KR880012519A - 고품질 테레프탈산의 제조방법 - Google Patents
고품질 테레프탈산의 제조방법 Download PDFInfo
- Publication number
- KR880012519A KR880012519A KR1019880004638A KR880004638A KR880012519A KR 880012519 A KR880012519 A KR 880012519A KR 1019880004638 A KR1019880004638 A KR 1019880004638A KR 880004638 A KR880004638 A KR 880004638A KR 880012519 A KR880012519 A KR 880012519A
- Authority
- KR
- South Korea
- Prior art keywords
- oxidation
- terephthalic acid
- post
- oxidation reaction
- temperature
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C63/00—Compounds having carboxyl groups bound to a carbon atoms of six-membered aromatic rings
- C07C63/14—Monocyclic dicarboxylic acids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
- C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
내용 없음
Description
본 내용은 요부공개 건이므로 전문내용을 수록하지 않았음
제1도는 본 발명의 실시예에서 사용한 반응기의 유통도이다. 제2도는 실시예1에서 얻은 고온 후산화전의 페테프탈산 결정의 분광 반사율을 나타내는 그래프이다. 제3도는 실시예1에서 얻은 테레프탈산 결정의 분광 반사율을 나타내는 그래프이다.
Claims (21)
- p-크실렌을 아세트산 용매중에서 최소한 중금속 및 브롬으로 이루어진 촉매 의 존재하에 180~230℃의 온도에서 산소분자를 이용하여 산화시켜 최소한 95중량%의 p-크실렌을 테레프탈산으로 전환시키고, 임의로, 생성된 반응 혼합물을 제1산화 반응의 온도보다 낮은 온도에서 산소분자를 이용하여 저온 후산화시켜 하기에 정의한 분광 반사율이 70%이상이고 하기에 정의한 반사율 비율(400/500)이 0.92이상인 테레프탈산 입자를 함유하는 슬러리를 수득하고 ; 슬러리를 235~290℃의 온도에서 산소분자를 이용하여 고온 후산화시킨 후에 결정화하고;생성된 테레프탈산의 제조방법.분광분사율=백색광 조명법에 따라 측정한 파장500nm에서의 분광 분사율
- 제1항에 있어서, 회수된 고품질 테레프탈산이 70%이상의 분광분사율 및 0.96이상의 반사율 비율(400/500)을 가짐을 특징으로 하는 방법.
- 제1항에 있어서, 고온 후산화시킨 슬러리중의 테레프탈산 입자가 0.97이상의 반사율 비율(450/500)을 갖는 방법.
- 제1항에 있어서, 고온 후산화시킨 슬러리중의 테레프탈산 입자가 80%이상의 분광 반사율 및 0.93~0.98의 반사율 비율(400/500)을 갖는 방법.
- 제1항 또는 2항에 있어서, 회수된 테레프탈산이 0.985이상의 반사율 비율(450/500)을 갖는 방법.
- 제1항 또는 4항에 있어서, 회수한 테레프탈산이 80%이상의 분광 반사율 및 0.965~1.005의 반사율비율(400/500)을 갖는 방법.
- 제1항에 있어서, 촉매가 필수적으로 코발트, 망간 및 브롬으로 이루어진 삼원 촉매인 방법.
- 제1항에 있어서, 제1산화반응의 압력이 10~30Kg/cm2의 범위인 방법.
- 제1항에 있어서, 제1산화반응의 시간이 40~150분의 범위인 방법.
- 제1항에 있어서, 제1산화반응에서 배출된 기체중의 산소농도가 1.5~8부피%의 범위인 방법.
- 제1항에 있어서, 제1산화반응의 액산중의 물의 농도가 5~15중량%의 범위인 방법.
- 제1항에 있어서, 제1산화반응 중의 산소 분자 공급량이 p-크실렌 공급량의 3~100배몰인 방법.
- 제1항에 있어서, 저온 후산화를 제1산화반응 후에 수행하는 방법.
- 제1항 또는 13항에 있어서, 저온 후산화의 온도가 제1산화반응의 온도보다 2~30℃낮은 방법.
- 제1항 또는 13항에 있어서, 저온 후산화의 반응시간이 5~90분의 범위인 방법.
- 제1항 또는 13항에 있어서, 저온 후산화에 이용되는 산소분자의 공급량이 제1산화반응의 공급량의 1/10~1/1000인 방법.
- 제1항에 있어서, 고온 후산화의 온도가 240~280℃인 방법
- 제1항에 있어서, 고온 후산화의 압력이 30~100Kg/cm2인 방법.
- 제1항에 있어서, 고온 후산화에서 배출된 기체중의 산소 농도가 0.5부피% 이하인 방법.
- 제1항 또는 19항에 있어서, 고온 후산화반응에서 이용된 산소 분자의 공급량이 슬러리중의 테레프탈산의 양의 0.003~0.3몰배 범위인 방법.
- 제1항에 있어서, 결정화 도중에, 산소분자를 배출기체중의 산소농도가 2~8부피%로 되는 양으로 160~230℃ 구역의 슬러리에 공급하는 방법.※ 참고사항 : 최초출원 내용에 의하여 공개하는 것임.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP62101373A JP2504461B2 (ja) | 1987-04-24 | 1987-04-24 | 高品質テレフタル酸の製法 |
JP62-101373 | 1987-04-24 |
Publications (1)
Publication Number | Publication Date |
---|---|
KR880012519A true KR880012519A (ko) | 1988-11-28 |
Family
ID=14299009
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
KR1019880004638A KR880012519A (ko) | 1987-04-24 | 1988-04-23 | 고품질 테레프탈산의 제조방법 |
Country Status (4)
Country | Link |
---|---|
US (1) | US4877900A (ko) |
JP (1) | JP2504461B2 (ko) |
KR (1) | KR880012519A (ko) |
GB (1) | GB2204581B (ko) |
Families Citing this family (50)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5095142A (en) * | 1990-11-29 | 1992-03-10 | Amoco Corporation | Solvent recovery during production of aromatic polycarboxylic acids |
DE4334100C2 (de) * | 1992-10-13 | 2003-02-13 | Mitsubishi Chem Corp | Verfahren zur Herstellung hochreiner Terephthalsäure |
KR970000136B1 (ko) * | 1993-09-28 | 1997-01-04 | 브이.피. 유리예프 | 고순도 벤젠디카르복실산 이성질체의 제조방법 |
US6013835A (en) * | 1995-06-07 | 2000-01-11 | Hfm International, Inc. | Method and apparatus for preparing purified terephthalic acid |
US6054610A (en) * | 1995-06-07 | 2000-04-25 | Hfm International, Inc. | Method and apparatus for preparing purified terephthalic acid and isophthalic acid from mixed xylenes |
US5767311A (en) * | 1995-06-07 | 1998-06-16 | Glitsch International, Inc. | Method and apparatus for preparing purified terephtalic acid |
US5929274A (en) * | 1995-06-07 | 1999-07-27 | Hfm International, Inc. | Method to reduce carboxybenzaldehyde isomers in terephthalic acid or isophthalic acid |
US6657067B2 (en) | 2002-03-22 | 2003-12-02 | General Electric Company | Method for the manufacture of chlorophthalic anhydride |
US6649773B2 (en) | 2002-03-22 | 2003-11-18 | General Electric Company | Method for the manufacture of halophthalic acids and anhydrides |
US6657068B2 (en) | 2002-03-22 | 2003-12-02 | General Electric Company | Liquid phase oxidation of halogenated ortho-xylenes |
US7541489B2 (en) | 2004-06-30 | 2009-06-02 | Sabic Innovative Plastics Ip B.V. | Method of making halophthalic acids and halophthalic anhydrides |
US7683210B2 (en) | 2004-09-02 | 2010-03-23 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7495125B2 (en) | 2004-09-02 | 2009-02-24 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7608733B2 (en) | 2004-09-02 | 2009-10-27 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7504535B2 (en) | 2004-09-02 | 2009-03-17 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7507857B2 (en) | 2004-09-02 | 2009-03-24 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7589231B2 (en) | 2004-09-02 | 2009-09-15 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7692036B2 (en) | 2004-11-29 | 2010-04-06 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7572932B2 (en) | 2004-09-02 | 2009-08-11 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7586000B2 (en) | 2004-09-02 | 2009-09-08 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7482482B2 (en) | 2004-09-02 | 2009-01-27 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7741515B2 (en) | 2004-09-02 | 2010-06-22 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7399882B2 (en) | 2004-09-02 | 2008-07-15 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7371894B2 (en) | 2004-09-02 | 2008-05-13 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7390921B2 (en) | 2004-09-02 | 2008-06-24 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7910769B2 (en) | 2004-09-02 | 2011-03-22 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7381836B2 (en) | 2004-09-02 | 2008-06-03 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7608732B2 (en) | 2005-03-08 | 2009-10-27 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7568361B2 (en) | 2004-09-02 | 2009-08-04 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7582793B2 (en) | 2004-09-02 | 2009-09-01 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7563926B2 (en) | 2004-09-02 | 2009-07-21 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7692037B2 (en) | 2004-09-02 | 2010-04-06 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7572936B2 (en) | 2004-09-02 | 2009-08-11 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7361784B2 (en) | 2004-09-02 | 2008-04-22 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7550627B2 (en) * | 2005-03-08 | 2009-06-23 | Eastman Chemical Company | Processes for producing aromatic dicarboxylic acids |
RU2435754C2 (ru) | 2005-03-21 | 2011-12-10 | Бп Корпорейшн Норт Америка Инк. | Способ возврата энергии в процессе производства ароматических карбоновых кислот |
US7884232B2 (en) | 2005-06-16 | 2011-02-08 | Eastman Chemical Company | Optimized liquid-phase oxidation |
US7355068B2 (en) | 2006-01-04 | 2008-04-08 | Eastman Chemical Company | Oxidation system with internal secondary reactor |
US7358389B2 (en) | 2006-01-04 | 2008-04-15 | Eastman Chemical Company | Oxidation system employing internal structure for enhanced hydrodynamics |
US7420082B2 (en) | 2006-03-01 | 2008-09-02 | Eastman Chemical Company | Polycarboxylic acid production system employing hot liquor removal downstream of oxidative digestion |
US7326807B2 (en) | 2006-03-01 | 2008-02-05 | Eastman Chemical Company | Polycarboxylic acid production system with enhanced heating for oxidative digestion |
US20070208194A1 (en) | 2006-03-01 | 2007-09-06 | Woodruff Thomas E | Oxidation system with sidedraw secondary reactor |
US7816556B2 (en) | 2006-03-01 | 2010-10-19 | Eastman Chemical Company | Polycarboxylic acid production system employing enhanced multistage oxidative digestion |
US7393973B2 (en) | 2006-03-01 | 2008-07-01 | Eastman Chemical Company | Polycarboxylic acid production system with enhanced residence time distribution for oxidative digestion |
US7326808B2 (en) | 2006-03-01 | 2008-02-05 | Eastman Chemical Company | Polycarboxylic acid production system employing cooled mother liquor from oxidative digestion as feed to impurity purge system |
US7772424B2 (en) | 2006-03-01 | 2010-08-10 | Eastman Chemical Company | Polycarboxylic acid production system employing enhanced evaporative concentration downstream of oxidative digestion |
US7501537B2 (en) * | 2006-03-01 | 2009-03-10 | Eastman Chemical Company | Polycarboxylic acid production system employing oxidative digestion with reduced or eliminated upstream liquor exchange |
US8080685B2 (en) * | 2007-06-27 | 2011-12-20 | H R D Corporation | System and process for production of benzoic acids and phthalic acids |
US9205388B2 (en) * | 2007-06-27 | 2015-12-08 | H R D Corporation | High shear system and method for the production of acids |
EP3083543B1 (en) | 2013-12-18 | 2021-04-14 | Ineos Us Chemicals Company | Improved process for manufacturing aromatic carboxylic acids |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS59106435A (ja) * | 1982-12-10 | 1984-06-20 | Mitsubishi Chem Ind Ltd | 高純度テレフタル酸の製法 |
US4447646A (en) * | 1983-01-28 | 1984-05-08 | Eastman Kodak Company | Process for the purification of terephthalic acid |
JPS60233032A (ja) * | 1984-05-04 | 1985-11-19 | Kuraray Yuka Kk | 直接重合用に適したテレフタル酸の製造法 |
US4605763A (en) * | 1984-08-31 | 1986-08-12 | Eastman Kodak Company | Process for the purification of terephthalic acid |
-
1987
- 1987-04-24 JP JP62101373A patent/JP2504461B2/ja not_active Expired - Fee Related
-
1988
- 1988-03-31 GB GB8807731A patent/GB2204581B/en not_active Expired - Fee Related
- 1988-04-05 US US07/177,951 patent/US4877900A/en not_active Expired - Fee Related
- 1988-04-23 KR KR1019880004638A patent/KR880012519A/ko not_active Application Discontinuation
Also Published As
Publication number | Publication date |
---|---|
JP2504461B2 (ja) | 1996-06-05 |
GB2204581A (en) | 1988-11-16 |
GB8807731D0 (en) | 1988-05-05 |
JPS63267744A (ja) | 1988-11-04 |
GB2204581B (en) | 1991-02-06 |
US4877900A (en) | 1989-10-31 |
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