EP3426645A1 - Herstellungsausrüstung zur herstellung von caprolacton - Google Patents

Herstellungsausrüstung zur herstellung von caprolacton

Info

Publication number
EP3426645A1
EP3426645A1 EP17763648.7A EP17763648A EP3426645A1 EP 3426645 A1 EP3426645 A1 EP 3426645A1 EP 17763648 A EP17763648 A EP 17763648A EP 3426645 A1 EP3426645 A1 EP 3426645A1
Authority
EP
European Patent Office
Prior art keywords
production equipment
equipment according
hydrogen peroxide
anyone
section
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.)
Pending
Application number
EP17763648.7A
Other languages
English (en)
French (fr)
Other versions
EP3426645A4 (de
Inventor
William John MAYO
Neil David EDWARDSON
Antony ORRELL
Jeremy Charles HAZLEHURST
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ingevity UK Ltd
Original Assignee
Perstorp AB
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Perstorp AB filed Critical Perstorp AB
Publication of EP3426645A1 publication Critical patent/EP3426645A1/de
Publication of EP3426645A4 publication Critical patent/EP3426645A4/de
Pending legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/242—Tubular reactors in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/243—Tubular reactors spirally, concentrically or zigzag wound
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00027—Process aspects
    • B01J2219/0004—Processes in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00101—Reflux columns
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2219/0011—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant liquids

Definitions

  • the present invention refers to a production equipment for production of a caprolactone, such as ⁇ -caprolactone, by reaction between peracetic acid and cyclohexanone in a so called Baeyer-Villiger reaction.
  • the first step in a caprolactone synthesis is typically the generation of peracetic acid, from acetic acid and hydrogen peroxide, used to oxidise cyclohexanone according to reaction scheme (I) below
  • the present invention is directed to a production equipment for production of a caprolactone by above disclosed reactions, said equipment is in embodiments split into a first section wherein peracetic acid is produced, a second section wherein caprolacton is produced, and a third section wherein yielded product is purified.
  • Said first section comprises, in embodiments of the present invention, a hydrogen peroxide inlet (1), a concentration unit (2) wherein hydrogen peroxide is concentrated into high strength hydrogen peroxide, a high strength hydrogen peroxide tank (3), a measure unit (4) wherein said high strength hydrogen peroxide and acetic acid are measured before being mixed and cooled in a premix unit (5), and peracetic acid stills (6) wherein said high strength hydrogen peroxide and said acetic acid is reacted in presence of a catalyst, such as sulphuric acid, and fractionated by distilling off yielded peracetic acid, unreacted acetic acid and water and holding back unreacted peroxide and catalyst.
  • a catalyst such as sulphuric acid
  • Said concentration unit (2) comprises, in especially preferred embodiments of said first section (Fig. 1), a serious of 3 peroxide concentrators (2a, 2b and 2c) being for instance film evaporators having large surface areas.
  • said premix unit (5) comprises a series of 3 agitated vessels (5a, 5b and 5c).
  • hydrogen peroxide is in said concentration unit (2), at a pressure of for instance 20-45 mBar and at a temperature of 50-60°C, such as 55 +/-2°C, concentrated into high strength peroxide comprising at least 80%, such as at least 85%, hydrogen peroxide.
  • the peracetic acid stills (6) are in said preferred embodiments suitably operated at 70-150, such as 1 10-130, mBar and yielded peracetic acid has typically a peracetic acid concentration of 30-55%.
  • Said second section (Fig. 2) comprises a peracetic inlet (7), a cyclohexanone inlet (8), at least two continuously stirred reactors (9 and 10) followed by a set of tubular reactors (11), in especially preferred embodiments at least 4, such as 6, tubular reactors (11a, l ib, 1 1c, l id, l ie and 11 f) in series wherein said peracetic acid and said cyclohexanone are reacted, a product cooler (12) wherein yielded reaction mixture is cooled, and an outlet (13) for further feeding of yielded reaction mixture to said third section.
  • tubular reactors 11a, l ib, 1 1c, l id, l ie and 11 f
  • Said third sector comprises, in preferred embodiments of the present invention, an inlet (14) for feeding of yielded reaction mixture, a pre-heater (15) heating the reaction mixture to a predetermined temperature, such as 50 +/- 5°C, a stripper (16) wherein water is removed, a fractionator (17) wherein light ends and unreacted raw materials are removed through an outlet (18).
  • the fractionated product is fed to a tank (19) and subsequently to a thin film evaporator (20) via a pre-heater (21) and finally to a distillation column (22), operating at for instance 0.5-20, such as 5-10, mbar, comprising separation steps yielding purified caprolactone.
  • the production equipment according to the present invention may optionally and additionally comprise a forth section (Fig. 4) comprising a tank (23) comprising unreacted raw materials and light ends which products are separated in at least a primary (24), a secondary (25) and a tertiary (26) distillation column, whereby cyclohexanone and acetic acid are recovered and optionally recycled.
  • Said primary distillation column (24) is, in preferred embodiments, operated at for instance atmospheric pressure, whereby an azeotrope of water and cyclohexanone is distilled off and separated in a decanter (27).
  • Acetic acid is, in said secondary distillation column (25), which suitably operates at for instance a temperature of 1 10-120°C, distilled off and sent to a storage tank.
  • Cyclohexanone is, under for instance vacuum condition, purified in said tertiary distillation column (26) and remains are sent for disposal. While particular embodiments of the invention have been shown, it will be understood, of course, that the invention is not limited thereto since many modifications may be made, and it is, therefore, contemplated to cover by the appended claims any such modifications as fall within the true spirit and scope of the invention.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP17763648.7A 2016-03-09 2017-03-03 Herstellungsausrüstung zur herstellung von caprolacton Pending EP3426645A4 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB1604114.7A GB2548138A (en) 2016-03-09 2016-03-09 Production equipment (II) for production of a caprolactone
PCT/SE2017/000018 WO2017155441A1 (en) 2016-03-09 2017-03-03 Production equipment for production of caprolactone

Publications (2)

Publication Number Publication Date
EP3426645A1 true EP3426645A1 (de) 2019-01-16
EP3426645A4 EP3426645A4 (de) 2019-08-14

Family

ID=55859280

Family Applications (1)

Application Number Title Priority Date Filing Date
EP17763648.7A Pending EP3426645A4 (de) 2016-03-09 2017-03-03 Herstellungsausrüstung zur herstellung von caprolacton

Country Status (3)

Country Link
EP (1) EP3426645A4 (de)
GB (1) GB2548138A (de)
WO (1) WO2017155441A1 (de)

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11208394B2 (en) 2018-09-17 2021-12-28 Regents Of The University Of Minnesota Chemical process to manufacture branched-caprolactone
CN109748900A (zh) * 2019-01-29 2019-05-14 安徽华业香料合肥有限公司 一种ε-癸内酯合成香料的生产方法
CN109705083A (zh) * 2019-01-29 2019-05-03 安徽华业香料合肥有限公司 一种ε-癸内酯香料的合成方法
DE102019103123A1 (de) 2019-02-08 2020-08-13 Tesa Se Thermisch erweichbares Klebeband und Verfahren zum Ummanteln von langgestrecktem Gut insbesondere Leitungen
DE102019103120A1 (de) 2019-02-08 2020-08-13 Tesa Se UV-härtbares Klebeband und Verfahren zum Ummanteln von langgestrecktem Gut insbesondere Leitungen
DE102019103122A1 (de) 2019-02-08 2020-08-13 Tesa Se Mit Feuchtigkeit härtbares Klebeband und Verfahren zum Ummanteln von langgestrecktem Gut insbesondere Leitungen

Family Cites Families (20)

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Publication number Priority date Publication date Assignee Title
GB1203752A (en) * 1966-09-30 1970-09-03 Laporte Chemical Preparation of lactones
DE2038455A1 (de) * 1970-08-01 1972-02-10 Bayer Ag Verfahren zur Herstellung von epsilon-Caprolacton
DE2519300C3 (de) * 1975-04-30 1979-06-13 Bayer Ag, 5090 Leverkusen Verfahren zur Herstellung von Perpropionsäurelösungen unter explosionssicheren Bedingungen
DE2920436A1 (de) * 1979-05-19 1980-12-04 Bayer Ag Verfahren zur herstellung von epsilon -caprolacton
DE2934659A1 (de) * 1979-08-28 1981-03-19 Bayer Ag, 5090 Leverkusen Verfahren zur herstellung von sehr reinem epsilon -caprolacton
JPS5742684A (en) * 1980-08-28 1982-03-10 Daicel Chem Ind Ltd Preparation of epsilon-caprolactone
FR2500453A1 (fr) * 1981-02-20 1982-08-27 Ugine Kuhlmann Procede d'obtention de l'epsilon-caprolactone
FR2519985A1 (fr) * 1982-01-15 1983-07-22 Ugine Kuhlmann Procede perfectionne de fabrication de l'e-caprolactone
JPH0798816B2 (ja) * 1990-04-25 1995-10-25 宇部興産株式会社 ε―カプロラクトンの製造法
EP1004576A1 (de) * 1998-11-23 2000-05-31 SOLVAY (Société Anonyme) Verfahren zur Herstellung von Peressigsäure
US7012154B2 (en) * 2004-07-28 2006-03-14 Peragen Systems, Llc Continuous process for on-site and on-demand production of aqueous peracteic acid
US8075857B2 (en) * 2006-10-18 2011-12-13 Ecolab Usa Inc. Apparatus and method for making a peroxycarboxylic acid
CN102584775B (zh) * 2011-01-12 2015-04-22 中国石油化工集团公司 制备ε-己内酯的方法
CN102584776A (zh) * 2011-01-12 2012-07-18 中国石油化工集团公司 一种制备ε-己内酯的方法
CN103570667B (zh) * 2012-08-09 2015-01-21 中国石油化工股份有限公司 一种连续制备ε一己内酯的方法
CN103539770B (zh) * 2013-10-08 2016-06-08 常州大学 一种制备ε-己内酯的连续反应工艺方法及微通道反应装备
CN104003972A (zh) * 2014-04-28 2014-08-27 安徽红太阳新材料有限公司 一种制备己内酯的方法
CN104119309B (zh) * 2014-07-24 2016-03-09 江苏红太阳新材料有限公司 一种环境友好型催化剂用于合成ε-己内酯的方法
CN105646433A (zh) * 2014-11-11 2016-06-08 中国石油化工股份有限公司 一种连续制备高纯ε－己内酯的工艺
CN104370873A (zh) * 2014-11-21 2015-02-25 南京工业大学 一种由环己酮催化氧化制备己内酯的方法

Also Published As

Publication number Publication date
EP3426645A4 (de) 2019-08-14
WO2017155441A1 (en) 2017-09-14
GB201604114D0 (en) 2016-04-20
GB2548138A (en) 2017-09-13

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