[특허]Optimized liquid-phase oxidation

[미국특허] Optimized liquid-phase oxidation 원문보기

IPC분류정보
국가/구분	United States(US) Patent 등록
국제특허분류(IPC7판)	C07C-051/16
출원번호	US-0703331 (2010-02-10)
등록번호	US-8501986 (2013-08-06)
발명자 / 주소	Wonders, Alan George Lin, Robert Partin, Lee Reynolds de Vreede, Marcel Strasser, Wayne Scott
출원인 / 주소	Grupo Petrotemex, S.A. de C.V.
대리인 / 주소	Oblon, Spivak, McClelland, Maier & Neustadt, L.L.P.
인용정보	피인용 횟수 : 1 인용 특허 : 150

초록 ▼

Disclosed is an optimized process and apparatus for more efficiently and economically carrying out the liquid-phase oxidation of an oxidizable compound. Such liquid-phase oxidation is carried out in a bubble column reactor that provides for a highly efficient reaction at relatively low temperatures. When the oxidized compound is para-xylene and the product from the oxidation reaction is crude terephthalic acid (CTA), such CTA product can be purified and separated by more economical techniques than could be employed if the CTA were formed by a conventional high-temperature oxidation process.

대표청구항 ▼

1. A process for producing terephthalic acid, said process comprising: (a) oxidizing para-xylene in a liquid phase of a multi-phase reaction medium contained in a bubble column reactor to thereby form crude terephthalic acid, wherein said reaction medium has a maximum height (H) and a minimum width occurring above H/5 from the bottom of said reaction zone (Wmin), wherein the total upright surface area of said reactor that contacts said reaction medium is greater than 3.25 WminH; and(b) oxidizing said crude terephthalic acid in a secondary oxidation reactor to thereby form purer terephthalic acid. 2. The process of claim 1 wherein the total upright surface area of said reactor that contacts said reaction medium is in the range of from about 3.5 WminH to about 20 WminH. 3. The process of claim 1 wherein the total upright surface area of said reactor that contacts said reaction medium is in the range of from about 4 WminH to about 15 WminH. 4. The process of claim 1 wherein the total upright surface area of said reactor that contacts said reaction medium is in the range of from 5 WminH to about 10 WminH. 5. The process of claim 1 wherein said oxidizing in said secondary oxidation reactor decreases the average concentration of 4-CBA present in said crude terephthalic acid by at least about 200 ppmw to thereby form said purer terephthalic acid. 6. The process of claim 1 wherein said crude terephthalic acid has an average 4-CBA concentration of at least about 400 ppmw and said purer terephthalic acid has an average 4-CBA concentration of less than about 400 ppmw. 7. The process of claim 1 wherein said oxidizing in said secondary oxidation reactor decreases the average concentration of 4-CBA in said crude terephthalic acid by at least about 400 ppmw to thereby form said purer terephthalic acid, wherein said crude terephthalic acid has an average 4-CBA concentration of at least about 800 ppmw and said purer terephthalic acid has an average 4-CBA concentration of less than about 250 ppmw. 8. The process of claim 1 wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature at least about 10° C. greater than the average temperature of said oxidizing in said bubble column reactor. 9. The process of claim 1 wherein said oxidizing in said bubble column reactor is carried out at an average temperature in the range of from about 125 to about 200° C., wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature in the range of from about 160 to about 240° C. 10. The process of claim 1 wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature in the range of from about 20 to about 80° C. greater than the average temperature of said oxidizing in said bubble column reactor, wherein said oxidizing in said bubble column reactor is carried out at an average temperature in the range of from about 140 to about 180° C., wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature in the range of from about 180 to about 220° C. 11. The process of claim 1 wherein a substantial portion of said crude terephthalic acid exists as solid crude terephthalic acid particles having an average BET surface area of at least about 0.6 meters squared per gram. 12. The process of claim 11 wherein said solid crude terephthalic acid particles have an average particle size in the range of from about 20 to about 150 microns. 13. The process of claim 12 wherein a substantial portion of said solid crude terephthalic acid particles are formed of a plurality of agglomeraged sub-particles having an average particle size in the range of from about 0.5 to about 30 microns. 14. The process of claim 13 wherein said solid crude terephthalic acid particles have an average particle size in the range of from about 30 to about 120 microns, wherein said sub-particles have an average particle size in the range of from about 1 to about 15 microns. 15. The process of claim 1 wherein said process further comprises recovering an initial slurry comprising a mother liquor and said crude terephthalic acid from said bubble column reactor, wherein said process further comprises replacing at least about 50 weight percent of said mother liquor in said initial slurry with a replacement solvent to thereby provide a solvent-exchanged slurry comprising said replacement solvent and said crude terephthalic acid, wherein said process further comprises introducing said solvent-exchanged slurry into said secondary oxidation reactor. 16. A process for producing terephthalic acid, said process comprising: (a) oxidizing para-xylene in a liquid phase of a multi-phase reaction medium contained in a bubble column reactor to thereby form crude terephthalic acid, wherein said reaction medium has a maximum height (H) and a minimum width occurring above H/5 from the bottom of said reaction zone (Wmin), wherein the total upright surface area of said reactor that contacts said reaction medium is greater than 3.25 WminH; and(b) oxidizing said crude terephthalic acid in a secondary oxidation reactor to thereby form purer terephthalic acid, wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature at least about 10° C. greater than the average temperature of said oxidizing in said bubble column reactor and decreases the average concentration of 4-CBA present in said crude terephthalic acid by at least about 200 ppmw to thereby form said purer terephthalic acid. 17. The process of claim 16 wherein the total upright surface area of said reactor that contacts said reaction medium is in the range of from about 3.5 WminH to about 20 WminH. 18. The process of claim 16 wherein the total upright surface area of said reactor that contacts said reaction medium is in the range of from about 4 WminH to about 15 WminH.

이 특허에 인용된 특허 (150) 인용/피인용 타임라인 분석

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Tsong-Dar Vincent Lin, Process of purifying and producing high purity aromatic polycarboxylic acids.
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Lin Tsong-Dar Vincent, Process of purifying and producing high purity aromatic polycarboxylic acids and derivatives thereof.
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Graham, Derek Alexander; Hamley, Paul Anthony; Oliver, Raymond; Poliakoff, Martyn; Woodcock, Duncan; Ilkenhans, Thomas, Production of aromatic carboxylic acids.
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Park Chang-Man (Naperville IL) Micklewright Donald G. (Broadview Heights OH), Production of fiber-grade terephthalic acid.
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Sikkenga, David L.; Pandya, Alpen K.; Zaenger, Ian C.; Abrams, Kenneth J.; Bartos, Thomas M., Production of high purity aromatic carboxylic acid by oxidation in benzoic acid and water solvent.
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Mikitenko Paul,FRX ; Hotier Gerard,FRX, Production of para-xylene from an effluent from paraselective toluene disproportionation using a crystallization process combined with simulated moving bed adsorption.
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Hanotier Jacques D. V. (Lasne Chapelle St. Lambert BEX) Hanotier-Bridoux Monique J. S. (Lasne Chapelle St. Lambert BEX), Production of terephthalic acid.
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Ramachandran Ramakrishnan (Allendale NJ) Sethna Rustam H. (New Brunswick NJ) Tamhankar Satish S. (Scotch Plains NJ), Production of terephthalic acid.
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Turner John Arthur,GBX ; Royall David John,GBX ; Hugall Duncan Stuart,GBX ; Jones Graham Howard,GBX ; Woodcock Duncan Charles,GBX, Production of terephthalic acid.
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Roby Anne Katherine (Golden\s Bridge NY), Production of terephthalic acid with excellent optical properties through the use of pure or nearly pure oxygen as the o.
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Brumbaugh, David L., Property prediction using residual stepwise regression.
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Guentert Josef,DEX ; Frey Hansjoerg,DEX, Radial piston pump for high pressure fuel delivery.
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Dassel Mark William ; Vassiliou Eustathios, Reaction control by regulating internal condensation inside a reactor.
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Schoengen Anton (Witten DEX) Schroeder Heinrich (Dortmund-Syburg DEX), Reactor for the oxidation of alkyl aromatics with oxygen-containing gases in the liquid phase.
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Zeitlin Martin A. (Naperville IL) McQuillin Stafford J. (Mount Pleasant SC), Recycle of vaporized solvent in liquid phase oxidation of an alkyl aromatic.
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Kinnari Keijo J.,NOX ; Schanke Dag,NOX, Regeneration of Fischer-Tropsch catalysts by using synthesis gas at a low flow rate.
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Culross, Claude Clarence, Slurry catalyst rejuvenation in-situ in slurry reactor.
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Degeorge Charles W. ; Chang Min, Slurry hydrocarbon synthesis with external product filtration.
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Giacobbe Thomas J. (Skillman NJ) Williams ; Jr. Thomas N. (Plainfield NJ) Horn James M. (Richmond VA), Solvent and catalyst recovery and recycle in the manufacture of phenoxybenzoic acid.
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Janulis Rose M. (Downers Grove IL), Solvent recovery during production of aromatic polycarboxylic acids.
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Nowicki Neal R. (Naperville IL) Lowry ; Jr. James D. (Bolingbrook IL), Staged aromatics oxidation in aqueous systems.
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Cheng Alan Tat Yan, Stationary vortex system for direct injection of supplemental reactor oxygen.
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Forsyth Malcolm W. (Cleveland GB2) Hind Stephen H. (Derbyshire GB2), Sterile aerobic fermentation process.
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Odueyungbo,Oluwaseyi A.; Espinoza,Rafael L.; Mohedas,Sergio R.; Ortego, Jr.,James Dale; Ortego,Beatrice C.; Goodwin,Ralph T.; Harkins,Todd H., Systems and methods for catalyst/hydrocarbon product separation.
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Kingsley Jeffrey P. (Newburgh NY) Roby Anne K. (Peekskill NY), Terephthalic acid production using evaporative cooling.
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Fisher Jay A. (Naperville IL), Terephthalic acid recovery by continuous flash crystallization.
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Machado Reinaldo Mario, Two stage reactor for continuous three phase slurry hydrogenation and method of operation.
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Faivre Michel,FRX ; Martin Nathalie,FRX ; Boisdon Vincent,FRX, Unit for the treatment of water by ozonization, and a corresponding installation for the production of ozonized water.
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Strock Thomas Wayne ; Gohara Wadie Fawzy, Wet scrubber oxidation air sparger arrangement.
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Quintero Barajas, José Gabriel; Ramírez Sosa, Pamela Shantal; Escobar López, Alfredo; Medina Valencia, Verona; Bulbarela Croda, Arturo; Morán Delgado, Bertha, Energy and environmentally integrated method for production of aromatic dicarboxylic acids by oxidation.
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IPC	Description
A	생활필수품
A62	인명구조; 소방(사다리 E06C)
A62B	인명구조용의 기구, 장치 또는 방법(특히 의료용에 사용되는 밸브 A61M 39/00; 특히 물에서 쓰이는 인명구조 장치 또는 방법 B63C 9/00; 잠수장비 B63C 11/00; 특히 항공기에 쓰는 것, 예. 낙하산, 투출좌석 B64D; 특히 광산에서 쓰이는 구조장치 E21F 11/00)
A62B-1/08	.. 윈치 또는 풀리에 제동기구가 있는 것

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안내	총 건의 자료가 검색되었습니다. 다운받으실 자료의 인덱스를 입력하세요. (1-10,000) 검색결과의 순서대로 최대 10,000건 까지 다운로드가 가능합니다. 데이타가 많을 경우 속도가 느려질 수 있습니다.(최대 2~3분 소요) 다운로드 파일은 UTF-8 형태로 저장됩니다. 파일의 내용이 제대로 보이지 않을실 때는 웹브라우저 상단의 보기 -> 인코딩 -> 자동선택 여부를 확인하십시오. ~ Text(ASCII format) Excel format

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