WO2012057437A2 - 1,3,5-트리옥산의 제조방법 - Google Patents
1,3,5-트리옥산의 제조방법 Download PDFInfo
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- WO2012057437A2 WO2012057437A2 PCT/KR2011/006061 KR2011006061W WO2012057437A2 WO 2012057437 A2 WO2012057437 A2 WO 2012057437A2 KR 2011006061 W KR2011006061 W KR 2011006061W WO 2012057437 A2 WO2012057437 A2 WO 2012057437A2
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- trioxane
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D323/00—Heterocyclic compounds containing more than two oxygen atoms as the only ring hetero atoms
- C07D323/04—Six-membered rings
- C07D323/06—Trioxane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/40—Extractive distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Definitions
- the present invention relates to a method for producing 1,3,5-trioxane using a reaction distillation column comprising a reactor, a distillation section and an extraction section.
- 1,3,5-trioxane is obtained by cyclization of formaldehyde in the presence of an acidic catalyst or a solid acid catalyst.
- the vapor comprising 1,3,5-trioxane obtained by the cyclization reaction is transferred from the reactor to the distillation column.
- the boiled 1,3,5-trioxane is concentrated in a distillation column and flowed out once, and the 1,3,5-trioxane vapor is extracted with an insoluble or insoluble organic solvent in water.
- the boiled 1,3,5-trioxane vapor in the distillation column is extracted with an organic solvent that is poorly or insoluble in water.
- a distillation column and an extraction column are configured to extract 1,3,5-trioxane, and the extract is recycled to the extraction tower as a solution containing a small amount of 1,3,5-trioxane in the rectification column.
- the present invention is a method for producing 1,3,5-trioxane, using a reaction distillation column including a reactor and an integrally formed distillation unit and extraction unit, 1,3,5-trioxane production efficiency is improved, It is intended to provide a method for preparing 5-trioxane.
- the present invention is a first preferred embodiment, the reactor 10; And a reaction distillation tower (20) comprising a distillation unit (21) and an extracting unit (22) formed integrally.
- the extracting unit (22) has 1,3, 1,3,5-Tree, characterized in that some of the phase separated in the stream exited to the top of the reaction distillation tower 20 during the 5-trioxane extraction is recycled to the top of the extractant feed stream of the extractor 22
- a method for preparing oxane is provided in that some of the phase separated in the stream exited to the top of the reaction distillation tower 20 during the 5-trioxane extraction is recycled to the top of the extractant feed stream of the extractor 22.
- formaldehyde concentration may be 15 wt% or less in the water phase separated from the top of the reaction distillation tower 20 by phase separation.
- FIG. 1 is a schematic diagram of a reaction distillation tower used in the preparation of 1,3,5-trioxane according to the present invention, in which a distillation unit and an extracting unit are integrally formed, and in a phase separated from a stream discharged to the top of the reaction distillation tower.
- Schematic diagram of a reaction distillation column showing a portion recycled to the top of the extractant feed stream of the extract.
- FIG. 2 is a schematic diagram of a reaction distillation column used for preparing 1,3,5-trioxane, and is a schematic diagram of a reaction distillation column configured by distillation and extraction.
- FIG 3 is a schematic diagram of a reaction distillation tower used for the preparation of 1,3,5-trioxane, the distillation unit and the extraction unit integrally, a part of the phase separated from the water phase separated from the stream flowing into the tower top of the reaction distillation column Schematic diagram of a reaction distillation column showing recycling to the bottom of the extractant feed stream.
- the present invention is a first preferred embodiment, a reactor; And a reaction distillation tower including a distillation unit and an extracting unit formed integrally with each other.
- Some of the water phase separated in the stream relates to a process for producing 1,3,5-trioxane, characterized in that it is recycled to the top of the extractant feed stream of the extract.
- the stream discharged to the sidecut portion of the reaction distillation column consisting of a distillation unit and an extraction unit phase-separates the oil phase and the aqueous phase, and then returns the water phase to the distillation unit of the distillation column, and simultaneously, the water supplied to the reactor passes through the distillation unit of the reaction distillation column.
- the extraction section for extracting, 5-trioxane, azeotropic with the extractant and flowing into the column top of the distillation column to separate the phases the aqueous phase is discharged out of the system, and the remaining water phase is recycled to the top of the extractant feed stream to form at the column top column.
- It relates to a method for producing 1,3,5-trioxane, which can increase the production efficiency of 1,3,5-trioxane by reducing the amount of formaldehyde released to the system without lowering the concentration of formaldehyde. .
- the method for producing 1,3,5-trioxane using a reaction distillation column including a reactor and a distillation unit and an extraction unit generally includes the following steps.
- the present invention uses the above-mentioned method for producing 1,3,5-trioxane, but (i) the distillation unit and the extraction unit included in the reaction distillation column are integral; And (ii) recycling the aqueous phase discharged to the top of the reaction distillation tower after extraction of 1,3,5-trioxane to the discharge or extraction section out of the system, when recycling to the extraction section, to the top of the extractant feed stream. do.
- the (2), (3) and (4) process is implemented in one distillation column, but in the discharge of water supplied to the reactor of (4) in the reactor to minimize the formaldehyde discharged accompanying
- the supplied water is azeotropic with the extractant in the extraction section of the reaction distillation column and flows to the top of the distillation column to separate the phases and then discharges part of the aqueous phase to the outside of the system. It is possible to increase the production efficiency of 1,3,5-trioxane by reducing the aldehyde concentration and reducing the amount of formaldehyde released to the system without being involved in the reaction.
- 1,3,5-trioxane is synthesized from formaldehyde under an acid catalyst.
- Formaldehyde which is a raw material of 1,3,5-trioxane, is supplied to the reactor 10, where 1,3,5-trioxane is synthesized by heating in the presence of an acid catalyst.
- Formaldehyde which is a reaction raw material for synthesizing the 1,3,5-trioxane, may include formaldehyde gas, formaldehyde aqueous solution, paraformaldehyde, and the like, but an aqueous formaldehyde solution may be used in view of ease of handling.
- the acid catalyst may be a homogeneous catalyst, it may be used a solid acid catalyst.
- the side solvent include mineral acids such as sulfuric acid and phosphoric acid, and strong organic acids such as sulfonic acid, phosphonic acid and trifluoroacetic acid; Solid acid catalysts such as strongly acidic cation exchange resins, zeolites, silica, alumina and activated clay; Heteropoly acids, such as in molybdate and phosphotungstic acid, etc. are mentioned.
- the 1,3,5-trioxane synthesized in the reactor 10 is supplied to the reaction distillation tower 20 together with water and formaldehyde supplied to the reactor 10.
- the 1,3,5-trioxane is 1,3,5-trioxane containing form 1,3,5-trioxane, formaldehyde and water.
- 1,3,5-trioxane-containing steam supplied from the reactor 10 is distilled and extracted to extract 1,3,5-trioxane.
- the reaction distillation tower 20 for this purpose is composed of a distillation unit 21 and an extraction unit 22 at the lower side, and between the distillation unit 21 and the extraction unit 22 is a Chimney Tray or a column having the same function. It may be composed of a side cut portion 23 in the form of an internal structure such as an adapter.
- 1,3,5-trioxane-containing steam supplied from the reactor 10 is introduced into the distillation unit 21 located at the lower end of the reaction distillation column 20.
- 1,3,5-trioxane-containing steam supplied from the reactor 10 is introduced into the lower part of the distillation unit 21, and the side cut portion 23 of the reaction distillation column 20 is provided.
- the water phase (a) returned to the distillation unit 21 from the condensate condenses the 1,3,5-trioxane-containing vapors coming up to the distillation unit 21, and some 1,3,5-trioxane-containing vapors are distilled. It flows into the extraction part 22 from the part 21 through the side cut 23.
- the formaldehyde contained in the water phase (a) returned to the distillation unit 21 may be used again in the reactor 10 for synthesizing 1,3,5-trioxane.
- the extractant is supplied through the extractant feed stream d to extract 1,3,5-trioxane from the 1,3,5-trioxane containing steam introduced from the distillation section 21.
- Some of the extractant supplied through the extractant feed stream (d) is azeotropic with water in the extraction unit 22 and flows out to the top of the reaction distillation tower 2, and then is returned to the extraction unit 22 (g ).
- the liquid phase containing 1,3,5-trioxane extracted from the extraction section 22 is discharged into the stream (c) through the side cut section 23 of the reaction distillation tower 20 and then the oil phase (b) and the water phase Phase separated into (a), the water phase (a) may be returned to the distillation unit 21 of the distillation column (20).
- the stream (c) may include trioxane, formaldehyde extractant, and water.
- an extractant is supplied from the outside through the extractant feed stream d for extracting 1,3,5-trioxane, and among extractants for extracting 1,3,5-trioxane
- Some may be organic solvents which can be azeotropic with water.
- halogenated aliphatic hydrocarbons such as methylene chloride, chloroform, carbon tetrachloride, and ethylene chloride
- halogenated aromatic hydrocarbons such as chlorobenzene and o-chlorobenzene, benzene, and toluene May be an aromatic hydrocarbon, of which benzene may be preferably used.
- the extractant supplied to the extractor 22 and introduced into the reactor 10 and then introduced into the extractor 22 through the distillation unit 21 flow out to the top of the reaction distillation tower 20 through azeotropic distillation.
- the vapor containing formaldehyde may also flow out to the tower.
- Other substances included in the oil phase (g) and the water phase (e, f) from which the streams flowing into the column top are separated may include methanol, formic acid, methylal, methylformate, and the like.
- 1,3,5-trioxane was prepared using the reaction distillation column 20 of the arrangement as shown in FIG.
- the reaction distillation tower 20 is a distillation unit 21 (top diameter 30mm, 15 stages, Bubble-cap tray), extraction unit 22 (top diameter 50mm, 20 stages, Bubble-cap tray), distillation unit 21 and extraction A column adapter 23 (stage 1, chimney-tray), a reactor 10 (5L, with heating unit), and a decanter (1.5L) between the sections 22, wherein the distillation unit 21 and the extraction unit ( 22 is formed in one piece.
- An aqueous solution having a formaldehyde concentration of 65.0 wt% was supplied to the reactor 10 at 400 g / hr, and the sulfuric acid concentration in the reaction solution was adjusted to 2.0 wt%.
- the 1,3,5-trioxane-containing vapor generated by heating at 1400 g / hr of steam was supplied to the distillation unit 21 of the reaction distillation column 20.
- the 1,3,5-trioxane-containing vapor supplied to the distillation section 21 is introduced into the extraction section 22 and through the sidecut 23 stream c together with the benzene supplied from the extraction section 22.
- the phase separated oil phase (b) after discharged was adjusted to 620g / hr to balance the benzene supplied to the extraction unit 22.
- the water phase a separated from the side cut 23 of the distillation column was recycled to the distillation unit 21 for maintaining the interface.
- stream (e) was maintained at 162 g / hr
- stream (f) was 300 g / hr
- the composition formed in the water phase in the column top of the distillation column 20 after 20 hours from the start of operation was 84.0 wt% of water and 11.6 wt of formaldehyde. %, Other 4.4 wt%.
- the distillation unit 21 and the extraction unit 22 of the distillation column 20 are separated, and the distillation column 24 (top diameter 30 mm, 15 stages, bubble-cap tray) and the extraction column of the arrangement as shown in FIG. (25) (Total diameter 50mm, 20-stage, bubble-cap tray), reactor 10 (5L, with heating unit), using a decanter (1.5L), to condense a part of the effluent vapor at the top of the distillation column (24)
- the condenser 40 was further configured to produce trioxane.
- An aqueous solution having a formaldehyde concentration of 65.0 wt% was supplied to the reactor 10 at 400 g / hr, and the sulfuric acid concentration in the reaction solution was adjusted to 2.0 wt%.
- the 1,3,5-trioxane containing steam produced by heating to 1400 g / hr of steam was fed to the distillation column 24.
- Part of the column top vapor (a ') is returned to the column top column of the distillation column 24 and the extraction tower 25 is supplied as an extractant when the 1,3,5-trioxane-containing steam is supplied to the extraction column 25.
- Benzene was fed (d).
- phase separation and phase separation (b) was adjusted to 600g / hr to balance the benzene supplied to the extraction column (25).
- the water phase a separated from the bottom of the extraction column 25 was recycled to the distillation column 24 for maintaining the interface.
- the top stream e of the extraction tower 25 was maintained at 175 g / hr, and the stream f was 156 g / hr.
- the concentration of formaldehyde formed in the water phase (e) in the column top of the extraction tower 25 after the passage of time was 19.5 wt%.
- Trioxane was prepared under the same conditions as in Example 1, but as shown in FIG. 3, 1,3,5-trioxane was prepared by returning the phase-separated water phase (f) from the top of the distillation column 20 to the bottom of the extractant feed stream. It was.
- stream (e) was maintained at 195 g / hr, and stream (f) was at 268 g / hr.
- Gas chromatography (detector TCD, separation pipe APS-201 20% Flusin T 30-60mesh 4m) is used, and the analysis conditions of gas chromatography for the measurement of the inlet temperature 170 °C, detector temperature 150 °C, separator tube temperature 110 °C 1 ⁇ l of the sample was taken with a 10 ⁇ l syringe under a helium gas rate of 20 ml / min, and analyzed.
- Example 2 when the phase separated from the top of the reaction distillation column is returned to the top of the extractant feed stream when the phase separated water phase is returned to the extraction unit (Example 1) is also compared to when it is returned to the bottom of the extractant feed stream (Comparative Example 2) In addition, the amount of formaldehyde emitted to the outside of the system was low.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Heterocyclic Compounds That Contain Two Or More Ring Oxygen Atoms (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
단위 | 실시예 1 | 비교예 1 | 비교예 2 | |
계내로 공급된 포름알데히드(α) | g/hr | 260.0 | 260.0 | 260.0 |
계외로 배출된 포름알데히드(β) | g/hr | 18.8 | 30.4 | 51.8 |
반응에 관여하지 않고 계외로 배출된 포름알데히드 ratio(β/α) | % | 7.2 | 11.7 | 19.9 |
추출부(22) 탑정 또는 추출탑(25) 탑정으로 유출된 수상(e,f) 중 포름알데히드 농도 | wt% | 11.6 | 19.5 | 32.0 |
증류탑 구성 | 1기 단독구성 | 2기 별도구성- 증류탑 1기- 추출탑 1기 | 1기 단독구성 | |
추출제와 공비된 물 중 계외로 배출되지 않고 재순환된 수상 스트림(f) 공급 위치 | 추출제 공급 스트림(d) 상부(탑정) | 추출제 공급 스트림(d) 상부(탑정) | 추출제 공급 스트림(d) 하부 |
Claims (2)
- 반응기(10); 및 일체형으로 형성된 증류부(21)와 추출부(22)를 포함하는 반응증류탑(20);을 이용한 1,3,5-트리옥산의 제조방법으로서,상기 추출부(22)에서 1,3,5-트리옥산 추출시 반응증류탑(20)의 탑정으로 유출된 스트림에서 상분리된 수상 중 일부가 상기 추출부(22)의 추출제 공급 스트림 상단으로 재순환되는 것을 특징으로 하는 1,3,5-트리옥산의 제조방법.
- 제1항에 있어서,반응증류탑(20)의 탑정으로 유출되어 상분리된 수상 중에 포름알데히드 농도가 15 wt% 이하인 것을 특징으로 하는 1,3,5-트리옥산의 제조방법.
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/882,034 US8981125B2 (en) | 2010-10-29 | 2011-08-18 | Method for preparing 1,3,5-trioxane |
CN201180063318.9A CN103370313B (zh) | 2010-10-29 | 2011-08-18 | 1,3,5-三氧杂环己烷的制备方法 |
JP2013536489A JP5873096B2 (ja) | 2010-10-29 | 2011-08-18 | 1,3,5−トリオキサンの製造方法 |
BR112013010541A BR112013010541A8 (pt) | 2010-10-29 | 2011-08-18 | Método de preparação de 1,3,5-trioxano |
EP11836529.5A EP2634182B8 (en) | 2010-10-29 | 2011-08-18 | Method for preparing 1,3,5-trioxane |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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KR1020100107119A KR101092220B1 (ko) | 2010-10-29 | 2010-10-29 | 1.3,5―트리옥산의 제조방법 |
KR10-2010-0107119 | 2010-10-29 |
Publications (2)
Publication Number | Publication Date |
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WO2012057437A2 true WO2012057437A2 (ko) | 2012-05-03 |
WO2012057437A3 WO2012057437A3 (ko) | 2012-06-21 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/KR2011/006061 WO2012057437A2 (ko) | 2010-10-29 | 2011-08-18 | 1,3,5-트리옥산의 제조방법 |
Country Status (7)
Country | Link |
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US (1) | US8981125B2 (ko) |
EP (1) | EP2634182B8 (ko) |
JP (1) | JP5873096B2 (ko) |
KR (1) | KR101092220B1 (ko) |
CN (1) | CN103370313B (ko) |
BR (1) | BR112013010541A8 (ko) |
WO (1) | WO2012057437A2 (ko) |
Families Citing this family (3)
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KR101496621B1 (ko) | 2014-09-16 | 2015-02-25 | 백승용 | 트리옥산의 제조 방법 |
MY187412A (en) * | 2015-12-18 | 2021-09-22 | Basf Se | Energy recovery in a method for preparing 1,3,5-trioxane |
CN105622366B (zh) * | 2016-03-14 | 2017-09-12 | 凯瑞环保科技股份有限公司 | 一种生产聚甲氧基二甲醚dmm3‑5的装置及方法 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS57200383A (en) | 1981-06-02 | 1982-12-08 | Mitsubishi Gas Chem Co Inc | Preparation of trioxan |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1493997C3 (de) * | 1964-11-28 | 1973-11-08 | Fa. Josef Meissner, 5000 Koeln | Verfahren zur Herstellung von Trioxan |
DE2912767A1 (de) * | 1979-03-30 | 1980-10-09 | Hoechst Ag | Verfahren zur kontinuierlichen herstellung von trioxan |
JPH06228127A (ja) * | 1993-02-02 | 1994-08-16 | Asahi Chem Ind Co Ltd | トリオキサンの製造方法 |
DE19842579A1 (de) * | 1998-09-17 | 2000-03-23 | Ticona Gmbh | Abtrennung von Trioxan aus flüssigen Gemischen |
JP2001199978A (ja) | 1999-11-10 | 2001-07-24 | Toray Ind Inc | トリオキサンの製造方法 |
KR20010097592A (ko) * | 2000-04-25 | 2001-11-08 | 구광시 | 트리옥산의 제조방법 |
JP2005247719A (ja) | 2004-03-02 | 2005-09-15 | Toray Ind Inc | 1,3,5トリオキサンの連続製造方法 |
-
2010
- 2010-10-29 KR KR1020100107119A patent/KR101092220B1/ko active IP Right Grant
-
2011
- 2011-08-18 BR BR112013010541A patent/BR112013010541A8/pt not_active Application Discontinuation
- 2011-08-18 EP EP11836529.5A patent/EP2634182B8/en active Active
- 2011-08-18 JP JP2013536489A patent/JP5873096B2/ja active Active
- 2011-08-18 WO PCT/KR2011/006061 patent/WO2012057437A2/ko active Application Filing
- 2011-08-18 CN CN201180063318.9A patent/CN103370313B/zh active Active
- 2011-08-18 US US13/882,034 patent/US8981125B2/en active Active
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS57200383A (en) | 1981-06-02 | 1982-12-08 | Mitsubishi Gas Chem Co Inc | Preparation of trioxan |
Also Published As
Publication number | Publication date |
---|---|
JP2013542221A (ja) | 2013-11-21 |
US20130261318A1 (en) | 2013-10-03 |
EP2634182A4 (en) | 2014-04-02 |
EP2634182A2 (en) | 2013-09-04 |
KR101092220B1 (ko) | 2011-12-12 |
CN103370313A (zh) | 2013-10-23 |
BR112013010541A2 (pt) | 2016-07-05 |
EP2634182B1 (en) | 2015-08-05 |
CN103370313B (zh) | 2015-04-01 |
BR112013010541A8 (pt) | 2017-10-31 |
EP2634182B8 (en) | 2015-09-16 |
WO2012057437A3 (ko) | 2012-06-21 |
JP5873096B2 (ja) | 2016-03-01 |
US8981125B2 (en) | 2015-03-17 |
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