CN1194268A - Process of preparing gamma-butyrolactone by gas phase dehydrogenation of 1,4-butanediol - Google Patents
Process of preparing gamma-butyrolactone by gas phase dehydrogenation of 1,4-butanediol Download PDFInfo
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- CN1194268A CN1194268A CN97103634A CN97103634A CN1194268A CN 1194268 A CN1194268 A CN 1194268A CN 97103634 A CN97103634 A CN 97103634A CN 97103634 A CN97103634 A CN 97103634A CN 1194268 A CN1194268 A CN 1194268A
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- butyleneglycol
- hydrogen
- butyrolactone
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Abstract
In the presence of hydrogen gas and under the conditions of 170-250 deg.c and 0.1-0.6 MPa, 1,4-butanediol in reator is contacted with the oxide catalyst with the general expression of CuMaOx, where M is Mn or Zr and a=0.3-2.0. The said method has high 1,4-butanediol conversion rate and gamma-butyrolactone selectivity without Cr pollution, which existed in prior art.
Description
The present invention is a kind of method by dehydrogenation reaction continuous production gamma-butyrolactone, specifically, is 1, and 4-butyleneglycol vapor catalytic dehydrogenation in the presence of hydrogen prepares the method for gamma-butyrolactone.
Gamma-butyrolactone is important organic chemistry product, and the known method for preparing gamma-butyrolactone mainly is divided into two classes, and a class is that maleic anhydride or its ester gas phase hydrogenation prepare gamma-butyrolactone, as USP4, and 584,419; USP 3,853, and 922; USP 3,829, and 448; Described in the CN1034541A.Another kind of is 1, and 4-butyleneglycol vapor catalytic dehydrogenation prepares gamma-butyrolactone, narrates the correlation technique of this respect below emphatically.
This field catalyzer commonly used is the Cu-Cr series catalysts, use the Cu-Cr-Ba catalyzer as Japanese patent laid-open 3-232874, Te Kaiping 3-232875 uses the Cu-Cr-Mn-Ba catalyzer, the spy opens flat 5-25151 and then is presented in adding K or Na in the Cu-Cr catalyzer, can the draw up generation of side reaction improves activity of such catalysts and selectivity.When this patent has also been pointed out independent use Cu-Cr two constituent element catalyzer, in 230 ℃, 0.5MPa, hydrogen/pure mol ratio 4: 1,1,4-butyleneglycol weight liquid hourly space velocity 3 hours
-1Under the condition, 1, the transformation efficiency of 4-butyleneglycol can reach 91.69 heavy %, and the gamma-butyrolactone selectivity reaches 96.86 heavy %.
EP 523774 A
1A kind of method for preparing gamma-butyrolactone is also disclosed, be in Cu-Cr-Mn or Cu-Cr-Mn-Ba catalyzer, to add alkali metallic sodium or potassium, its objective is the generation that suppresses the by product tetrahydrofuran (THF), because the acid sites on the catalyzer helps the generation of tetrahydrofuran (THF), in addition, the acid mistake also easily causes catalyzer coking, inactivation by force, thereby influences life of catalyst.This patent also points out, high temperature, low pressure and low hydrogen alcohol mol ratio help generating gamma-butyrolactone, but temperature is too high, will cause that by product increases, the catalyzer coking, and therefore optimum temperature of reaction is 150～300 ℃, and pressure is 0～8 kg/cm
2, hydrogen alcohol mol ratio is 0.5～10,1, and the liquid hourly space velocity of 4-butyleneglycol is 0.2～16 hour
-1, preferably 0.4～6.0 hour
-1React 1 with this understanding, the transformation efficiency of 4-butyleneglycol can reach more than the 81.0 heavy %, and the selectivity of gamma-butyrolactone reaches more than the 97.0 heavy %.
Though the catalyzer that above prior art is used has higher activity and selectivity, all contains strong toxicity, heavy-polluted Cr component, all caused great harm for producers and environment, pollute for eliminating Cr, must drop into substantial contribution and protect and administer.Though the pollution that Cr caused still can not be solved so.
The purpose of this invention is to provide the no Cr catalyzer of a kind of usefulness with 1,4-butanediol gas phase dehydrogenation high-speed, highly selective prepare the method for gamma-butyrolactone.
Method provided by the invention is: with 1, the 4-butyleneglycol gasifies in the presence of hydrogen, by reactor, contacts dehydrogenation with the catalyzer of the following oxide compound expression formula of having of pre-reduction and makes gamma-butyrolactone under 170～250 ℃, 0.1～0.6 MPa condition.
CuM
aO
x
M is Mn or Zr in the formula, and a is the atomicity of Mn or Zr, a=0.3～2.0, and when M is Zr, a=0.5～1.5, X is for satisfying the valent oxygen atomicity of above-mentioned oxide compound.Specifically, method provided by the invention is: with hydrogen and 1, the 4-butyleneglycol is pressed 1～12: 1 the formed gas-liquid mixture of mixed in molar ratio, feed continuously after gasifier vaporizes, feeding the fixed-bed reactor that catalyzer is housed again reacts, be reflected at 170～250 ℃, 0.1～0.6 MPa pressure, 1,4-butyleneglycol weight liquid hourly space velocity (W.H.S.V) 3.0～10.0 hours
-1Condition under carry out, reaction back effluent goes out purpose product gamma-butyrolactone through condensation separation.
The gasification of alcohol described in the aforesaid method can be undertaken by the disclosed any way of prior art, and the mode of normal employing is with 1, and the 4-butyleneglycol gasifies in the hydrogen-containing gas streams of heat, this mixture is contacted with catalyzer again.
Described hydrogen generally is commercially pure hydrogen, except that hydrogen, also contains nitrogen (N
2), oxygen (O
2), a small amount of hydrocarbon gas (as methane) and carbon oxides are (as CO, CO
2).
1, the reaction of 4-butanediol dehydrogenation, the amount of hydrogen existence is few more good more theoretically, but in the actual mechanical process, the existence of excess hydrogen can make side reaction reduce, and helps improving the selectivity of gamma-butyrolactone, reaction raw materials is gasified at a lower temperature, prevent raw material when gasification temperature too high and take place rotten.But hydrogen is excessive too many, not only can reduce the duration of contact of reactant and catalyzer, and reaction conversion ratio is reduced, also can cause the increase of system energy consumption, therefore, comparatively suitable hydrogen/pure mol ratio that the present invention selects is 1～12: 1, and the exess of H2 gas in the reaction can be recycled.
1,4-butyleneglycol vapor catalytic dehydrogenation is a gas-solid phase reaction, therefore temperature of reaction must be higher than the dew point of reactant under this reaction conditions, and in addition, the temperature height also helps the carrying out that react, but temperature is too high, gamma-butyrolactone, 1, the 4-butyleneglycol will the hydrogenation dehydration generate tetrahydrofuran (THF), propyl carbinol, and tetrahydrofuran (THF) and 1 takes place, the etherification reaction of 4-butyleneglycol causes the gamma-butyrolactone selectivity to descend.Temperature of reaction too low (even being higher than the dew point of reactant), then transformation efficiency descends, and therefore, the most suitable temperature of reaction that the present invention selects is 175～250 ℃.
In this reaction system, the reduction reaction pressure helps molecular balance and moves to the gamma-butyrolactone direction.Common 1, the 4-butanediol dehydrogenation prepares being reflected under the normal pressure of gamma-butyrolactone just can carry out, but for the ease of industrialization, especially considers recycling of hydrogen, and the pressure of Xuan Zeing is 0.1～0.6 MPa in the methods of the invention.
Method provided by the invention adopted 3.0～10.0 hours that are complementary with catalyst system therefor
-1High by 1,4-butyleneglycol charging liquid phase air speed as increasing the liquid phase air speed again, for guaranteeing high transformation efficiency, certainly will will improve temperature of reaction, side reaction will increase, the selectivity of gamma-butyrolactone will descend.
The catalyzer that the inventive method adopted has following oxide compound general formula and forms: CuM
aO
x, M is Mn or Zr in the formula, a is the atomicity of Mn or Zr, and a=0.3～2.0, when M is Zr, a=0.5～1.5, X is for satisfying the valent oxygen atomicity of above-mentioned oxide compound.
This catalyzer adopts following coprecipitation method preparation, soluble salt with Cu, Mn or Zr, preferably nitrate is dissolved in the decationized Y sieve water, under stirring at room, with alkali, preferably ammonia precipitation process to pH value is 4～9, aging 1～5 hour, filter then, washing, collecting precipitation, 100～250 ℃ of dryings 4～20 hours, 400～550 ℃ of roastings 2～24 hours.
Catalyst system therefor need pass through prereduction before use in the inventive method, and reductive agent can adopt H
2Or CO reducing gas such as (carbon monoxide).Reduction is carried out under 0.5～6.0 MPa, 250～300 ℃, and the reducing gas flow is with respect to every milliliter of catalyzer 50～500 ml/min.
The inventive method is applicable to 1, and the 4-butanediol gas phase dehydrogenation prepares gamma-butyrolactone.
The inventive method is because employing Cu-Mn or Cu-Zr two component composite oxides are catalyzer, solved the Cr pollution problem that exists in the prior art, and catalyst component is few, cheap and easy to get, preparation is simple, under 170～250 ℃ of temperature, pressure 0.1～0.6 MPa condition, uses the inventive method 1,4-butyleneglycol transformation efficiency can reach more than the 99.0 heavy %, and the gamma-butyrolactone selectivity can reach more than the 98.0 heavy %.
Further specify the present invention below by example, but the present invention is not limited to this.
Example 1
Preparation of catalysts:
With 52.2 gram Cu (NO
3)
23H
2O (chemical pure, Beijing Chemical Plant), 70.0 grams, 50 heavy %Mn (NO
3)
2(the connection chemical plant produces in Beijing, analytical pure) aqueous solution is added in 500 milliliters of decationized Y sieve water, dropping ammonia (chemical pure under the stirring at room, the Beijing Chemical Plant), until the solution pH value is 6.5 ± 0.5, aging 2 hours, filters then, washing, collecting precipitation, 200 ℃ of dryings 6 hours, 500 ℃ of roastings 24 hours catalyst A: CuMn
0.8O
2.2Metal is wherein formed with X-ray fluorometry mensuration, and oxygen level is a calculated value, down together.
The prereduction of catalyzer:
After the catalyst A moulding, make 26～40 purpose particles, get 3.2 milliliters of this particles and pack in the stainless steel tubular type reactor of 8 millimeters of internal diameters, 400 millimeters of length, under 300 ℃ of temperature, 2.0 MPa pressure, feed H with the flow velocity of 500 ml/min
2Reduced 4 hours.Catalyzer prereduction is all according to said method carried out in the following example.
Catalytic dehydrogenating reaction:
After catalyzer prereduction finishes, 230 ℃ of regulation system pressure 0.1 MPa, temperature, with 1, the 4-butyleneglycol is that raw material reacts, hydrogen during charging/pure mol ratio is 4: 1,1,4-butyleneglycol weight liquid phase air speed is 6.0 hours
-1, reaction product is measured through FID with the gas chromatograph of packed column PEG 2000, the results are shown in Table 1.
Example 2
With 26.6 gram Cu (NO
3)
23H
2Mn (the NO of O, 65.5 grams, 50 heavy %
3)
2Solution joins in 300 milliliters of decationized Y sieve water, under stirring at room, with ammoniacal liquor drip to solution PH be 8.0 ± 0.5, make catalyst B by Preparation of catalysts method in the example 1 then: CuMn
1.7O
3.55
After catalyst B prereduction, react: 230 ℃ of temperature, pressure 0.4 MPa, hydrogen/pure mol ratio 5: 1,1,4-butyleneglycol weight liquid phase air speed 6.0 hours by following condition
-1, reaction result sees Table 1.
Example 3
Method by example 2 prepares catalyzer C, and that different is Cu (NO
3)
23H
2O, 50 heavy %Mn (NO
3)
2The solution add-on is respectively 17.4 grams, 11.1 grams, and catalyzer C consists of: CuMn
0.45O
2.68
The mode of pressing example 1 is with catalyzer C reduction, reaction.Different is reaction conditions is 230 ℃, 0.4 MPa, hydrogen/pure mol ratio 7.6: 1,1,4-butyleneglycol liquid phase air speed 3.9 hours
-1Reaction result sees Table 1.
Example 4
With 52.2 gram Cu (NO
3)
23H
2O, 57.7 gram ZrO (NO
3)
22H
2O (Beijing Chemical Plant, chemical pure) is dissolved in 500 milliliters of decationized Y sieve water, and dropping ammonia under the stirring at room is 5.0 ± 0.5 until the solution pH value, and the method by example 1 makes catalyzer D:CuZrO then
3
The mode of pressing example 1 is with catalyzer D prereduction afterreaction.Reaction conditions is 230 ℃, 0.1 MPa, 1,4-butyleneglycol liquid phase air speed 5.0 hours
-1, hydrogen/pure mol ratio 4: 1, reaction result sees Table 1.
Example 5
Mode by example 4 prepares catalyzer E, and that different is ZrO (NO
3)
22H
2The add-on of O is 46.2 grams, is 7.5 ± 0.5 with solution pH value behind the ammonia precipitation process, and catalyzer E consists of: CuZr
0.8O
2.6
After catalyzer E prereduction, undertaken 1 by following condition, the reaction of 4-butanediol dehydrogenation: 230 ℃ of temperature, pressure 0.3 MPa, hydrogen/pure mol ratio are 6: 1,1,4-butyleneglycol weight liquid hourly space velocity 5.0 hours
-1, reaction result sees Table 1.
Comparative example 1
With EP 0523774 A
1The CuO-Cr of preparation in the middle comparative example 6
2O
3Catalyzer is a Comparative Examples, and this catalyzer contains the heavy % of Cu36.2, the heavy % of Cr33.3, numbering a.This catalyzer is used for 1, and reaction result and processing condition when the 4-butanediol dehydrogenation prepares gamma-butyrolactone are listed in table 1.
Comparative example 2
Open the CuO-Cr described in the comparative example 1 among the flat 5-25151 with the spy
2O
3Catalyzer is a Comparative Examples, and numbering b contains the heavy % of Cu36.2 heavy %, Cr33.3 in this catalyzer, the processing condition of reaction and the results are shown in table 1.
As shown in Table 1, compare with two constituent element catalyzer of the prior art, the catalyzer that uses in the inventive method does not contain the Cr component of strong toxicity, even with prior art quite surpass its 1, under the situation of 4-butyleneglycol feeding liquid hourly space velocity, can obtain high by 1,4-butyleneglycol transformation efficiency and gamma-butyrolactone selectivity.
Table 1
| Example 1 | Example 2 | Example 3 | Example 4 | Example 5 | Comparative example 1 | Comparative example 2 | |
| The catalyzer numbering | ????A | ????B | ????C | ????D | ????E | ????a | ????b |
| Temperature of reaction, ℃ | ??230 | ??230 | ??230 | ??230 | ??230 | ??230 | ??230 |
| Reaction pressure, MPa | ??0.1 | ??0.4 | ??0.4 | ??0.1 | ??0.3 | ??0.1 | ??0.5 |
| H 2∶BDO *, mole | ??4∶1 | ??5∶1 | ??7.6∶1 | ??4∶1 | ??6∶1 | ??4∶1 | ??4∶1 |
| BDO liquid phase air speed, hour -1 | ??6.0 | ??6.0 | ??3.9 | ??5.0 | ??5.0 | ??5.0 | ??3.0 |
| The BDO transformation efficiency, heavy % | ＞99.5 | ＞99.5 | ＞99.5 | ＞99.3 | ??98.7 | ??85.7 | ??91.7 |
| GBL *Selectivity, heavy % | ??98.6 | ??98.9 | ??98.7 | ??98.7 | ??98.5 | ??96.6 | ??96.9 |
*BDO-1, the 4-butyleneglycol
The GBL-gamma-butyrolactone
Claims (9)
1, a kind of 1, the 4-butanediol gas phase dehydrogenation prepares the method for gamma-butyrolactone continuously, it is characterized in that with 1 the 4-butyleneglycol gasifies in the presence of hydrogen, under 170～250 ℃, 0.1～0.6 MPa condition with pre-reduction the catalyzer with following oxide compound expression formula contact: CuM
aO
x, M is Mn or Zr in the formula, a is the atomicity of Mn or Zr, and a=0.3～2.0, X is for satisfying the valent oxygen atomicity of above-mentioned oxide compound.
2, in accordance with the method for claim 1, it is characterized in that when M is Zr a=0.5～1.5.
3, according to claim 1 or 2 described methods, it is characterized in that hydrogen and 1, the raw materials components mole ratio of 4-butyleneglycol is 1～12: 1.
4, in accordance with the method for claim 3, it is characterized in that hydrogen and 1, the raw materials components mole ratio of 4-butyleneglycol is 3～9: 1.
5, according to claim 1 or described method, it is characterized in that 1, the weight liquid hourly space velocity of 4-butyleneglycol is 3.0～10.0 hours
-1
6,, it is characterized in that described catalyzer is that soluble salt co-precipitation in the presence of alkali of Cu, Mn or Zr makes according to claim 1 or 2 described methods.
7, in accordance with the method for claim 6, the pH value is 4～9 when it is characterized in that co-precipitation.
8, in accordance with the method for claim 6, it is characterized in that described alkali is ammoniacal liquor.
9, according to claim 1 or 2 described methods, the reduction that it is characterized in that described catalyzer be with hydrogen or carbon monoxide 250～300 ℃ of temperature, carry out under 0.5～6.0 MPa pressure finishing in 4～10 hours.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97103634A CN1058264C (en) | 1997-03-24 | 1997-03-24 | Process of preparing gamma-butyrolactone by gas phase dehydrogenation of 1,4-butanediol |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97103634A CN1058264C (en) | 1997-03-24 | 1997-03-24 | Process of preparing gamma-butyrolactone by gas phase dehydrogenation of 1,4-butanediol |
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| CN1194268A true CN1194268A (en) | 1998-09-30 |
| CN1058264C CN1058264C (en) | 2000-11-08 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101992127B (en) * | 2009-08-31 | 2013-05-08 | 中国石油化工股份有限公司 | Catalyst reduction method |
| CN104549399B (en) * | 2013-10-23 | 2017-02-15 | 中国石油化工股份有限公司 | Shell catalyst for 1, 4-butanediol vapor-phase dehydrogenation and application of shell catalyst |
| CN108246293A (en) * | 2018-01-12 | 2018-07-06 | 中国石油大学(北京) | Dehydrating alkanes alkene catalyst, preparation method and application |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1045174C (en) * | 1994-05-05 | 1999-09-22 | 化学工业部北京化工研究院 | Catalyst for preparing gamma-butyrolactone from 1,4-butanediol by dehydrogenation |
| CN1046216C (en) * | 1994-06-04 | 1999-11-10 | 中国石油化工总公司 | Catalyst for preparing 1,4-butanediol and/or gamma-butyrolactone |
| CN1048487C (en) * | 1994-08-10 | 2000-01-19 | 中国石油化工总公司 | Method for preparing gamma-butyrolactone |
| CN1046509C (en) * | 1995-06-26 | 1999-11-17 | 中国石油化工总公司 | Preparation of gamma-butyrolactone |
-
1997
- 1997-03-24 CN CN97103634A patent/CN1058264C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101992127B (en) * | 2009-08-31 | 2013-05-08 | 中国石油化工股份有限公司 | Catalyst reduction method |
| CN104549399B (en) * | 2013-10-23 | 2017-02-15 | 中国石油化工股份有限公司 | Shell catalyst for 1, 4-butanediol vapor-phase dehydrogenation and application of shell catalyst |
| CN108246293A (en) * | 2018-01-12 | 2018-07-06 | 中国石油大学(北京) | Dehydrating alkanes alkene catalyst, preparation method and application |
| CN108246293B (en) * | 2018-01-12 | 2020-02-07 | 中国石油大学(北京) | Method for preparing olefin by alkane dehydrogenation |
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