WO1997024346A1 - Verfahren zur herstellung von gamma-butyrolacton sowie dessen verwendung - Google Patents
Verfahren zur herstellung von gamma-butyrolacton sowie dessen verwendung Download PDFInfo
- Publication number
- WO1997024346A1 WO1997024346A1 PCT/EP1996/005486 EP9605486W WO9724346A1 WO 1997024346 A1 WO1997024346 A1 WO 1997024346A1 EP 9605486 W EP9605486 W EP 9605486W WO 9724346 A1 WO9724346 A1 WO 9724346A1
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- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- weight
- reaction
- gamma
- butyrolactone
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D207/00—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom
- C07D207/02—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom with only hydrogen or carbon atoms directly attached to the ring nitrogen atom
- C07D207/18—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom with only hydrogen or carbon atoms directly attached to the ring nitrogen atom having one double bond between ring members or between a ring member and a non-ring member
- C07D207/22—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom with only hydrogen or carbon atoms directly attached to the ring nitrogen atom having one double bond between ring members or between a ring member and a non-ring member with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D207/24—Oxygen or sulfur atoms
- C07D207/26—2-Pyrrolidones
- C07D207/263—2-Pyrrolidones with only hydrogen atoms or radicals containing only hydrogen and carbon atoms directly attached to other ring carbon atoms
- C07D207/267—2-Pyrrolidones with only hydrogen atoms or radicals containing only hydrogen and carbon atoms directly attached to other ring carbon atoms with only hydrogen atoms or radicals containing only hydrogen and carbon atoms directly attached to the ring nitrogen atom
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D315/00—Heterocyclic compounds containing rings having one oxygen atom as the only ring hetero atom according to more than one of groups C07D303/00 - C07D313/00
Definitions
- the invention relates to a process for the production of gamma-butyrolactone by catalytic hydrogenation of maleic anhydride, succinic anhydride or their acids in the vapor phase and the use thereof for the production of pyrrolidones and N-alkylpyrrolidones.
- Garnma-butyrolactone is an important chemical that is important as a starting material for numerous syntheses. For example, it plays a role in the production of butteric acid and its derivatives, 1,4-butanediol, tetrahydrofuran, N-methylpyrrolidone, polyvinylpyrrolidone, methionine and the like.
- Gamma-butyrolactone is also an important solvent for, among other things, acrylates and styrene-based polymers. It can also be used as a solvent, inter alia, in the production of synthetic fibers.
- a number of production methods are based on maleic anhydride or derivatives such as maleic acid, succinic anhydride, maleic acid esters, which are subjected to hydrogenation.
- the hydrogenation is usually carried out in the vapor phase and in the presence of catalysts.
- catalysts There will be Numerous catalysts for these reactions have been described.
- US Pat. No. 3,065,243 shows a process in which copper chromite serves as a catalyst.
- this reaction still produces considerable amounts of succinic anhydride, which must be circulated.
- DE-OS 24 04 493 describes a process in which hydrogenation is carried out in the presence of water vapor. This is to reduce coking of the catalyst.
- One disadvantage of this process is that additional water is introduced, which is already formed as a by-product anyway, which makes this process more complex.
- EP-A1-0 638 565 describes a process in which gamma-butyrolactone is produced in a reduced form by catalytic hydrogenation of maleic anhydride in the vapor phase in the presence of catalysts based on copper chromite.
- catalysts based on copper chromite Although with the uniform, i.e. homogeneous catalyst based on the three components copper oxide, chromium oxide and silicon dioxide high selectivities and good yields have been achieved, it has been shown that the durability of the catalyst still leaves something to be desired.
- US Pat. No. 5,347,021 describes a process for the production of gamma-butyrolactone, in which hydrogen and maleic anhydride are likewise reacted in the presence of a catalyst in the vapor phase.
- the catalyst is based on the components copper oxide, zinc oxide, aluminum oxide and graphite. Although the process works with relatively good selectivities and yields, in the process described there the catalyst has to be reactivated after a running time of about 100 hours.
- This object is achieved by a process for the production of gamma-butyrolactone by catalytic hydrogenation of maleic anhydride, succinic anhydride or their acids in the vapor phase in the presence of catalysts based on copper oxide and aluminum oxide in reduced form, characterized in that: to carry out the reaction, a catalyst is used which is based on 50 to 95% by weight copper oxide, 3 to 30% by weight aluminum oxide and 0 to 25% by weight of a binder.
- the catalyst used is preferably based on 80 to 90% copper oxide, 5 to 15% aluminum oxide and in the 100% missing remainder from a binder.
- Graphite and silica gel are particularly suitable as binders.
- a particularly advantageous catalyst for the process is based on 83.5-85.5% by weight of copper oxide, 9-11% by weight of aluminum oxide and 4.5-6.5% by weight of graphite. It is advantageous if the catalyst has a uniform structure, i.e. is homogeneous.
- the catalyst can also be applied to a support.
- the hydrogenation can also be carried out in the presence of an inert gas as a diluent, preferably nitrogen.
- an inert gas preferably nitrogen.
- the well-known noble gases such as argon, Krypton, helium or mixtures thereof with one another or with nitrogen can be used.
- the catalyst based on the 3 components is reduced in a conventional manner in a conventional manner before use in the reaction.
- the reduction is preferably carried out in the reactor itself.
- the reduction can be carried out, for example, according to the following procedure.
- the catalyst which is present as a catalyst bed, is heated to 150 ° C. in a nitrogen stream in the reactor. At this temperature, hydrogen is slowly fed in up to an input concentration of up to 8% by volume. The temperature in the catalyst bed should not rise more than 25 ° C.
- the hydrogen concentration is increased to 80-100% by reducing the nitrogen flow and the temperature is raised up to 280.degree.
- the temperature is maintained for 12 hours under a H j flow; this
- Process is generally called post-reaction.
- Uniform catalyst in the context of the invention means that the components are so intimately connected to one another that the catalyst has a uniform structure, i.e. is essentially homogeneous and has no major heterogeneous components of different structures.
- the catalyst can then immediately be introduced into the reactor and, after a corresponding reduction, used for the reaction.
- the hydrogenation of maleic anhydride ie the reaction of maleic anhydride with hydrogen, is carried out in the vapor phase, ie at elevated temperatures, for example in a range from about 100 to 400 ° C., the range from about 260 to 320 ° C. is preferred.
- the gaseous maleic anhydride can be fed into the reaction space by heating and transferring to the vapor phase and metering accordingly.
- this can also be done by the inert gas, such as nitrogen, which may also be used.
- the molar ratio of maleic anhydride to hydrogen can vary within wide limits in the stream of the starting products and can be, for example, between 1:20 and 1: 250. The range 1:40 to 1: 100 is preferred.
- the reaction can be carried out both under normal pressure and under reduced pressure or elevated pressure, for example between 0.1 and 10 bar.
- inert gas means that it does not participate in the reaction as a reaction partner or reaction product and does not change itself as a result of a reaction.
- an inert gas as a diluent, it is possible to influence the reaction favorably.
- the dilution depending on the other reaction conditions chosen, finds its limit where the proportion of the diluent is so large that there is too little hydrogen and the yield, based on maleic anhydride, drops sharply. This limit can be determined by a few simple tests which belong to the manual skills of an average specialist.
- the dwell time can thus be changed, which can be made possible by setting different metering speeds, but which can also be accomplished by extending the reaction zone, for example by using a longer reaction tube which is correspondingly filled with catalyst.
- the catalyst can be wholly or partially diluted with a material which is inert in the reaction medium and has a sufficiently high thermal conductivity, for which purpose e.g. Steel balls, steatite, etc. are suitable.
- the reaction can be controlled in such a way that the succinic anhydride formed as an intermediate is no longer present at the end of the reactor and therefore no longer has to be circulated.
- the reaction can also be controlled in such a way that succinic anhydride is still present in the emerging reaction products in more or less large quantities and is then either processed further for itself after separation or is also circulated again.
- the gamma-butyrolactone and the water formed are separated in a manner known per se. It was completely surprising that the use of the catalyst according to the invention brings about both a high selectivity and a high yield.
- the advantages of the catalyst used according to the invention are not only evident when working with or without a diluent, they are also evident when the molar ratios of the reactants are changed and when the temperatures are varied. This catalyst can thus be used with great advantages in the production of gamma-butyrolactone by reduction of maleic anhydride by means of hydrogen under the most varied of process conditions.
- the gamma-butyrolactone formed in the process according to the invention directly without separating off the water formed for the preparation of pyrrolidone and N-alkylpyrrolidones in the liquid phase under high pressure, in particular for the preparation of N-methylpyrrolidone by adding Methylamine can be used.
- Example 1 (Atmospheric Pressure Without Hydrogen Recycling)
- the catalyst was reduced in the following way:
- the catalyst is heated to 150 ° C. in a stream of nitrogen. At this temperature, hydrogen is slowly fed in up to an input concentration of up to 8 percent by volume. The temperature rise of the bed is kept below 25 ° C. After the heat of reaction has subsided, the hydrogen content is increased from 80% to 100% and the temperature is raised to 280 ° C. The temperature is maintained under the flow of hydrogen for 2 hours (after-reaction).
- Maleic anhydride and hydrogen are then added in gaseous form in the desired amount, i.e. 1 mole per hour of hydrogen and 0.01 mole per hour of maleic anhydride.
- the temperature of the heating is set to 265 ° C. A hot spot of 7 ° C is observed. The yield was 98% with 100% conversion.
- 660 g of catalyst in a stainless steel tube reactor with an inner diameter of 30 mm and a length of 1.2 m, 660 g of catalyst, as described in Example 1, are used without comminution.
- the aforementioned 660 g of catalyst are mixed with 160 g of 160 g of an inert material consisting of steel balls in order to reduce the temperature in the area of the hot spot. This mixture forms the upper part of the catalyst bed.
- the heat is dissipated via a heat transfer oil which flows through the double jacket of the reactor tube.
- the hydrogen used for the hydrogenation is recycled after the products have been condensed (condensation at 25 ° C.).
- the condensed products are fed directly to an analysis. Approximately 10% of the amount of hydrogen required for the actual implementation is removed in order to reduce the accumulation of by-products in the cycle gas.
- the pressure is 6 bar absolute.
- a hydrogen flow through the reactor of 1000 nl / h is set after the reduction, where nl means standard liters.
- 60 g / hour of maleic anhydride are metered in.
- the freshly added amount of hydrogen is 60 nl / h.
- the amount of gas discharged is controlled by a pressure regulator.
- the maleic anhydride is metered in liquid in an evaporator upstream of the actual reactor.
- the amount of gas discharged is controlled by a pressure regulator.
- the pressure is 6 bar.
- the catalyst bed which is already in the intended reactor, is heated to 150 ° C. in a stream of nitrogen. At this temperature, hydrogen is slowly fed in up to an input concentration of up to 8% by volume.
- the rise in temperature of the bed should not be greater than 25 ° C. (reduction step).
- the catalyst pellets are crushed and a fraction from 0.8 to 1.2 mm is selected. These are placed in a quartz glass tube with 1 cm inner diameter and 30 cm length that can be heated with silicone oil. After carrying out the reduction step described above, the test is carried out. Hydrogen is metered in via a mass flow controller and the maleic anhydride partial pressure is set using a so-called saturator. This is done by passing hydrogen and possibly nitrogen through the saturator in which liquid maleic anhydride is located, a known maleic anhydride partial pressure being established on the basis of the precisely fixed temperature. The mixture is fed to the reactor via heated lines.
- the catalysts were reduced as described above. In each case 20 ml bulk volume of the reduced catalyst were introduced into the reactor and brought to a reaction temperature of 275 ° C. at a flow rate of 0.38 mol N 2 / h and 2 mol H 2 / h. The gas mixture was then passed through the saturator and a mole stream of maleic anhydride of 0.02 mol / h was thus set. After a reaction time of 2 h, the product mixture was analyzed. The results are shown in Table 3 below.
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1019980704886A KR19990076763A (ko) | 1995-12-27 | 1996-12-07 | 감마-부티로락톤의 제조 방법 및 이의 용도 |
AT96943900T ATE242228T1 (de) | 1995-12-27 | 1996-12-07 | Verfahren zur herstellung von gamma-butyrolacton sowie dessen verwendung |
EP96943900A EP0882032B1 (de) | 1995-12-27 | 1996-12-07 | Verfahren zur herstellung von gamma-butyrolacton sowie dessen verwendung |
DE59610515T DE59610515D1 (de) | 1995-12-27 | 1996-12-07 | Verfahren zur herstellung von gamma-butyrolacton sowie dessen verwendung |
US09/051,542 US6075153A (en) | 1995-12-27 | 1996-12-07 | Process for the preparation of Gamma-Butyrolactone and the use thereof |
JP9523991A JP2000502685A (ja) | 1995-12-27 | 1996-12-07 | γ―ブチロラクトンの製造方法及びその使用 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19548818 | 1995-12-27 | ||
DE19548818.0 | 1995-12-27 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1997024346A1 true WO1997024346A1 (de) | 1997-07-10 |
Family
ID=7781479
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1996/005486 WO1997024346A1 (de) | 1995-12-27 | 1996-12-07 | Verfahren zur herstellung von gamma-butyrolacton sowie dessen verwendung |
Country Status (10)
Country | Link |
---|---|
US (2) | US6075153A (de) |
EP (1) | EP0882032B1 (de) |
JP (1) | JP2000502685A (de) |
KR (1) | KR19990076763A (de) |
AT (1) | ATE242228T1 (de) |
CA (1) | CA2240133A1 (de) |
DE (1) | DE59610515D1 (de) |
TW (1) | TW341568B (de) |
WO (1) | WO1997024346A1 (de) |
ZA (1) | ZA9610436B (de) |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6008375A (en) * | 1995-12-27 | 1999-12-28 | Akzo Nobel Nv | Process for manufacturing 2-pyrrolidone or N-alkylpyrrolidones |
WO2002047815A1 (de) * | 2000-12-11 | 2002-06-20 | Basf Aktiengesellschaft | SCHALENKATALYSATOR FÜR DIE HYDRIERUNG VON MALEINSÄUREANHYDRID UND VERWANDTEN VERBINDUNGER ZU η-BUTYROLACTON UND TETRAHYDROFURAN UND DERIVATEN DAVON |
WO2002102773A1 (de) * | 2001-06-19 | 2002-12-27 | Basf Aktiengesellschaft | Verfahren zur herstellung von pyrrolidonen |
WO2003074482A1 (de) * | 2002-03-02 | 2003-09-12 | Basf Aktiengesellschaft | Verfahren zur gleichzeitigen herstellung von tetrahydrofuran und pyrrolidonen |
US6831182B2 (en) | 2000-12-11 | 2004-12-14 | Basf Aktiengesellschaft | Method for the hydrogenation of maleic anhydride and related compounds in two serial reaction zones |
US6888011B2 (en) | 2000-12-11 | 2005-05-03 | Basf Aktiengesellschaft | Porous catalyst for the hydrogenation of maleic anhydride to tetrahydrofuran |
US6958404B2 (en) | 2000-12-11 | 2005-10-25 | Basf Aktiengesellschaft | Method for the hydrogenation of maleic anhydride and related compounds in a fluid bed reactor |
US7154011B2 (en) | 2002-06-11 | 2006-12-26 | Basf Aktiengesellschaft | Method for the production of 1,4- butanediol |
US7169958B2 (en) | 2002-06-11 | 2007-01-30 | Basf Aktiengesellschaft | Method for the production of 1,4- butane-diol by combined gas-phase and liquid-phase hydrogenation |
US7271299B2 (en) | 2002-06-11 | 2007-09-18 | Basf Aktiengesellschaft | Two-stage method for producing butanediol with intermediated separation of succinic anhydride |
WO2016008904A1 (en) | 2014-07-16 | 2016-01-21 | Basf Se | METHOD FOR PURIFYING RAW γ-BUTYROLACTONE |
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BE1012013A6 (fr) * | 1998-04-09 | 2000-04-06 | Pantochim Sa | Procede de production de n-methylpyrrolidone. |
MY122525A (en) * | 1999-10-12 | 2006-04-29 | Kvaerner Process Tech Ltd | Process for the simultaneous production of maleic anyhydride and its hydrogenated derivatives |
BE1012946A6 (fr) | 1999-10-27 | 2001-06-05 | Pantochim Sa | Procede de production de n-methyl pyrrolidone en utilisant de la gamma-butyrolactone et des methylamines mixtes comme materiaux de depart. |
DE10021703A1 (de) * | 2000-05-04 | 2001-11-08 | Basf Ag | Verfahren zur destillativen Trennung von Tetrahydrofuran, gamma-Butyrolacton und/oder 1,4-Butandiol enthaltenden Gemischen |
US6603021B2 (en) * | 2001-06-18 | 2003-08-05 | Battelle Memorial Institute | Methods of making pyrrolidones |
KR100457066B1 (ko) * | 2002-04-22 | 2004-11-12 | 애경유화 주식회사 | 수소화 반응촉매 및 그의 제조방법, 및 이 촉매를이용하여 무수말레인산으로부터 감마-부티로락톤을제조하는 방법 |
DE10219224A1 (de) * | 2002-04-30 | 2003-11-13 | Basf Ag | Verfahren zur Herstellung von gamma-Butyrolacton |
US7199250B2 (en) * | 2002-12-20 | 2007-04-03 | Battelle Memorial Institute | Process for producing cyclic compounds |
GB0325384D0 (en) * | 2003-10-30 | 2003-12-03 | Davy Process Techn Ltd | Process |
CN102781926B (zh) | 2010-02-11 | 2016-11-09 | 梅塔玻利克斯公司 | γ-丁内酯的生产方法 |
US20140170714A1 (en) | 2011-08-10 | 2014-06-19 | Metabolix, Inc. | Post process purification for gamma-butyrolactone production |
CN112742432B (zh) * | 2019-10-30 | 2022-09-20 | 中国石油化工股份有限公司 | 一种顺酐加氢制γ-丁内酯的方法 |
CN112756004B (zh) * | 2019-11-04 | 2022-09-20 | 中国石油化工股份有限公司 | 用于顺酐加氢制γ-丁内酯的催化剂及其制备方法和应用 |
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Cited By (16)
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US6075153A (en) * | 1995-12-27 | 2000-06-13 | Akzo Nobel Nv | Process for the preparation of Gamma-Butyrolactone and the use thereof |
US6008375A (en) * | 1995-12-27 | 1999-12-28 | Akzo Nobel Nv | Process for manufacturing 2-pyrrolidone or N-alkylpyrrolidones |
KR100773174B1 (ko) * | 2000-12-11 | 2007-11-02 | 바스프 악티엔게젤샤프트 | 말레산 무수물 및 관련된 화합물을 수소첨가하여γ-부티로락톤, 테트라히드로푸란 및 그의 유도체를수득하기 위한 촉매적 코팅 |
WO2002047815A1 (de) * | 2000-12-11 | 2002-06-20 | Basf Aktiengesellschaft | SCHALENKATALYSATOR FÜR DIE HYDRIERUNG VON MALEINSÄUREANHYDRID UND VERWANDTEN VERBINDUNGER ZU η-BUTYROLACTON UND TETRAHYDROFURAN UND DERIVATEN DAVON |
US6831182B2 (en) | 2000-12-11 | 2004-12-14 | Basf Aktiengesellschaft | Method for the hydrogenation of maleic anhydride and related compounds in two serial reaction zones |
US6888011B2 (en) | 2000-12-11 | 2005-05-03 | Basf Aktiengesellschaft | Porous catalyst for the hydrogenation of maleic anhydride to tetrahydrofuran |
US6958404B2 (en) | 2000-12-11 | 2005-10-25 | Basf Aktiengesellschaft | Method for the hydrogenation of maleic anhydride and related compounds in a fluid bed reactor |
US7217679B2 (en) | 2000-12-11 | 2007-05-15 | Basf Aktiengesellschaft | Catalytic coating for the hydrogenation of maleic anhydride and related compounds to give γ-butyrolactone, tetrahydrofuran and derivatives thereof |
WO2002102773A1 (de) * | 2001-06-19 | 2002-12-27 | Basf Aktiengesellschaft | Verfahren zur herstellung von pyrrolidonen |
WO2003074482A1 (de) * | 2002-03-02 | 2003-09-12 | Basf Aktiengesellschaft | Verfahren zur gleichzeitigen herstellung von tetrahydrofuran und pyrrolidonen |
KR100934056B1 (ko) * | 2002-03-02 | 2009-12-24 | 바스프 에스이 | 테트라히드로푸란과 피롤리돈을 동시에 제조하는 방법 |
US7193091B2 (en) | 2002-03-02 | 2007-03-20 | Basf Aktiengesellschaft | Method for the simultaneous production of tetrahydrofurans and pyrrolidones |
US7154011B2 (en) | 2002-06-11 | 2006-12-26 | Basf Aktiengesellschaft | Method for the production of 1,4- butanediol |
US7271299B2 (en) | 2002-06-11 | 2007-09-18 | Basf Aktiengesellschaft | Two-stage method for producing butanediol with intermediated separation of succinic anhydride |
US7169958B2 (en) | 2002-06-11 | 2007-01-30 | Basf Aktiengesellschaft | Method for the production of 1,4- butane-diol by combined gas-phase and liquid-phase hydrogenation |
WO2016008904A1 (en) | 2014-07-16 | 2016-01-21 | Basf Se | METHOD FOR PURIFYING RAW γ-BUTYROLACTONE |
Also Published As
Publication number | Publication date |
---|---|
US6008375A (en) | 1999-12-28 |
CA2240133A1 (en) | 1997-07-10 |
EP0882032B1 (de) | 2003-06-04 |
KR19990076763A (ko) | 1999-10-15 |
US6075153A (en) | 2000-06-13 |
EP0882032A1 (de) | 1998-12-09 |
JP2000502685A (ja) | 2000-03-07 |
DE59610515D1 (de) | 2003-07-10 |
ATE242228T1 (de) | 2003-06-15 |
TW341568B (en) | 1998-10-01 |
ZA9610436B (en) | 1997-06-24 |
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