA-N tetracosan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCCCCCCCO TYWMIZZBOVGFOV-UHFFFAOYSA-N 0.000 description 2
- HLZKNKRTKFSKGZ-UHFFFAOYSA-N tetradecan-1-ol Chemical compound CCCCCCCCCCCCCCO HLZKNKRTKFSKGZ-UHFFFAOYSA-N 0.000 description 2
- 125000002889 tridecyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 2
- KJIOQYGWTQBHNH-UHFFFAOYSA-N undecanol Chemical compound CCCCCCCCCCCO KJIOQYGWTQBHNH-UHFFFAOYSA-N 0.000 description 2
- ALSTYHKOOCGGFT-KTKRTIGZSA-N (9Z)-octadecen-1-ol Chemical compound CCCCCCCC\C=C/CCCCCCCCO ALSTYHKOOCGGFT-KTKRTIGZSA-N 0.000 description 1
- JXNPEDYJTDQORS-HZJYTTRNSA-N (9Z,12Z)-octadecadien-1-ol Chemical compound CCCCC\C=C/C\C=C/CCCCCCCCO JXNPEDYJTDQORS-HZJYTTRNSA-N 0.000 description 1
- MLRYPOCSLBIUHY-ZHACJKMWSA-N (e)-dodec-2-en-1-ol Chemical compound CCCCCCCCC\C=C\CO MLRYPOCSLBIUHY-ZHACJKMWSA-N 0.000 description 1
- VPYJHNADOJDSGU-VAWYXSNFSA-N (e)-tridec-2-en-1-ol Chemical compound CCCCCCCCCC\C=C\CO VPYJHNADOJDSGU-VAWYXSNFSA-N 0.000 description 1
- 239000005968 1-Decanol Substances 0.000 description 1
- 229940094997 1-tetracosanol Drugs 0.000 description 1
- WADSJYLPJPTMLN-UHFFFAOYSA-N 3-(cycloundecen-1-yl)-1,2-diazacycloundec-2-ene Chemical compound C1CCCCCCCCC=C1C1=NNCCCCCCCC1 WADSJYLPJPTMLN-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
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- ALINDUHUXHQTEU-UHFFFAOYSA-N N-nonyl-N-propylnonan-1-amine Chemical compound CCCCCCCCCN(CCC)CCCCCCCCC ALINDUHUXHQTEU-UHFFFAOYSA-N 0.000 description 1
- NKGSHSILLGXYDW-UHFFFAOYSA-N N-undecylundecan-1-amine Chemical compound CCCCCCCCCCCNCCCCCCCCCCC NKGSHSILLGXYDW-UHFFFAOYSA-N 0.000 description 1
- KDYFGRWQOYBRFD-UHFFFAOYSA-N Succinic acid Natural products OC(=O)CCC(O)=O KDYFGRWQOYBRFD-UHFFFAOYSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
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- KDYFGRWQOYBRFD-NUQCWPJISA-N butanedioic acid Chemical compound O[14C](=O)CC[14C](O)=O KDYFGRWQOYBRFD-NUQCWPJISA-N 0.000 description 1
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- ZMCUDHNSHCRDBT-UHFFFAOYSA-M caesium bicarbonate Chemical compound [Cs+].OC([O-])=O ZMCUDHNSHCRDBT-UHFFFAOYSA-M 0.000 description 1
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- NAPSCFZYZVSQHF-UHFFFAOYSA-N dimantine Chemical compound CCCCCCCCCCCCCCCCCCN(C)C NAPSCFZYZVSQHF-UHFFFAOYSA-N 0.000 description 1
- 229950010007 dimantine Drugs 0.000 description 1
- LAWOZCWGWDVVSG-UHFFFAOYSA-N dioctylamine Chemical compound CCCCCCCCNCCCCCCCC LAWOZCWGWDVVSG-UHFFFAOYSA-N 0.000 description 1
- QILSFLSDHQAZET-UHFFFAOYSA-N diphenylmethanol Chemical compound C=1C=CC=CC=1C(O)C1=CC=CC=C1 QILSFLSDHQAZET-UHFFFAOYSA-N 0.000 description 1
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- 239000003480 eluent Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
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- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
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- 230000003301 hydrolyzing effect Effects 0.000 description 1
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- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
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- 230000002401 inhibitory effect Effects 0.000 description 1
- 229910010276 inorganic hydride Inorganic materials 0.000 description 1
- 239000004310 lactic acid Substances 0.000 description 1
- 235000014655 lactic acid Nutrition 0.000 description 1
- JXNPEDYJTDQORS-UHFFFAOYSA-N linoleyl alcohol Natural products CCCCCC=CCC=CCCCCCCCCO JXNPEDYJTDQORS-UHFFFAOYSA-N 0.000 description 1
- 229910000032 lithium hydrogen carbonate Inorganic materials 0.000 description 1
- HQRPHMAXFVUBJX-UHFFFAOYSA-M lithium;hydrogen carbonate Chemical compound [Li+].OC([O-])=O HQRPHMAXFVUBJX-UHFFFAOYSA-M 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- ZQJAONQEOXOVNR-UHFFFAOYSA-N n,n-di(nonyl)nonan-1-amine Chemical compound CCCCCCCCCN(CCCCCCCCC)CCCCCCCCC ZQJAONQEOXOVNR-UHFFFAOYSA-N 0.000 description 1
- JEIFGNLZAYFLFL-UHFFFAOYSA-N n,n-di(undecyl)undecan-1-amine Chemical compound CCCCCCCCCCCN(CCCCCCCCCCC)CCCCCCCCCCC JEIFGNLZAYFLFL-UHFFFAOYSA-N 0.000 description 1
- XTAZYLNFDRKIHJ-UHFFFAOYSA-N n,n-dioctyloctan-1-amine Chemical compound CCCCCCCCN(CCCCCCCC)CCCCCCCC XTAZYLNFDRKIHJ-UHFFFAOYSA-N 0.000 description 1
- YGNSGUIRANPPSW-UHFFFAOYSA-N n-decyl-n-ethyldecan-1-amine Chemical compound CCCCCCCCCCN(CC)CCCCCCCCCC YGNSGUIRANPPSW-UHFFFAOYSA-N 0.000 description 1
- ATBNMWWDBWBAHM-UHFFFAOYSA-N n-decyl-n-methyldecan-1-amine Chemical compound CCCCCCCCCCN(C)CCCCCCCCCC ATBNMWWDBWBAHM-UHFFFAOYSA-N 0.000 description 1
- GMTCPFCMAHMEMT-UHFFFAOYSA-N n-decyldecan-1-amine Chemical compound CCCCCCCCCCNCCCCCCCCCC GMTCPFCMAHMEMT-UHFFFAOYSA-N 0.000 description 1
- GNWJPYGUYHYTSI-UHFFFAOYSA-N n-dodecyl-n-ethyldodecan-1-amine Chemical compound CCCCCCCCCCCCN(CC)CCCCCCCCCCCC GNWJPYGUYHYTSI-UHFFFAOYSA-N 0.000 description 1
- VEVUAJBJLBWXAK-UHFFFAOYSA-N n-dodecyl-n-propyldodecan-1-amine Chemical compound CCCCCCCCCCCCN(CCC)CCCCCCCCCCCC VEVUAJBJLBWXAK-UHFFFAOYSA-N 0.000 description 1
- GESMBXUFPAHBOJ-UHFFFAOYSA-N n-ethyl-n-nonylnonan-1-amine Chemical compound CCCCCCCCCN(CC)CCCCCCCCC GESMBXUFPAHBOJ-UHFFFAOYSA-N 0.000 description 1
- KYSDFVPIAZIJAW-UHFFFAOYSA-N n-ethyl-n-octyloctan-1-amine Chemical compound CCCCCCCCN(CC)CCCCCCCC KYSDFVPIAZIJAW-UHFFFAOYSA-N 0.000 description 1
- YMCSXHNAZSSXTO-UHFFFAOYSA-N n-ethyl-n-undecylundecan-1-amine Chemical compound CCCCCCCCCCCN(CC)CCCCCCCCCCC YMCSXHNAZSSXTO-UHFFFAOYSA-N 0.000 description 1
- IITLRKXIQJEWFI-UHFFFAOYSA-N n-methyl-n-nonylnonan-1-amine Chemical compound CCCCCCCCCN(C)CCCCCCCCC IITLRKXIQJEWFI-UHFFFAOYSA-N 0.000 description 1
- ISZWDCITQRHAEG-UHFFFAOYSA-N n-methyl-n-undecylundecan-1-amine Chemical compound CCCCCCCCCCCN(C)CCCCCCCCCCC ISZWDCITQRHAEG-UHFFFAOYSA-N 0.000 description 1
- OMEMQVZNTDHENJ-UHFFFAOYSA-N n-methyldodecan-1-amine Chemical compound CCCCCCCCCCCCNC OMEMQVZNTDHENJ-UHFFFAOYSA-N 0.000 description 1
- MFHKEJIIHDNPQE-UHFFFAOYSA-N n-nonylnonan-1-amine Chemical compound CCCCCCCCCNCCCCCCCCC MFHKEJIIHDNPQE-UHFFFAOYSA-N 0.000 description 1
- JVHQABRJBCIYFO-UHFFFAOYSA-N n-octyl-n-propyloctan-1-amine Chemical compound CCCCCCCCN(CCC)CCCCCCCC JVHQABRJBCIYFO-UHFFFAOYSA-N 0.000 description 1
- AQCYZQXAHSRKIF-UHFFFAOYSA-N n-propyl-n-undecylundecan-1-amine Chemical compound CCCCCCCCCCCN(CCC)CCCCCCCCCCC AQCYZQXAHSRKIF-UHFFFAOYSA-N 0.000 description 1
- ALSTYHKOOCGGFT-MDZDMXLPSA-N oleyl alcohol Chemical compound CCCCCCCC\C=C\CCCCCCCCO ALSTYHKOOCGGFT-MDZDMXLPSA-N 0.000 description 1
- 229940055577 oleyl alcohol Drugs 0.000 description 1
- XMLQWXUVTXCDDL-UHFFFAOYSA-N oleyl alcohol Natural products CCCCCCC=CCCCCCCCCCCO XMLQWXUVTXCDDL-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 125000002524 organometallic group Chemical group 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- ACVYVLVWPXVTIT-UHFFFAOYSA-N phosphinic acid Chemical group O[PH2]=O ACVYVLVWPXVTIT-UHFFFAOYSA-N 0.000 description 1
- ABLZXFCXXLZCGV-UHFFFAOYSA-N phosphonic acid group Chemical group P(O)(O)=O ABLZXFCXXLZCGV-UHFFFAOYSA-N 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 125000001436 propyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 238000010561 standard procedure Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 125000000542 sulfonic acid group Chemical group 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
- ABVVEAHYODGCLZ-UHFFFAOYSA-N tridecan-1-amine Chemical compound CCCCCCCCCCCCCN ABVVEAHYODGCLZ-UHFFFAOYSA-N 0.000 description 1
- YFTHZRPMJXBUME-UHFFFAOYSA-N tripropylamine Chemical compound CCCN(CCC)CCC YFTHZRPMJXBUME-UHFFFAOYSA-N 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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- Extraction Or Liquid Replacement (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
本発明は、ギ酸回収方法に関する。 The present invention relates to a method for recovering formic acid.
地球温暖化、化石燃料枯渇の問題などから、次世代エネルギーとして水素エネルギーに高い期待が寄せられている。水素エネルギー社会を実現するためには、水素の製造、貯蔵、利用の各技術が必要であるが、水素貯蔵には貯蔵、輸送、安全性、サイクル、コスト等の様々な課題がある。 Due to issues such as global warming and depletion of fossil fuels, high expectations are placed on hydrogen energy as a next-generation energy source. In order to realize a hydrogen energy society, technologies for hydrogen production, storage, and utilization are necessary, but hydrogen storage has various issues such as storage, transportation, safety, cycles, and cost.
水素貯蔵技術は、主に、圧縮水素での貯蔵、低温液体水素での貯蔵、水素貯蔵材料での貯蔵に分けられる。圧縮水素での貯蔵には３５～７０ＭＰａの高圧が、液体水素での貯蔵には－２５３℃以下と非常に低い温度が必要とされ、コスト面、安全面で優れた水素貯蔵法とは言えない。
こうした背景により水素貯蔵材料として、水素貯蔵合金、有機ハイドライド、無機ハイドライド、有機金属錯体、多孔質炭素材料等の、各種材料の開発が検討されている。中でも有機ハイドライドは、取扱いの簡便さや、水素貯蔵密度が高く軽量であるといった利点を有し注目されている。
Hydrogen storage technology is mainly divided into compressed hydrogen storage, cryogenic liquid hydrogen storage, and hydrogen storage material storage. Storing compressed hydrogen requires a high pressure of 35 to 70 MPa, and storing liquid hydrogen requires a very low temperature of -253°C or lower, so it cannot be said to be an excellent hydrogen storage method in terms of cost and safety. .
Against this background, various materials such as hydrogen storage alloys, organic hydrides, inorganic hydrides, organometallic complexes, and porous carbon materials are being developed as hydrogen storage materials. Among them, organic hydrides are attracting attention because of their advantages such as ease of handling, high hydrogen storage density, and light weight.
有機ハイドライドとしては、ベンゼン、トルエン、ビフェニル、ナフタレン、シクロヘキサン、メチルシクロヘキサン等の炭化水素化合物が知られている。これらの炭化水素化合物は、体積貯蔵密度及び質量貯蔵密度が圧縮水素や水素吸蔵合金等と比べて高く、また、常温で液体であるため、輸送面でのメリットがあるが、危険物とされているものもあるため、取扱いに注意が必要である。また、脱水素化反応により水素を取り出す際にはエネルギーが必要となる。
そして、炭化水素化合物と同等の体積貯蔵密度及び質量貯蔵密度を有し、脱水素化反応に必要なエネルギーが炭化水素化合物よりも低く、より簡便な取扱いが可能な化合物として、ギ酸が検討されている。ギ酸を水素貯蔵材料として用いるには、輸送コストの削減のためギ酸溶液を濃縮することが必要である。
Hydrocarbon compounds such as benzene, toluene, biphenyl, naphthalene, cyclohexane, and methylcyclohexane are known as organic hydrides. These hydrocarbon compounds have higher volume storage densities and mass storage densities than compressed hydrogen, hydrogen storage alloys, etc., and are liquid at room temperature, so they have advantages in terms of transportation, but they are not considered dangerous. Please be careful when handling it as some of them may be contaminated. Furthermore, energy is required when hydrogen is extracted through a dehydrogenation reaction.
Formic acid has been studied as a compound that has volume storage density and mass storage density equivalent to hydrocarbon compounds, requires less energy for dehydrogenation reaction than hydrocarbon compounds, and can be handled more easily. There is. To use formic acid as a hydrogen storage material, it is necessary to concentrate the formic acid solution to reduce transportation costs.
一方、乳酸、コハク酸等の有機酸の濃縮の方法としては、有機酸を陰イオン交換樹脂に吸着して濃縮する方法が検討されている。例えば、特許文献１には、発酵により生産された有機酸を含む有機酸水性粗溶液を、ＩＩ型強塩基性イオン交換樹脂と接触させて、有機酸イオンをＩＩ型強塩基性イオン交換樹脂に吸着させ、吸着された有機酸イオンを、鉱酸水溶液を含む溶離液によって溶出させる方法が記載されている。また、特許文献２には、有機酸を含有する被処理液を、強塩基性陰イオン交換樹脂を通過させて、有機酸を強塩基性陰イオン交換樹脂に吸着させ、水酸化ナトリウム水溶液を用いて、有機酸を溶出させ回収する有機酸の分離・回収方法が記載されている。
特許文献３には有機酸を低濃度で含有する水溶液からアミンを含む抽出液を用いて有機酸を回収する方法が記載されている。
また、特許文献４にはギ酸メチルを加水分解してギ酸を得るギ酸の製造方法と、抽出と蒸留によりギ酸溶液を濃縮する方法が記載されている。
On the other hand, as a method for concentrating organic acids such as lactic acid and succinic acid, a method of concentrating organic acids by adsorbing them onto an anion exchange resin has been studied. For example, in Patent Document 1, an organic acid aqueous crude solution containing an organic acid produced by fermentation is brought into contact with a type II strong basic ion exchange resin, and the organic acid ions are converted into a type II strong basic ion exchange resin. A method is described in which the organic acid ions are adsorbed and the adsorbed organic acid ions are eluted with an eluent containing an aqueous mineral acid solution. In addition, Patent Document 2 discloses that a liquid to be treated containing an organic acid is passed through a strong basic anion exchange resin, the organic acid is adsorbed on the strong basic anion exchange resin, and a sodium hydroxide aqueous solution is used. A method for separating and recovering organic acids is described in which the organic acids are eluted and recovered.
Patent Document 3 describes a method for recovering an organic acid from an aqueous solution containing the organic acid at a low concentration using an extract containing an amine.
Further, Patent Document 4 describes a method for producing formic acid in which formic acid is obtained by hydrolyzing methyl formate, and a method for concentrating a formic acid solution by extraction and distillation.
ギ酸を水素貯蔵材料として用いる場合、塩基性溶液中で、二酸化炭素と水素とを接触させる、又は二酸化炭素を電気化学的に還元する反応等によりギ酸を生成させる。しかし、反応が平衡により停止し、低濃度のギ酸溶液しか得られない。輸送コストの削減には、高濃度のギ酸溶液とすることが望ましく、本発明者らは、低濃度でギ酸を含む塩基性溶液から、低エネルギーでギ酸溶液を濃縮し、高収率でギ酸を回収する必要があるという、新たな課題を見出した。 When formic acid is used as a hydrogen storage material, formic acid is produced by contacting carbon dioxide and hydrogen in a basic solution, or by electrochemically reducing carbon dioxide. However, the reaction stops due to equilibrium and only a low concentration formic acid solution is obtained. In order to reduce transportation costs, it is desirable to have a highly concentrated formic acid solution, and the present inventors concentrated the formic acid solution with low energy from a basic solution containing formic acid at a low concentration, and produced formic acid in high yield. We discovered a new problem: the need to collect the materials.
しかしながら、二酸化炭素と水素より生成した低濃度のギ酸溶液を、抽出と蒸留で回収するには多大なエネルギーを要するため、高効率で濃縮し、高収率でギ酸を回収する必要がある。
特許文献１及び２で得られる有機酸溶液は酸性であり、従来の技術においては、塩基性のギ酸溶液を、陽イオン交換樹脂で酸性化し、特定のアミンを含む抽出剤によりギ酸を抽出する方法については検討がされていない。
また、本発明者らの知見によれば、塩基性のギ酸溶液の濃縮に陰イオン交換樹脂を用いた場合、ギ酸の吸着量が少なく、その濃縮効率は満足できるものではないことがわかった。
そして、特許文献３及び４に記載の、低濃度のギ酸溶液から抽出と蒸留のみでギ酸を回収する方法では、多大なエネルギーを要するという問題がある。
However, since a large amount of energy is required to recover a low concentration formic acid solution generated from carbon dioxide and hydrogen through extraction and distillation, it is necessary to concentrate it with high efficiency and recover formic acid with a high yield.
The organic acid solutions obtained in Patent Documents 1 and 2 are acidic, and in the conventional technique, a basic formic acid solution is acidified with a cation exchange resin, and the formic acid is extracted with an extractant containing a specific amine. has not been considered.
Further, according to the findings of the present inventors, when an anion exchange resin is used to concentrate a basic formic acid solution, the amount of formic acid adsorbed is small, and the concentration efficiency is not satisfactory.
The methods described in Patent Documents 3 and 4 for recovering formic acid from a low-concentration formic acid solution by only extraction and distillation have a problem in that they require a large amount of energy.
そこで、本発明は、ギ酸イオンを含む塩基性溶液を、高効率で濃縮し、高収率でギ酸を回収し得るギ酸回収方法を提供する。 Therefore, the present invention provides a formic acid recovery method that can concentrate a basic solution containing formate ions with high efficiency and recover formic acid with a high yield.
本発明者らは、ギ酸イオンを含む塩基性溶液を、高効率で濃縮し、高収率でギ酸を回収することを目的として、鋭意検討を重ねた結果、ギ酸イオンを含む塩基性溶液を陽イオン交換樹脂と接触させて、ギ酸イオンを含む酸性溶液とし、特定のアミンを含む抽出剤を用いることが重要であることを見出し、本発明を完成するに至った。 The present inventors have conducted intensive studies with the aim of concentrating a basic solution containing formate ions with high efficiency and recovering formic acid with a high yield. They discovered that it is important to contact an ion exchange resin to form an acidic solution containing formate ions and to use an extractant containing a specific amine, and have completed the present invention.
即ち、本発明の一態様は、ギ酸イオンを含む塩基性溶液を、陽イオン交換樹脂と接触させて、ギ酸イオンを含む酸性溶液を得る第一の工程、及び、
上記酸性溶液と、少なくとも式（１）で表されるアミンを含む抽出剤とを接触させて得られる抽出液からギ酸を回収する第二の工程、を含むギ酸回収方法に関する。
式（１） ＮＲ１Ｒ２Ｒ３
（Ｒ１及びＲ２はそれぞれ独立して炭素数５以上のアルキル基を表し、Ｒ３は水素原子またはアルキル基を表す。）
That is, one aspect of the present invention includes a first step of contacting a basic solution containing formate ions with a cation exchange resin to obtain an acidic solution containing formate ions, and
The present invention relates to a method for recovering formic acid, which includes a second step of recovering formic acid from an extract obtained by contacting the acidic solution with an extractant containing at least an amine represented by formula (1).
Formula (1) NR 1 R 2 R 3
(R 1 and R 2 each independently represent an alkyl group having 5 or more carbon atoms, and R 3 represents a hydrogen atom or an alkyl group.)
本発明の一態様において、上記第一の工程において、上記酸性溶液のｐＨが７．０未満であることが好ましい。 In one aspect of the present invention, in the first step, the pH of the acidic solution is preferably less than 7.0.
本発明の一態様において、上記陽イオン交換樹脂は強酸性陽イオン交換樹脂であってもよい。 In one embodiment of the present invention, the cation exchange resin may be a strongly acidic cation exchange resin.
本発明の一態様において、上記Ｒ３はアルキル基を表すことが好ましい。 In one aspect of the present invention, R 3 preferably represents an alkyl group.
本発明の一態様において、上記式（１）で表されるアミンの、コンピュータソフトウェアＨａｎｓｅｎ Ｓｏｌｕｂｉｌｉｔｙ Ｐａｒａｍｅｔｅｒｓ ｉｎ Ｐｒａｃｔｉｃｅ（ＨＳＰｉＰ）にて求めたハンセン溶解度パラメータにおける分散項（δＤ）は、１５．６以上であることが好ましい。 In one aspect of the present invention, the dispersion term (δD) of the amine represented by the above formula (1) in the Hansen solubility parameter determined using the computer software Hansen Solubility Parameters in Practice (HSPiP) is 15.6 or more. It is preferable.
本発明の一態様において、上記Ｒ１、Ｒ２、及びＲ３の炭素数の合計は１５以上であることが好ましい。 In one aspect of the present invention, the total number of carbon atoms in R 1 , R 2 , and R 3 is preferably 15 or more.
本発明の一態様において、上記抽出剤が、さらに炭素数１０～５０のアルコールを含むことが好ましい。 In one aspect of the present invention, it is preferable that the extractant further contains an alcohol having 10 to 50 carbon atoms.
本発明の一態様において、上記第二の工程は、上記酸性溶液と上記抽出液とを分液する工程、及び上記抽出液を分解蒸留することにより、ギ酸を回収する工程を含むことが好ましい。 In one aspect of the present invention, the second step preferably includes a step of separating the acidic solution and the extract, and a step of recovering formic acid by decomposing and distilling the extract.
本発明によれば、ギ酸イオンを含む塩基性溶液を高効率で濃縮し、高収率でギ酸を回収し得る、ギ酸回収方法を提供することができる。 According to the present invention, it is possible to provide a formic acid recovery method that can concentrate a basic solution containing formate ions with high efficiency and recover formic acid with a high yield.
以下、本発明の実施形態について、詳細に説明する。
本発明の実施形態に係るギ酸回収方法は、
ギ酸イオンを含む塩基性溶液を、陽イオン交換樹脂と接触させて、ギ酸イオンを含む酸性溶液を得る第一の工程、及び、
前記酸性溶液と、少なくとも式（１）で表わされるアミン（単にアミンと称する場合がある）を含む抽出剤とを接触させて、前記酸性水溶液からギ酸を回収する第二の工程を含む。
式（１） ＮＲ１Ｒ２Ｒ３
（Ｒ１及びＲ２はそれぞれ独立して炭素数５以上のアルキル基を表し、Ｒ３は水素原子またはアルキル基を表す。）
Embodiments of the present invention will be described in detail below.
The formic acid recovery method according to the embodiment of the present invention includes:
A first step of contacting a basic solution containing formate ions with a cation exchange resin to obtain an acidic solution containing formate ions, and
The method includes a second step of contacting the acidic solution with an extractant containing at least an amine represented by formula (1) (sometimes simply referred to as amine) to recover formic acid from the acidic aqueous solution.
Formula (1) NR 1 R 2 R 3
(R 1 and R 2 each independently represent an alkyl group having 5 or more carbon atoms, and R 3 represents a hydrogen atom or an alkyl group.)
〔第一の工程〕
第一の工程は、ギ酸イオンを含む塩基性溶液を陽イオン交換樹脂と接触させて、ギ酸イオンを含む酸性溶液を得る工程である。この工程により、ギ酸イオンを含む塩基性溶液中に存在する金属イオン等の陽イオンが、陽イオン交換樹脂に吸着され、水素イオンが陽イオン交換樹脂より放出されて、ギ酸イオンを含む酸性溶液（以下、酸性ギ酸溶液と称する場合がある）が得られる。
ここで、ギ酸イオンを含む塩基性溶液を酸性化せずに、第二の工程によりギ酸の抽出を行うと、ギ酸イオンがアルカリ金属等との塩を形成しているため抽出ができない。また、陽イオン交換樹脂を用いずに塩酸等の鉱酸を用いて塩基性ギ酸溶液を酸性化すると、ギ酸溶液が更に低濃度になるという問題がある。さらに、ギ酸に比べて鉱酸が強固にアミンと塩を形成してしまうために、第二の工程における抽出効率が低下し、ギ酸の回収率が悪化する。
[First step]
The first step is a step of bringing a basic solution containing formate ions into contact with a cation exchange resin to obtain an acidic solution containing formate ions. Through this step, cations such as metal ions present in the basic solution containing formate ions are adsorbed by the cation exchange resin, and hydrogen ions are released from the cation exchange resin, and the acidic solution containing formate ions ( (hereinafter sometimes referred to as acidic formic acid solution) is obtained.
Here, if formic acid is extracted in the second step without acidifying the basic solution containing formate ions, extraction cannot be performed because formate ions form a salt with an alkali metal or the like. Furthermore, when a basic formic acid solution is acidified using a mineral acid such as hydrochloric acid without using a cation exchange resin, there is a problem that the formic acid solution becomes even lower in concentration. Furthermore, since mineral acids more strongly form salts with amines than formic acid, the extraction efficiency in the second step decreases and the recovery rate of formic acid deteriorates.
塩基性ギ酸溶液におけるギ酸濃度は、イオン交換樹脂を使用する観点から、３０質量％以下が好ましく、１０質量％以下がより好ましい。塩基性ギ酸溶液におけるギ酸濃度の下限値としては、特に限定はないが、０．０１質量％以上が好ましく、０．１質量％以上がより好ましい。 From the viewpoint of using an ion exchange resin, the formic acid concentration in the basic formic acid solution is preferably 30% by mass or less, more preferably 10% by mass or less. The lower limit of the formic acid concentration in the basic formic acid solution is not particularly limited, but is preferably 0.01% by mass or more, more preferably 0.1% by mass or more.
塩基性ギ酸溶液の溶媒としては、塩基性ギ酸溶液が均一となる溶媒であればよく、特に制限は無いが、水、メタノール、エタノール、Ｎ，Ｎ－ジメチルホルムアミド、ジメチルスルホキシド、テトラヒドロフラン、ベンゼン、トルエン、及びこれらの混合溶媒等が挙げられ、水を含むことが好ましく、水であることがより好ましい。
塩基性ギ酸溶液中には、炭酸水素リチウム、炭酸水素ナトリウム、炭酸水素カリウム、炭酸水素セシウム、水酸化カリウム、水酸化ナトリウム、ジアザビシクロウンデセン、又はトリエチルアミン等を含有することが好ましく、炭酸水素ナトリウム、又は炭酸水素カリウムを含有することがより好ましい。
塩基性ギ酸溶液のｐＨとしては、８．０より大きいことが好ましく、８．５以上がより好ましい。また、塩基性溶液のｐＨは、酸性化効率化の観点から、１２以下が好ましく、１１以下がより好ましい。
The solvent for the basic formic acid solution is not particularly limited as long as it makes the basic formic acid solution uniform, but examples include water, methanol, ethanol, N,N-dimethylformamide, dimethyl sulfoxide, tetrahydrofuran, benzene, and toluene. , and mixed solvents thereof, preferably containing water, more preferably water.
The basic formic acid solution preferably contains lithium hydrogen carbonate, sodium hydrogen carbonate, potassium hydrogen carbonate, cesium hydrogen carbonate, potassium hydroxide, sodium hydroxide, diazabicycloundecene, triethylamine, etc. It is more preferable to contain sodium or potassium hydrogen carbonate.
The pH of the basic formic acid solution is preferably higher than 8.0, more preferably 8.5 or higher. Further, the pH of the basic solution is preferably 12 or less, more preferably 11 or less, from the viewpoint of increasing acidification efficiency.
塩基性ギ酸溶液を陽イオン交換樹脂に接触させる方式に特に制限は無く、陽イオン交換樹脂をカラムに充填して塩基性ギ酸溶液を通液するカラム式でも、陽イオン交換樹脂を塩基性ギ酸溶液中に分散させて攪拌するバッチ式でもよい。好ましくは、連続して行えるカラム式の方法で行う。 There are no particular restrictions on the method of bringing the basic formic acid solution into contact with the cation exchange resin. A batch method may be used in which the liquid is dispersed in the liquid and stirred. Preferably, it is carried out in a column method which can be carried out continuously.
カラム式を用いる場合、カラムに塩基性ギ酸溶液を接触させる条件としては、例えば、製造効率の観点から、好ましくは空塔速度（ＳＶ）＝０．１ｈｒ－１以上、より好ましくは０．２ｈｒ－１以上、更に好ましくは、０．５ｈｒ－１以上を挙げることができる。また、十分に酸性化を行う観点から、好ましくは空塔速度（ＳＶ）＝５０ｈｒ－１以下、より好ましくは１０ｈｒ－１以下、更に好ましくは、８ｈｒ－１以下を挙げることができる。
塩基性ギ酸溶液は、陽イオン交換樹脂の総イオン交換容量に対して、塩基性ギ酸溶液中の陽イオンの量が０．０１～１倍量となる量を通液することにより行うことが好ましい。また、カラムからの流出液中のｐＨをモニタしながら、酸性化を確認することが好ましい。
When using a column method, the conditions for contacting the basic formic acid solution with the column are, for example, from the viewpoint of production efficiency, preferably superficial velocity (SV) = 0.1 hr -1 or more, more preferably 0.2 hr - 1 or more, more preferably 0.5 hr -1 or more. In addition, from the viewpoint of sufficient acidification, the superficial velocity (SV) is preferably 50 hr -1 or less, more preferably 10 hr -1 or less, and even more preferably 8 hr -1 or less.
The basic formic acid solution is preferably passed through in an amount such that the amount of cations in the basic formic acid solution is 0.01 to 1 times the total ion exchange capacity of the cation exchange resin. . Moreover, it is preferable to confirm acidification while monitoring the pH in the effluent from the column.
また、バッチ式を用いる場合には、塩基性ギ酸溶液に陽イオン交換樹脂を加えた後、一定時間撹拌後、陽イオン交換樹脂を取り除く方法が例示できる。
塩基性ギ酸溶液に陽イオン交換樹脂を接触させる時間としては、十分に酸性化を行う観点から、１０分以上が好ましく、２０分以上がより好ましい。また、製造効率の観点から、５時間以下が好ましく、２時間以下がより好ましい。
陽イオン交換樹脂の総イオン交換容量と、塩基性ギ酸溶液の陽イオン量との比率は、塩基性ギ酸溶液中の陽イオン量に対し、陽イオン交換樹脂の総イオン交換容量を、好ましくは１倍以上、より好ましくは５倍以上、更に好ましくは１０倍以上を例示することができる。
In addition, when using a batch method, an example is a method in which a cation exchange resin is added to a basic formic acid solution, stirred for a certain period of time, and then the cation exchange resin is removed.
The time for contacting the cation exchange resin with the basic formic acid solution is preferably 10 minutes or more, more preferably 20 minutes or more, from the viewpoint of sufficient acidification. Moreover, from the viewpoint of production efficiency, the time is preferably 5 hours or less, and more preferably 2 hours or less.
The ratio between the total ion exchange capacity of the cation exchange resin and the amount of cations in the basic formic acid solution is such that the total ion exchange capacity of the cation exchange resin is preferably 1 to the amount of cations in the basic formic acid solution. Examples include times or more, more preferably 5 times or more, still more preferably 10 times or more.
陽イオン交換樹脂としては、スルホン酸基等の強酸基を有する強酸性陽イオン交換樹脂や、カルボキシル基、ホスホン酸基、ホスフィン酸基等の弱酸基を有する弱酸性陽イオン交換樹脂等が挙げられる。
強酸性陽イオン交換樹脂としては、例えば、デュオライト（登録商標）Ｃ２０ＪＨ、Ｃ２５５ＬＦＨ、Ｃ２６ＴＲＨ（以上住友ケムテックス社製）、ダイヤイオン（登録商標）ＳＫ１Ｂ、ＳＫ１０４、ＳＫ１１０、ＰＫ２０８、ＰＫ２１２、ＰＫ２１６（以上、三菱化学社製）等が挙げられる。
弱酸性陽イオン交換樹脂としては、例えば、ダイヤイオン（登録商標）ＷＫ１０、ＷＫ１１、ＷＫ１００、ＷＫ４０Ｌ（以上、三菱化学社製）が挙げられる。
中でも、陽イオン交換樹脂としては、陽イオンの吸着能力が高い点から強酸性陽イオン交換樹脂であることが好ましい。
第一の工程により得られる酸性ギ酸溶液のｐＨは、最終的に得られるギ酸溶液の濃縮効果をより高くする観点から、７．０未満が好ましく、６．０以下がより好ましく、５．０以下が更に好ましく、４．０以下が特に好ましい。また、酸性ギ酸溶液のｐＨは、第二の工程におけるギ酸の抽出効率及び回収率の観点から、１．０以上が好ましく、２．０以上がより好ましく、３．０以上が更に好ましい。ｐＨは、陽イオン交換樹脂の種類、使用量、接触条件等により調整が可能である。
Examples of the cation exchange resin include strongly acidic cation exchange resins having strong acid groups such as sulfonic acid groups, and weakly acidic cation exchange resins having weak acid groups such as carboxyl groups, phosphonic acid groups, and phosphinic acid groups. .
Examples of strong acidic cation exchange resins include Duolite (registered trademark) C20JH, C255LFH, C26TRH (manufactured by Sumitomo Chemtex), Diaion (registered trademark) SK1B, SK104, SK110, PK208, PK212, PK216 (manufactured by Sumitomo Chemtex), manufactured by Mitsubishi Chemical Corporation).
Examples of the weakly acidic cation exchange resin include Diaion (registered trademark) WK10, WK11, WK100, and WK40L (all manufactured by Mitsubishi Chemical Corporation).
Among these, the cation exchange resin is preferably a strongly acidic cation exchange resin because of its high ability to adsorb cations.
The pH of the acidic formic acid solution obtained in the first step is preferably less than 7.0, more preferably 6.0 or less, and 5.0 or less, from the viewpoint of increasing the concentration effect of the formic acid solution finally obtained. is more preferable, and 4.0 or less is particularly preferable. Moreover, from the viewpoint of extraction efficiency and recovery rate of formic acid in the second step, the pH of the acidic formic acid solution is preferably 1.0 or more, more preferably 2.0 or more, and even more preferably 3.0 or more. The pH can be adjusted depending on the type of cation exchange resin, the amount used, contact conditions, etc.
陽イオン交換樹脂の粒径は、好ましくは０．１ｍｍ以上、より好ましくは０．２ｍｍ以上であり、特に好ましくは０．３ｍｍ以上である。また、陽イオン交換樹脂の粒径は、好ましくは２ｍｍ以下、より好ましくは１．５ｍｍ以下であり、特に好ましくは１．２ｍｍ以下である。 The particle size of the cation exchange resin is preferably 0.1 mm or more, more preferably 0.2 mm or more, particularly preferably 0.3 mm or more. Further, the particle size of the cation exchange resin is preferably 2 mm or less, more preferably 1.5 mm or less, particularly preferably 1.2 mm or less.
〔第二の工程〕
第二の工程は、酸性溶液と、少なくとも式（１）で表わされるアミンを含む抽出剤とを接触させて得られる抽出液からギ酸を回収する工程である。
この工程により、酸性溶液中のギ酸をアミン塩として高効率に抽出し、得られた抽出液を分解蒸留等の常法により、高い収率でギ酸を回収することができる。
酸性溶液と、少なくとも式（１）で表わされるアミンを含む抽出剤とを接触させる方法に特に制限はなく、公知の方法を用いることができる。接触方法としては、例えば、酸性溶液と抽出剤とを混合し、振とう、攪拌、ラインミキサー等を用いる方法、向流接触法等が挙げられる。
第二の工程は、前記酸性溶液と前記抽出液とを分液する工程（工程Ａ）、及び前記抽出液を分解蒸留することにより、ギ酸を回収する工程（工程Ｂ）を含むことが好ましい。
[Second process]
The second step is a step of recovering formic acid from an extract obtained by contacting an acidic solution with an extractant containing at least an amine represented by formula (1).
Through this step, formic acid in an acidic solution can be extracted with high efficiency as an amine salt, and the resulting extract can be used in a conventional method such as decomposition distillation to recover formic acid in high yield.
There is no particular restriction on the method of bringing the acidic solution into contact with the extractant containing at least the amine represented by formula (1), and any known method can be used. Examples of the contact method include a method of mixing an acidic solution and an extractant and using shaking, stirring, a line mixer, etc., and a countercurrent contact method.
The second step preferably includes a step of separating the acidic solution and the extract (step A), and a step of recovering formic acid by decomposing and distilling the extract (step B).
［アミン］
本発明の実施形態に係る抽出剤は、少なくとも式（１）で表わされるアミンを含む。
式（１） ＮＲ１Ｒ２Ｒ３
（Ｒ１及びＲ２はそれぞれ独立して炭素数５以上のアルキル基を表し、Ｒ３は水素原子またはアルキル基を表す。）
[Amine]
The extractant according to the embodiment of the present invention contains at least an amine represented by formula (1).
Formula (1) NR 1 R 2 R 3
(R 1 and R 2 each independently represent an alkyl group having 5 or more carbon atoms, and R 3 represents a hydrogen atom or an alkyl group.)
Ｒ１及びＲ２がそれぞれ表わす炭素数５以上のアルキル基は、炭素数が５以上であれば直鎖アルキル基であっても分岐アルキル基であってもよい。Ｒ１及びＲ２のアルキル基の炭素数がそれぞれ４以下であると、アミンの水への溶解度が大きくなり、抽出効率が低下する。
Ｒ１及びＲ２はそれぞれ独立して、炭素数７以上のアルキル基を表すことが好ましく、炭素数１０以上のアルキル基を表すことがより好ましい。Ｒ１及びＲ２が表わすアルキル基の炭素数の上限値は、２０以下が好ましく、１５以下がより好ましい。炭素数が２０以下であれば、融点が高くなりすぎず、溶媒等へ溶解しやすいため抽出温度を高くする必要がなく、エネルギー消費を最小限に抑えられるため取扱いに優れる。
The alkyl group having 5 or more carbon atoms each represented by R 1 and R 2 may be a straight-chain alkyl group or a branched alkyl group as long as the alkyl group has 5 or more carbon atoms. When the number of carbon atoms in each of the alkyl groups of R 1 and R 2 is 4 or less, the solubility of the amine in water increases and the extraction efficiency decreases.
R 1 and R 2 each independently preferably represent an alkyl group having 7 or more carbon atoms, more preferably an alkyl group having 10 or more carbon atoms. The upper limit of the number of carbon atoms in the alkyl group represented by R 1 and R 2 is preferably 20 or less, more preferably 15 or less. When the number of carbon atoms is 20 or less, the melting point is not too high and it is easily dissolved in a solvent, etc., so there is no need to raise the extraction temperature, and energy consumption can be minimized, making it easy to handle.
Ｒ１及びＲ２が表わすアルキル基は、具体的には、ペンチル基、へキシル基、へプチル基、オクチル基、ノニル基、デシル基、ウンデシル基、ドデシル基、トリデシル基、テトラデシル基、ペンタデシル基、ヘキサデシル基、ヘプタデシル基、オクタデシル基などが挙げられ、これらは直鎖状でも分岐していてもよく、直鎖状であることが好ましい。Ｒ１及びＲ２が表わすアルキル基は、好ましくは、ペンチル基、へキシル基、へプチル基、オクチル基、ノニル基、デシル基、ウンデシル基、ドデシル基であり、より好ましくはペンチル基、オクチル基、ドデシル基である。
Ｒ１及びＲ２はそれぞれ同一でも異なっていてもよいが、同一であることが好ましい。
Specifically, the alkyl group represented by R 1 and R 2 is a pentyl group, hexyl group, heptyl group, octyl group, nonyl group, decyl group, undecyl group, dodecyl group, tridecyl group, tetradecyl group, pentadecyl group. , hexadecyl group, heptadecyl group, octadecyl group, etc., which may be linear or branched, and are preferably linear. The alkyl group represented by R 1 and R 2 is preferably a pentyl group, hexyl group, heptyl group, octyl group, nonyl group, decyl group, undecyl group, or dodecyl group, more preferably a pentyl group or an octyl group. , is a dodecyl group.
R 1 and R 2 may be the same or different, but are preferably the same.
Ｒ３は水素原子またはアルキル基を表す。Ｒ３が表わすアルキル基は、直鎖アルキル基であっても分岐アルキル基であってもよく、炭素数１～２０のアルキル基であることが好ましく、炭素数５～２０のアルキル基であることがより好ましく、炭素数７～２０のアルキル基であることがさらに好ましい。
具体的には、メチル基、エチル基、プロピル基、ブチル基、ペンチル基、へキシル基、へプチル基、オクチル基、ノニル基、デシル基、ウンデシル基、ドデシル基、トリデシル基、テトラデシル基、ペンタデシル基、ヘキサデシル基、ヘプタデシル基、オクタデシル基などが挙げられ、これらは直鎖状でも分岐していてもよい。好ましくは、ペンチル基、へキシル基、へプチル基、オクチル基、ノニル基、デシル基、ウンデシル基、ドデシル基であり、より好ましくはペンチル基、オクチル基、ドデシル基である。
Ｒ３はアルキル基を表すことが好ましい。Ｒ３がアルキル基を表す場合、式（１）で表されるアミンは三級アミンとなり、ギ酸回収の際に減圧条件下であっても脱水が起こりにくく、アミドの生成を抑制するためギ酸の収率が飛躍的に向上する。
R 3 represents a hydrogen atom or an alkyl group. The alkyl group represented by R 3 may be a straight-chain alkyl group or a branched alkyl group, preferably an alkyl group having 1 to 20 carbon atoms, and preferably an alkyl group having 5 to 20 carbon atoms. is more preferred, and even more preferably an alkyl group having 7 to 20 carbon atoms.
Specifically, methyl group, ethyl group, propyl group, butyl group, pentyl group, hexyl group, heptyl group, octyl group, nonyl group, decyl group, undecyl group, dodecyl group, tridecyl group, tetradecyl group, pentadecyl group. group, hexadecyl group, heptadecyl group, octadecyl group, etc., and these may be linear or branched. Preferred are pentyl group, hexyl group, heptyl group, octyl group, nonyl group, decyl group, undecyl group, and dodecyl group, and more preferred are pentyl group, octyl group, and dodecyl group.
Preferably, R 3 represents an alkyl group. When R 3 represents an alkyl group, the amine represented by formula (1) becomes a tertiary amine, and dehydration is unlikely to occur even under reduced pressure conditions during formic acid recovery, and in order to suppress the formation of amide, formic acid is The yield is dramatically improved.
Ｒ１、Ｒ２、及びＲ３の炭素数の合計は１５以上であることが好ましく、２０以上であることがより好ましい。Ｒ１、Ｒ２、及びＲ３の炭素数の合計は、抽出溶媒への溶解性を上げる観点から６０以下であることが好ましく、５０以下であることがより好ましい。 The total number of carbon atoms in R 1 , R 2 , and R 3 is preferably 15 or more, more preferably 20 or more. The total number of carbon atoms in R 1 , R 2 , and R 3 is preferably 60 or less, more preferably 50 or less, from the viewpoint of increasing solubility in the extraction solvent.
式（１）で表わされるアミンとして、具体的には、ジドデシルアミン、ジドデシルメチルアミン、ジドデシルエチルアミン、ジドデシルプロピルアミン、ジウンデシルアミン、ジウンデシルメチルアミン、ジウンデシルエチルアミン、ジウンデシルプロピルアミン、ジデシルアミン、ジデシルメチルアミン、ジデシルエチルアミン、ジデシルプロピルアミン、ジノニルアミン、ジノニルメチルアミン、ジノニルエチルアミン、ジノニルプロピルアミン、ジオクチルアミン、ジオクチルメチルアミン、ジオクチルエチルアミン、ジオクチルプロピルアミン、トリドデシルアミン、トリウンデシルアミン、トリデシルアミン、トリノニルアミン、トリオクチルアミン、トリアミルアミン等が挙げられ、ジドデシルメチルアミン、トリドデシルアミン、トリアミルアミン、ジオクチルメチルアミン、ジドデシルアミンが好ましく、ジドデシルメチルアミン、トリドデシルアミンがより好ましい。
式（１）で表わされるアミンは１種を単独で用いてもよいし、２種以上を一緒に用いてもよい。
Specific examples of the amine represented by formula (1) include didodecylamine, didodecylmethylamine, didodecylethylamine, didodecylpropylamine, diundecylamine, diundecylmethylamine, diundecylethylamine, and diundecylpropylamine. , didecylamine, didecylmethylamine, didecylethylamine, didecylpropylamine, dinonylamine, dinonylmethylamine, dinonylethylamine, dinonylpropylamine, dioctylamine, dioctylmethylamine, dioctylethylamine, dioctylpropylamine, tridodecylamine , triundecylamine, tridecylamine, trinonylamine, trioctylamine, triamylamine, etc., with didodecylmethylamine, tridodecylamine, triamylamine, dioctylmethylamine, and didodecylamine being preferred. Dodecylmethylamine and tridodecylamine are more preferred.
One type of amine represented by formula (1) may be used alone, or two or more types may be used together.
式（１）で表されるアミンの、コンピュータソフトウェアＨａｎｓｅｎ Ｓｏｌｕｂｉｌｉｔｙ Ｐａｒａｍｅｔｅｒｓ ｉｎ Ｐｒａｃｔｉｃｅ （ＨＳＰｉＰ）にて求めたハンセン溶解度パラメータにおける分散項（δＤ）は、１５．６以上であることが好ましい。
δＤが１５．６以上であれば、水の分散項（δＤ＝１５．５）と数値が離れるため好ましい。δＤはより好ましくは１５．９以上であり、更に好ましくは１６．０以上である。また、抽出溶媒の溶解性の観点から１７．０以下であることが好ましく、１６．５以下であることがより好ましい。
The dispersion term (δD) of the amine represented by formula (1) in the Hansen solubility parameter determined using the computer software Hansen Solubility Parameters in Practice (HSPiP) is preferably 15.6 or more.
It is preferable that δD is 15.6 or more because the numerical value is different from the water dispersion term (δD=15.5). δD is more preferably 15.9 or more, still more preferably 16.0 or more. Further, from the viewpoint of solubility of the extraction solvent, it is preferably 17.0 or less, more preferably 16.5 or less.
式（１）で表わされるアミンの使用量は、抽出効率の観点から酸性溶液中のギ酸に対して、１．０当量以上であることが好ましく、１．２当量以上であることがより好ましく、１．５当量以上であることがさらに好ましい。また、アミンの使用量は、環境負荷低減の観点から３．０当量以下であることが好ましく、２．８当量以下であることがより好ましく、２．５当量以下であることがさらに好ましい。 The amount of the amine represented by formula (1) to be used is preferably 1.0 equivalent or more, more preferably 1.2 equivalent or more, based on formic acid in the acidic solution from the viewpoint of extraction efficiency. More preferably, the amount is 1.5 equivalents or more. Further, the amount of amine used is preferably 3.0 equivalents or less, more preferably 2.8 equivalents or less, and even more preferably 2.5 equivalents or less from the viewpoint of reducing environmental load.
［抽出溶媒］
式（１）で表されるアミンが液体の場合、溶媒として用いることもできる。しかし、アミンの処理やコスト等の観点から式（１）で表されるアミンとは別に、抽出溶媒を用いてもよい。
抽出溶媒としては、酸性溶液と相分離する溶媒であることが好ましく、酸性溶液が水を溶媒とする場合は、水に不溶の抽出溶媒であることが好ましい。
[Extraction solvent]
When the amine represented by formula (1) is a liquid, it can also be used as a solvent. However, from the viewpoint of amine treatment, cost, etc., an extraction solvent may be used in addition to the amine represented by formula (1).
The extraction solvent is preferably a solvent that undergoes phase separation from the acidic solution, and when the acidic solution uses water as a solvent, it is preferably an extraction solvent that is insoluble in water.
水に不溶の抽出溶媒としては、水にほとんど溶解せず、前記アミンを溶解あるいは微分散できるものであれば特に制限はない。水への溶解度及び前記アミンを溶解させる観点から疎水性のアルコールが好ましく、炭素数１０以上のアルコールがより好ましい。また、アルコールの水酸基は１つであることが好ましく、直鎖または分岐鎖構造を有する一価の飽和アルコールもしくは芳香環を有する一価のアルコールが好ましい。 The water-insoluble extraction solvent is not particularly limited as long as it is hardly soluble in water and can dissolve or finely disperse the amine. From the viewpoint of solubility in water and dissolving the amine, hydrophobic alcohols are preferred, and alcohols having 10 or more carbon atoms are more preferred. Further, it is preferable that the alcohol has one hydroxyl group, and a monohydric saturated alcohol having a linear or branched structure or a monohydric alcohol having an aromatic ring is preferable.
直鎖アルコールとして具体的には、１－オクタノール、１－ノナノール、１－デカノール、１－ウンデカノール、１－ドデカノール、１－トリデカノール、１－テトラデカノール、１－ペンタデカノール、１－ヘキサデカノール、１－ヘプタデカノール、１－オクタデカノール、１－ノナデカノール、１－エイコサノール、１－ヘンエイコサノール、１－ドコサノール、１－テトラコサノール、１－ヘキサコサノール等が挙げられる。 Specifically, the straight chain alcohols include 1-octanol, 1-nonanol, 1-decanol, 1-undecanol, 1-dodecanol, 1-tridecanol, 1-tetradecanol, 1-pentadecanol, and 1-hexadecanol. , 1-heptadecanol, 1-octadecanol, 1-nonadecanol, 1-eicosanol, 1-heneicosanol, 1-docosanol, 1-tetracosanol, 1-hexacosanol and the like.
分岐鎖構造を有する飽和アルコールとしては、２－オクチル－１－ドデカノールなどが挙げられる。また不飽和アルコールとしては、ｔｒａｎｓ－２－ドデセノール、ｔｒａｎｓ－２－トリデセン－１－オール、ｔｒａｎｓ－９－オクタデセノール、オレイルアルコール、ｃｉｓ，ｃｉｓ－９，１２－オクタデカジエン－１－オール、ｃｉｓ－１３－ドコセノールなどが挙げられる。
芳香環を有するアルコールとしては、ジフェニルカルビノールなどが挙げられる。
Examples of the saturated alcohol having a branched chain structure include 2-octyl-1-dodecanol. Examples of unsaturated alcohols include trans-2-dodecenol, trans-2-tridecen-1-ol, trans-9-octadecenol, oleyl alcohol, cis,cis-9,12-octadecadien-1-ol, cis- Examples include 13-docosenol.
Examples of the alcohol having an aromatic ring include diphenylcarbinol.
これらのアルコールの中でも、疎水性が強く、融点が低いために扱いやすい２－オクチル－１－ドデカノールが特に好ましい。
これら炭素数が１０以上のアルコールは単独で使用してもよいし、２種以上を組み合わせて使用してもよい。また、本発明の効果を損なわない範囲であれば炭素数１０未満のアルコールが混入してもよい。
式（１）で表されるアミンと、抽出溶媒とを混合または溶解した液中のアミン濃度は抽出効率の観点から５質量％以上であることが好ましく、７質量％以上であることがより好ましく、１０質量％以上であることがさらに好ましい。また、５０質量％以下であることが好ましく、４５質量％以下であることがより好ましく、４０質量％以下であることがさらに好ましい。
Among these alcohols, 2-octyl-1-dodecanol is particularly preferred because it is easy to handle due to its strong hydrophobicity and low melting point.
These alcohols having 10 or more carbon atoms may be used alone or in combination of two or more. Furthermore, alcohols having less than 10 carbon atoms may be mixed as long as the effects of the present invention are not impaired.
The amine concentration in the mixed or dissolved solution of the amine represented by formula (1) and the extraction solvent is preferably 5% by mass or more, more preferably 7% by mass or more from the viewpoint of extraction efficiency. , more preferably 10% by mass or more. Further, it is preferably 50% by mass or less, more preferably 45% by mass or less, and even more preferably 40% by mass or less.
ギ酸が抽出除去された後の酸性溶液を排水として処理する場合に、この排水にアミン化合物が溶出していると、アミン化合物は一般に難分解性で阻害性もあるため好ましくない。また、排水にアミン化合物及びアルコールが溶出すれば、それはそのままロスすることになり、さらに水溶液中の全有機体炭素（ＴＯＣ）濃度も上昇させる。従って、本発明に用いるアミン及びアルコールは水への溶解度がなるべく小さいことが好ましい。 When treating the acidic solution after formic acid has been extracted and removed as wastewater, if amine compounds are eluted into the wastewater, it is not preferable because amine compounds are generally difficult to decompose and have inhibiting properties. Furthermore, if the amine compound and alcohol are eluted into the waste water, they will be lost as is, and the total organic carbon (TOC) concentration in the aqueous solution will also increase. Therefore, it is preferable that the amine and alcohol used in the present invention have as low a solubility in water as possible.
［その他成分］
本発明の実施形態にかかる抽出剤は、式（１）で表されるアミン、及び任意成分として使用してもよい抽出溶媒の他に、必要に応じてその他の成分を含んでいても良い。
[Other ingredients]
In addition to the amine represented by formula (1) and the extraction solvent that may be used as an optional component, the extractant according to the embodiment of the present invention may contain other components as necessary.
［工程Ａ］
工程Ａは、酸性溶液と抽出液とを分液する工程である。
ギ酸が溶解している塩基性溶液と、前記アミンを含む抽出剤とは公知の方法で接触させ、ギ酸をアミン塩として抽出剤へ抽出し、得られた抽出液と塩基性溶液とを分離する。
抽出後の酸性溶液と抽出液は、公知の方法で２層に分離することができる。連続抽出塔で分離してもよく、静置型の分離槽を使用してもよい。ギ酸が抽出された抽出液は蒸留工程へ送られ、ギ酸、水分、アミン、抽出溶媒（アルコール）をそれぞれ分離することができる。
[Process A]
Step A is a step of separating the acidic solution and the extract.
A basic solution in which formic acid is dissolved is brought into contact with the extractant containing the amine by a known method, the formic acid is extracted into the extractant as an amine salt, and the obtained extract and the basic solution are separated. .
The acidic solution and extract after extraction can be separated into two layers by a known method. Separation may be carried out in a continuous extraction column, or a stationary separation tank may be used. The extract from which formic acid has been extracted is sent to a distillation process to separate formic acid, water, amine, and extraction solvent (alcohol).
［工程Ｂ］
工程Ｂは、抽出液を分解蒸留することにより、ギ酸を回収する工程である。
抽出溶液相（有機相）からギ酸を回収する方法には特に制限はなく、分解蒸留が挙げられる。分解蒸留により、ギ酸のアミン塩をギ酸とアミンに分解し、ギ酸を蒸留により回収することができる。分解蒸留は必要に応じて減圧下で行ってもよい。分解蒸留で回収する場合の温度、圧力はギ酸が蒸留で溜出回収できる条件であれば特に制限はない。
[Process B]
Step B is a step of recovering formic acid by subjecting the extract to decomposition distillation.
There are no particular limitations on the method for recovering formic acid from the extraction solution phase (organic phase), and decomposition distillation may be used. By decomposition distillation, the amine salt of formic acid can be decomposed into formic acid and amine, and formic acid can be recovered by distillation. Decomposition distillation may be carried out under reduced pressure if necessary. The temperature and pressure for recovery by decomposition distillation are not particularly limited as long as formic acid can be recovered by distillation.
本発明の実施形態にかかるアミン、及び任意成分として用いても良いアルコールは分子量が大きく、ギ酸や水よりは高沸点である。従って、分解蒸留操作では先にギ酸と少量の水を低沸成分として溜去させることができる。抽出液に水が含まれる場合、蒸留の際にはまず主に水を溜去した後、さらに温度を上げてギ酸を溜去するという２段蒸留を用いると高純度のギ酸を効率的に回収できる。 The amine according to embodiments of the present invention and the alcohol that may be used as an optional component have a large molecular weight and a higher boiling point than formic acid or water. Therefore, in the cracking distillation operation, formic acid and a small amount of water can be distilled off first as low-boiling components. If the extract contains water, high-purity formic acid can be efficiently recovered by using two-stage distillation, in which the water is primarily distilled off first, and then the formic acid is further distilled off by raising the temperature. can.
水とギ酸は、沸点の差が大きくないが、抽出液に水が含まれる場合であっても、蒸留により分離が可能である。水はアミンとの相互作用がほとんどないが、ギ酸はアミンとの相互作用のため溜出温度が高くなっているためと考えられる。さらに、蒸留を減圧下で行えば水はより低温で溜出するようになるが、ギ酸の溜出温度はほとんど変わらず、沸点差が大きくなったような状態になると考えられる。
分解蒸留における温度は回収効率の観点から１００℃以上であることが好ましく、１２０℃以上であることがより好ましく、１４０℃以上であることがさらに好ましい。また、２５０℃以下であることが好ましく、２３０℃以下であることがより好ましく、２００℃以下であることがさらに好ましい。
分解蒸留における圧力は回収効率の観点から０．１ｍｍＨｇ以上であることが好ましく、０．５ｍｍＨｇ以上であることがより好ましく、１ｍｍＨｇ以上であることがさらに好ましい。また、３００ｍｍＨｇ以下であることが好ましく、２５０ｍｍＨｇ以下であることがより好ましく、２００ｍｍＨｇ以下であることがさらに好ましい。
Water and formic acid do not have a large difference in boiling point, but even if the extract contains water, they can be separated by distillation. This is thought to be because water has almost no interaction with amines, but formic acid has a high distillation temperature due to its interaction with amines. Furthermore, if distillation is performed under reduced pressure, water will be distilled out at a lower temperature, but the distillation temperature of formic acid will hardly change, and it is thought that the difference in boiling points will become larger.
From the viewpoint of recovery efficiency, the temperature in decomposition distillation is preferably 100°C or higher, more preferably 120°C or higher, and even more preferably 140°C or higher. Further, the temperature is preferably 250°C or lower, more preferably 230°C or lower, and even more preferably 200°C or lower.
From the viewpoint of recovery efficiency, the pressure in decomposition distillation is preferably 0.1 mmHg or higher, more preferably 0.5 mmHg or higher, and even more preferably 1 mmHg or higher. Further, it is preferably 300 mmHg or less, more preferably 250 mmHg or less, and even more preferably 200 mmHg or less.
本実施形態の方法によれば、塩基性ギ酸溶液を陰イオン交換樹脂と接触させて、ギ酸イオンを樹脂に吸着、及び溶出させるよりも、はるかに効率良くギ酸溶液を濃縮することができる。また、溶出液として得られた濃縮ギ酸溶液を、特定のアミンを含む抽出液により抽出し、定法に従いさらに減圧蒸留等に付することによって、水、鉱酸及び有機溶剤等を除去し、目的とするギ酸を高い回収率で得ることができる。 According to the method of this embodiment, a formic acid solution can be concentrated much more efficiently than when a basic formic acid solution is brought into contact with an anion exchange resin and formic acid ions are adsorbed and eluted from the resin. In addition, the concentrated formic acid solution obtained as the eluate is extracted with an extract containing a specific amine, and further subjected to vacuum distillation according to a standard method to remove water, mineral acids, organic solvents, etc. Formic acid can be obtained with a high recovery rate.
以下、実施例及び比較例を示して本発明を詳細に説明する。ただし、本発明はこれらの実施例に限定されるものではない。 Hereinafter, the present invention will be explained in detail by showing Examples and Comparative Examples. However, the present invention is not limited to these examples.
〔実施例１〕
下記のとおり塩基性ギ酸溶液の濃縮を行った。
[Example 1]
The basic formic acid solution was concentrated as described below.
＜第一の工程＞
炭酸水素ナトリウム（和光純薬製）６７．２ｇに水を加え１Ｌとし、攪拌し、０．８ｍｏｌ／Ｌ炭酸水素ナトリウム水溶液を得た。純度９８％ギ酸（和光純薬製）２．５５ｇに９７．４５ｇの０．８ｍｏｌ／Ｌ炭酸水素ナトリウム水溶液を加え、攪拌し、２．５質量％のギ酸を含んだ塩基性ギ酸溶液を得た（ｐＨ９．１）。上記で得られた塩基性ギ酸溶液１０ｇを、樹脂Ａ（強酸性陽イオン交換樹脂 デュオライトＣ２０ＪＨ、住化ケムテックス社製）１０ｇと混合して酸性化した後、濾別して酸性ギ酸溶液を得た。得られた酸性ギ酸溶液のｐＨを自動滴定装置 ＣＯＭ－１７５０Ｓ（平沼産業製）により測定したところ３．４であった。
<First step>
Water was added to 67.2 g of sodium hydrogen carbonate (manufactured by Wako Pure Chemical Industries, Ltd.) to make 1 L, and the mixture was stirred to obtain a 0.8 mol/L aqueous sodium hydrogen carbonate solution. 97.45 g of 0.8 mol/L sodium bicarbonate aqueous solution was added to 2.55 g of 98% pure formic acid (manufactured by Wako Pure Chemical Industries, Ltd.) and stirred to obtain a basic formic acid solution containing 2.5% by mass of formic acid. (pH 9.1). 10 g of the basic formic acid solution obtained above was acidified by mixing with 10 g of resin A (strongly acidic cation exchange resin Duolite C20JH, manufactured by Sumika Chemtex), and then filtered to obtain an acidic formic acid solution. The pH of the obtained acidic formic acid solution was measured using an automatic titrator COM-1750S (manufactured by Hiranuma Sangyo) and found to be 3.4.
＜第二の工程＞
ジドデシルメチルアミン（東京化成工業株式会社製）０．３９９ｇを抽出溶媒である２－オクチル－１－ドデカノール（東京化成工業株式会社製）１．６０１ｇと混合して得た抽出剤（アミン当量（ギ酸との比）：１．０）に、前記酸性ギ酸溶液を加え、激しく２００回振り混ぜた。その後静置すると、２層に分離したので、上層（有機相）と下層（水相）を分け取り、それぞれ成分分析を行った。水相中に残存するギ酸をＨＰＬＣ（高速液体クロマトグラフィー）により定量することで、抽出率を算出した。
ＨＰＬＣは以下の条件により行った。定量用標準物質にはギ酸（和光純薬製）濃度が０．００１～１質量％となるよう調整したギ酸水溶液を用いた。
装置：ＬＣ－ＭＳ２０１０ＥＶ（島津製作所製）
カラム：ＹＭＣ－Ｔｒｉａｒｔ Ｃ１８（３．０ｍｍΦ×１５ｃｍ，平均粒径５μｍ，平均細孔径１２ｎｍ）
カラム温度：３７℃
移動相：Ａ液 ０．１％Ｈ３ＰＯ４：アセトニトリル＝９５：５（体積比），
Ｂ液 アセトニトリル
グラジエント条件：０～５分，Ｂ液０％（ホールド）→５～５．０１分，Ｂ液０～９５％（グラジエント）→５．０１～１０分，Ｂ液９５％（ホールド）→１０～１０．０１分，Ｂ液９５～０％（グラジエント）→１０．０１～２０分，Ｂ液０％（ホールド）
流速：０．４２５ｍＬ／ｍｉｎ
検出：ＵＶ２１０ｎｍ
<Second process>
An extractant (amine equivalent ( The acidic formic acid solution was added to the mixture (ratio to formic acid): 1.0), and the mixture was vigorously shaken 200 times. After that, when it was allowed to stand still, it was separated into two layers, so the upper layer (organic phase) and lower layer (aqueous phase) were separated and component analysis was performed on each. The extraction rate was calculated by quantifying the formic acid remaining in the aqueous phase by HPLC (high performance liquid chromatography).
HPLC was performed under the following conditions. As a standard substance for quantitative determination, a formic acid aqueous solution (manufactured by Wako Pure Chemical Industries, Ltd.) whose concentration was adjusted to 0.001 to 1% by mass was used.
Equipment: LC-MS2010EV (manufactured by Shimadzu Corporation)
Column: YMC-Triart C18 (3.0 mmΦ x 15 cm, average particle size 5 μm, average pore size 12 nm)
Column temperature: 37℃
Mobile phase: Solution A 0.1% H 3 PO 4 :acetonitrile = 95:5 (volume ratio),
B solution Acetonitrile Gradient conditions: 0 to 5 minutes, B solution 0% (hold) → 5 to 5.01 minutes, B solution 0 to 95% (gradient) → 5.01 to 10 minutes, B solution 95% (hold) →10-10.01 minutes, B liquid 95-0% (gradient) →10.01-20 minutes, B liquid 0% (hold)
Flow rate: 0.425mL/min
Detection: UV210nm
得られたギ酸抽出層（有機相）を減圧下蒸留することにより高濃度のギ酸を得た。まず常圧下１００℃に設定することで、少量含まれる水をまず留去させた。その後、圧力１０ｍｍＨｇ、温度１７０℃に設定することで、高濃度のギ酸を得た。 Highly concentrated formic acid was obtained by distilling the obtained formic acid extraction layer (organic phase) under reduced pressure. First, by setting the temperature to 100° C. under normal pressure, a small amount of water contained was first distilled off. Thereafter, a high concentration of formic acid was obtained by setting the pressure to 10 mmHg and the temperature to 170°C.
〔実施例２〕
第二の工程におけるジドデシルメチルアミンの量を０．５９９ｇ（アミン当量：１．５）に変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 2]
The same procedure as in Example 1 was carried out except that the amount of didodecylmethylamine in the second step was changed to 0.599 g (amine equivalent: 1.5) and the amount of extraction solvent was changed as shown in Table 1. Formic acid was recovered. The results are shown in Table 1.
〔実施例３〕
第二の工程におけるジドデシルメチルアミンの量を０．７９９ｇ（アミン当量：２．０）に変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 3]
The same procedure as in Example 1 was carried out except that the amount of didodecylmethylamine in the second step was changed to 0.799 g (amine equivalent: 2.0) and the amount of extraction solvent was changed as shown in Table 1. Formic acid was recovered. The results are shown in Table 1.
〔実施例４〕
第二の工程において抽出溶媒を使用しなかったこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 4]
Formic acid was recovered in the same manner as in Example 1 except that no extraction solvent was used in the second step. The results are shown in Table 1.
〔実施例５〕
第二の工程においてジドデシルメチルアミン０．３９９ｇをトリドデシルアミン０．５６７ｇに変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 5]
Formic acid was recovered in the same manner as in Example 1, except that in the second step, 0.399 g of didodecylmethylamine was changed to 0.567 g of tridodecylamine, and the amount of extraction solvent was changed as described in Table 1. . The results are shown in Table 1.
〔実施例６〕
第二の工程においてジドデシルメチルアミン０．３９９ｇをトリアミルアミン０．２４７ｇに変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 6]
Formic acid was recovered in the same manner as in Example 1, except that in the second step, 0.399 g of didodecylmethylamine was changed to 0.247 g of triamylamine, and the amount of extraction solvent was changed as described in Table 1. . The results are shown in Table 1.
〔実施例７〕
第二の工程においてジドデシルメチルアミン０．３９９ｇをメチルジオクチルアミン０．２７８ｇに変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 7]
Formic acid was recovered in the same manner as in Example 1, except that in the second step, 0.399 g of didodecylmethylamine was changed to 0.278 g of methyldioctylamine, and the amount of extraction solvent was changed as described in Table 1. . The results are shown in Table 1.
〔実施例８〕
第二の工程においてジドデシルメチルアミン０．３９９ｇをジドデシルアミン０．３８４ｇに変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 8]
Formic acid was recovered in the same manner as in Example 1, except that in the second step, 0.399 g of didodecylmethylamine was changed to 0.384 g of didodecylamine, and the amount of extraction solvent was changed as described in Table 1. . The results are shown in Table 1.
〔実施例９〕
第二の工程において抽出溶媒である２－オクチル－１－ドデカノールを１－オクタノールに変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 9]
Formic acid was recovered in the same manner as in Example 1, except that in the second step, the extraction solvent 2-octyl-1-dodecanol was changed to 1-octanol. The results are shown in Table 1.
〔実施例１０〕
＜第一の工程＞
炭酸水素カリウム（和光純薬製）２００．２ｇに水を加え１Ｌとし、攪拌し、２ｍｏｌ／Ｌ炭酸水素カリウム水溶液を得た。純度９８％ギ酸（和光純薬製）２．５ｇに９７．５ｇの２ｍｏｌ／Ｌ炭酸水素カリウム水溶液を加え、攪拌し、２．５質量％のギ酸を含んだ塩基性ギ酸溶液を得た（ｐＨ９．１）。上記で得られた塩基性ギ酸溶液１０ｇを、樹脂Ａ（強酸性陽イオン交換樹脂 デュオライトＣ２０ＪＨ、住化ケムテックス社製）１０ｇと混合して酸性化した後、濾別して酸性ギ酸溶液を得た。得られた酸性ギ酸溶液のｐＨを自動滴定装置 ＣＯＭ－１７５０Ｓ（平沼産業製）により測定したところ３．４であった。
第二の工程は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 10]
<First step>
Water was added to 200.2 g of potassium hydrogen carbonate (manufactured by Wako Pure Chemical Industries, Ltd.) to make 1 L, and the mixture was stirred to obtain a 2 mol/L potassium hydrogen carbonate aqueous solution. 97.5 g of 2 mol/L potassium bicarbonate aqueous solution was added to 2.5 g of 98% pure formic acid (manufactured by Wako Pure Chemical Industries, Ltd.) and stirred to obtain a basic formic acid solution containing 2.5% by mass of formic acid (pH 9). .1). 10 g of the basic formic acid solution obtained above was acidified by mixing with 10 g of resin A (strongly acidic cation exchange resin Duolite C20JH, manufactured by Sumika Chemtex), and then filtered to obtain an acidic formic acid solution. The pH of the obtained acidic formic acid solution was measured using an automatic titrator COM-1750S (manufactured by Hiranuma Sangyo) and found to be 3.4.
In the second step, formic acid was recovered in the same manner as in Example 1. The results are shown in Table 1.
〔実施例１１〕
第一の工程において樹脂Ａを樹脂Ｂ（弱酸性陽イオン交換樹脂 ダイヤイオンＷＫ４０Ｌ、三菱ケミカル株式会社製）に変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Example 11]
Formic acid was recovered in the same manner as in Example 1, except that resin A was changed to resin B (weakly acidic cation exchange resin Diaion WK40L, manufactured by Mitsubishi Chemical Corporation) in the first step. The results are shown in Table 1.
〔比較例１〕
第一の工程において調製した塩基性ギ酸溶液を、酸性化せずに第二の工程に用いたこと以外は実施例１と同様の操作を行った結果、ギ酸を回収することができなかった。
[Comparative example 1]
As a result of performing the same operation as in Example 1 except that the basic formic acid solution prepared in the first step was used in the second step without acidifying it, formic acid could not be recovered.
〔比較例２〕
第一の工程において、陽イオン交換樹脂を用いず、塩基性ギ酸溶液１０ｇと３６質量％塩酸水溶液３ｇとを混合して酸性化し、酸性ギ酸溶液を得たこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Comparative example 2]
In the first step, 10 g of a basic formic acid solution and 3 g of a 36% by mass hydrochloric acid aqueous solution were mixed and acidified to obtain an acidic formic acid solution, without using a cation exchange resin. Formic acid was recovered. The results are shown in Table 1.
〔比較例３〕
第一の工程において、抽出剤にアミンを用いず、抽出溶媒である２－オクチル－１－ドデカノール（東京化成工業株式会社製）２．０００ｇを用いたこと以外は実施例１と同様の操作を行った結果、ギ酸を回収することができなかった。
[Comparative example 3]
In the first step, the same operation as in Example 1 was carried out, except that 2.000 g of 2-octyl-1-dodecanol (manufactured by Tokyo Chemical Industry Co., Ltd.) was used as the extraction solvent instead of using an amine as the extractant. As a result, formic acid could not be recovered.
〔比較例４〕
第二の工程においてジドデシルメチルアミン０．３９９ｇをトリプロピルアミン０．１５５ｇに変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様にしてギ酸を回収した。結果を表１に示す。
[Comparative example 4]
Formic acid was recovered in the same manner as in Example 1, except that in the second step, 0.399 g of didodecylmethylamine was changed to 0.155 g of tripropylamine, and the amount of extraction solvent was changed as described in Table 1. . The results are shown in Table 1.
〔比較例５〕
第二の工程においてジドデシルメチルアミン０．３９９ｇをジメチルオクタデシルアミン０．３２３ｇに変更し、抽出溶媒の量を表１に記載の通り変更したこと以外は実施例１と同様の操作を行った結果、ギ酸を回収することができなかった。
[Comparative example 5]
Results of performing the same operation as in Example 1 except that in the second step, 0.399 g of didodecylmethylamine was changed to 0.323 g of dimethyloctadecylamine, and the amount of extraction solvent was changed as shown in Table 1. , formic acid could not be recovered.
表１から分かるように、実施例１～１１は、第一の工程で陽イオン交換樹脂を用いて酸性化したことにより、第二の工程におけるギ酸の抽出率が高く、総合ギ酸回収率が高い。
実施例１～７、９～１１は、第二の工程で三級アミンを用いたため、実施例８と比較して分解蒸留におけるギ酸の回収率が高く、総合ギ酸回収率が非常に高い。
比較例１は、陽イオン交換樹脂による第一の工程を実施しなかったため、第二の工程においてギ酸の抽出ができず、ギ酸が回収できなかった。
比較例２は第一の工程に塩酸を用いたため、実施例１～１１と比較してギ酸の抽出率、及び分解蒸留におけるギ酸の回収率が低く、総合ギ酸回収率が低い結果となった。
第二の工程でアミンを用いなかった比較例３は、ギ酸の回収ができなかった。
比較例４は、第二の工程で用いたアミンのアルキル基の炭素数が少ないため、また、ＨＳＰにおけるδＤが低いため、実施例１～１１と比較してギ酸の抽出率、及び分解蒸留におけるギ酸の回収率が低く、総合ギ酸回収率が非常に低い結果となった。
比較例５は、第二の工程で用いたアミンの疎水性が低いため水相と有機相が分離せず、ギ酸が抽出できず、ギ酸の回収ができなかった。
As can be seen from Table 1, in Examples 1 to 11, by acidifying using a cation exchange resin in the first step, the extraction rate of formic acid in the second step was high, and the overall formic acid recovery rate was high. .
In Examples 1 to 7 and 9 to 11, since a tertiary amine was used in the second step, the recovery rate of formic acid in decomposition distillation was higher than in Example 8, and the overall recovery rate of formic acid was extremely high.
In Comparative Example 1, since the first step using a cation exchange resin was not performed, formic acid could not be extracted in the second step, and formic acid could not be recovered.
Since Comparative Example 2 used hydrochloric acid in the first step, the extraction rate of formic acid and the recovery rate of formic acid in decomposition distillation were lower than in Examples 1 to 11, resulting in a lower overall formic acid recovery rate.
In Comparative Example 3, in which no amine was used in the second step, formic acid could not be recovered.
In Comparative Example 4, the number of carbon atoms in the alkyl group of the amine used in the second step is small, and the δD in HSP is low, so the extraction rate of formic acid and decomposition distillation are lower than those in Examples 1 to 11. The recovery rate of formic acid was low, resulting in a very low overall formic acid recovery rate.
In Comparative Example 5, because the amine used in the second step had low hydrophobicity, the aqueous phase and organic phase were not separated, and formic acid could not be extracted and recovered.
Claims (8)
前記酸性溶液と、少なくとも式（１）で表されるアミンを含む抽出剤とを接触させて得られる抽出液からギ酸を回収する第二の工程、
を含み、
前記塩基性溶液は、炭酸水素ナトリウム水溶液、又は炭酸水素カリウム水溶液であり、
前記塩基性溶液のｐＨは８．０超である、ギ酸回収方法。
式（１） ＮＲ１Ｒ２Ｒ３
（Ｒ１及びＲ２はそれぞれ独立して炭素数５以上のアルキル基を表し、Ｒ３は水素原子またはアルキル基を表す。） A first step of contacting a basic solution containing 0.01 to 30% by mass of formic acid with a cation exchange resin to obtain an acidic solution containing formate ions, and
a second step of recovering formic acid from an extract obtained by contacting the acidic solution with an extractant containing at least an amine represented by formula (1);
including;
The basic solution is an aqueous sodium hydrogen carbonate solution or an aqueous potassium hydrogen carbonate solution,
A method for recovering formic acid , wherein the basic solution has a pH of more than 8.0 .
Formula (1) NR 1 R 2 R 3
(R 1 and R 2 each independently represent an alkyl group having 5 or more carbon atoms, and R 3 represents a hydrogen atom or an alkyl group.)
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