CN1483717A - Process for synthesizing isopropyl acetate and method for preparing its catalyst - Google Patents
Process for synthesizing isopropyl acetate and method for preparing its catalyst Download PDFInfo
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Abstract
The present invention relates to a process for synthesizing isopropyl acetate and preparation method of its catalyst. Its process adopts fixed bed reactor, uses solid catalyst, and makes reaction under the condition of gas-liquid-solid three-phase reaction, and its solid catalyst includes modified resin catalyst, silica-gel loaded heteropolyacid catalyst, silica-gel loaded phosphoric acid catalyst and super acidic catalyst, its reaction temp. is 80-125 deg.C, propylene pressure is 0.8-1.4 MPa, acetic acid feeding space velocity is 1.0-2.8 h(-1), propylene feeding space velocity is 80-108 hr(-1), and the mole ratio of acetic acid and propylene is 1:1.15-1.80. Said invention also includes the preparation method of the above-mentioned catalysts.
Description
Technical field
The present invention relates to synthesizing isopropyl acetate and Preparation of catalysts method thereof, belong to the technology of preparing of isopropyl acetate.
Background technology
Isopropyl acetate is a kind of important fine chemicals, has good alkali resistance, hydrophobicity, can be used as solvent, dewatering agent and extract drugs agent.Isopropyl acetate has than present widely used ethyl acetate and the more superior performance of n-butyl acetate, and its solubility property is better than ethyl acetate, and its volatile performance is better than n-butyl acetate.Therefore can substitute ethyl acetate, n-butyl acetate is applied to industries such as coating, printing ink, tackiness agent, pharmacy.The technology of present industrial production isopropyl acetate is: be raw material, be that the direct catalytic esterification of catalyzer makes with sulfuric acid with acetate and Virahol; There are problems such as equipment corrosion is serious, side reaction is many, product separation is difficult, production cost is high, wastewater treatment trouble in this technology.People find very early: carboxylic acid and alkene direct esterification can obtain carboxylicesters.But, adopt carboxylic acid and alkene synthesizing carboxylate not as good as adopting the reaction of carboxylic acid and alcohols more direct, more economical owing to early stage alkene usually is to be made by alcohols dehydration.So in a very long time, this technological process does not obtain people's attention.Since the seventies in 20th century, along with the development of petrochemical industry and the raising of Petroleum Processing Technology level, there are a large amount of byproduct alkene in petroleum refining industry, and it is abundant and cheap that the propylene resource becomes, and therefore the operational path by acetate and propylene direct esterification synthesis of acetic acid isopropyl ester receives publicity again.Compare with traditional acid alcohol esterification technique, the superiority of carboxylic acid/alkene esterification technique is embodied in following several aspect: (1) adopts cheap alkene to do raw material, can reduce production costs remarkable in economical benefits significantly; (2) acid/alkene technology belongs to typical green chemical industry technology, and a part acetate and the reaction of a part propylene obtain a part isopropyl acetate, produce without any unnecessary material.U.S. Pat 3644497 (1972) discloses a kind of heteropolyacid with molybdenum and tungsten as catalyzer, make the compound that contains unsaturated ethylene linkage and the technology of carboxylic acid reaction synthesizing carboxylate, reaction is carried out in tank reactor, under anhydrous condition, resultant is mainly carboxylicesters, and under the condition that has water to exist, resultant is carboxylicesters and alcohol; It is catalyzer that the clear and 47-42802 of Japanese Patent and clear and 54-52025 etc. also disclose with the heteropolyacid, is raw material with propylene and acetate, the technology of addition esterification synthesis of acetic acid isopropyl ester in tank reactor; At home, it is the research of catalyzer that Dalian University of Technology also reported with heteropolyacid (as: 12-phospho-wolframic acid, 12-silicotungstic acid, 12-phospho-molybdic acid, phospho-molybdic acid), in the research work of tank reactor discontinuous synthesis of acetic acid isopropyl ester; It is catalyzer that European patent EP 0483826A2 (1992) discloses employing acidic cation-exchange resin LEWATIT SPC118, acetate and propylene are all with the liquid form charging, wherein the acetate air speed is 1.0/h, the mol ratio of ethyl ester and propylene is 1.43: 1, the catalytic bed out temperature is respectively 85 ℃ and 92 ℃, pressure is 4.0Mpa reaction down, recording propylene conversion is 89.8%, the selectivity that propylene generates ester is 96.6%, U.S. Pat 5384426 also discloses and adopted propylene is the technology of raw material synthesis of acetic acid isopropyl ester, and discloses about the more isolating details of product.More than in the cited technology, adopt the technology of heteropolyacid catalyst to have heteropolyacid water-soluble problem and equipment corrosion problem easily.In addition, the rhythmic reaction in the tank reactor also is worthless on the angle of energy and operation.The disclosed technology of European patent EP 0483826A2 also exists system pressure too high, the problem that equipment input and maintenance cost are high.
Summary of the invention
Purpose of the present invention is exactly serious in order to overcome and solve the equipment corrosion that the technology of existing synthesis of acetic acid isopropyl ester exists, side reaction is many, the product separation difficulty, the production cost height, rhythmic reaction energy waste in wastewater treatment trouble or the still reaction is big, troublesome poeration, system pressure is too high, equipment drops into and high shortcoming and the problem of maintenance cost, research, invent a kind of not etching apparatus that has, product separation is easy, production cost is low, equipment input and maintenance cost are lower, energy waste is little, easy to operate, the worker by acetate and propylene reaction synthesis of acetic acid isopropyl ester of advantage such as practical on the industrial production.
Another object of the present invention is to provide a kind of activity of above-mentioned synthesizing isopropyl acetate use and the method for preparing catalyst that selectivity height, good stability, easy regeneration also can be recycled.
Purpose of the present invention is achieved through the following technical solutions: synthesizing isopropyl acetate is for being raw material with acetate and propylene, use solid catalyst, adopt fixed-bed reactor, under propylene self pressure, react in the mode of gas-liquid-solid phase reaction, synthesis of acetic acid isopropyl ester under the low pressure, adopt earlier successive reaction-fractionated mode to obtain thick isopropyl acetate product, obtain content greater than 99% ethyl ester isopropyl ester product through rectifying then; Its processing condition are: 80～125 ℃ of temperature of reaction, propylene pressure are 0.8～1.4Mpa, and acetate (liquid) charging air speed is: 1.0～2.8h
-1, propylene (gas) charging air speed is 80～108h
-1Acid/alkene mol ratio is 1: 1.15～1.80; Its optimum process condition is: 90～125 ℃ of temperature of reaction, pressure 0.9～1.3Mpa, acetic acid feed air speed 1.0～1.5h
-1, propylene feed air speed 80～100h
-1, acetate and propylene mol ratio are 1: 1.15～1.6.
Described solid catalyst comprises: silica gel or activated carbon supported heteropolyacid (comprising phospho-wolframic acid, phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) catalyzer, silica gel load phosphoric acid catalyst, modified resin catalyst and super acidic catalyst, wherein effect preferably catalyzer be: silica gel load heteropolyacid catalyst and modified resin catalyst demonstrate best catalytic activity.
The preparation method of described silica gel or activated carbon supported heteropolyacid catalyst is as follows: heteropolyacid (comprising phospho-wolframic acid, phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) is dissolved in is mixed with 3～10% solution in the suitable quantity of water, add silica gel or the absorption of pretreated active carbon equivalent through preroasting, drying is 24～48 hours under 110～200 ℃ of temperature, promptly makes silica gel or Catalyzed by Heteropolyacid Supported on Actived Carbon agent.
The preparation method of described modified resin catalyst is as follows: quantitatively take by weighing Platinic chloride or palladium chloride and heteropolyacid (comprising phospho-wolframic acid, phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) and be dissolved in certain water gaging, add quantitative resin catalyst, make its saturated absorption, drying is 24～48 hours under 110～130 ℃ of temperature, the content of the metal in the exchange is ten thousand/to 5/10000ths, the content of heteropolyacid is 0.1～1%.
Described super acidic catalyst preparation method is as follows: under the agitation condition, in 5～10% zirconyl chloride solution, add ammoniacal liquor, reach 10～10.5 until pH value, wore out 24～36 hours under the room temperature, extremely detect less than chlorion with the deionized water repetitive scrubbing, again suction filtration, drying, sulphuric acid soln with 0.3～0.5mol/l is handled, drying at 500～650 ℃ of roasting temperatures, promptly obtains described super acidic catalyst then.
The preparation method of the phosphoric acid catalyst of described silica gel load adds the saturated absorption of silica gel in 10～15% phosphoric acid solution, can make the phosphoric acid catalyst of silica gel load then 110～130 ℃ of following dryings.
The present invention compared with prior art has following advantage and effect: (1) the present invention adopts fixed-bed process and solid catalyst, deficiencies such as the energy consumption that can fundamentally overcome the existence of the existing equipment corrosion of traditional technology, side reaction and the reluctant problem of waste reaction solution and still reaction technology is big, troublesome poeration; (2) be raw material owing to the present invention adopts propylene, can reduce production cost of products significantly, also overcome the branch water difficulty that classical acid/pure esterification technique exists simultaneously, the problem that causes energy expenditure to increase; (3) modified resin catalyst of the present invention has good activity, selectivity and stability; As: the catalyzer that modification makes based on large hole cation exchanger resin that the present invention relates to (HD-1 type modified resin catalyst) has activity and selectivity height, good stability, regeneration easily, can recycle and repeatedly wait advantage; Under given processing condition, the acetate peak rate of conversion reaches more than 90.0%; The selectivity of the isopropyl acetate that generates is greater than 99%; At 95 ℃ of pressure is under 0.9～1.1Mpa, and 1850 hours (comprising regeneration tests) of catalyzer continuous operation, the transformation efficiency of acetate maintains more than 70%, and activity of such catalysts is kept stable basically.Catalyzer is after regeneration, and activity can return to more than 90% of initial level, the catalyzer continuous operation 850h after the regeneration, and the transformation efficiency of acetate maintains more than 70%.
Concrete embodiment
The contriver is through years of researches and test, the embodiment that a lot of successful experiments are arranged, it is as follows to think that it preferred embodiment can be: reaction tubes and preheating tube all are that the stainless steel tube of 8mm is made with the internal diameter, the loadings of catalyzer is 1～5 gram, reacting system pressure is propylene self pressure, glacial acetic acid is squeezed into micro-high pressure plunger pump metering, adopts precise temperature control equipment to carry out temperature control, and temperature-controlled precision is ± 1 ℃.Only enumerating 10 embodiment below is illustrated:
Embodiment 1:
HD-1 modified resin catalyst 2ml packs in aforesaid reaction tubes, the conditioned reaction temperature is 125 ℃, logical 8 hours deactivated catalysts of nitrogen, open micro-fresh feed pump by the per hour speed charging of 2.2ml, begin to feed propylene after 15 minutes, after the displaced air, progressively pressure boost is to 1.0Mpa under normal pressure, for promoting reaction, keeping tail propylene flow is 30ml/min.(6～8 hours) get final product sampling analysis through after a while in reaction.Product is by day island proper Tianjin GC-7A gas chromatograph analysis, and the acetate transformation efficiency is 90%, and the selectivity of the isopropyl acetate of generation is 99.1%.
Embodiment 2:
According to as embodiment 1 described condition HD-1 type modified resin catalyst having been carried out longevity test, continuous operation 1000 hours, catalyst activity drop to about 42% from 90%, and the selectivity of the isopropyl acetate of generation is 99%.
Embodiment 3:
Change into 95 ℃ except that temperature of reaction, other are with embodiment 1, and the result is: the acetate transformation efficiency is 80%, and the selectivity of isopropyl acetate is 99.0%.
Embodiment 4:
Except that temperature of reaction is changed into 95 ℃, other is with embodiment 1, and catalyzer continuous operation 1000 hours, the initial activity of catalyzer are 81% (acetate transformation efficiency), and the activity after 1000 hours is 72%, and catalyzer does not have caking, does not almost have the carbon distribution phenomenon.
Embodiment 5:
Except that catalyzer was changed into the H type macroporous resin catalyzer of non-modified, other were with embodiment 1.The result is: the acetate transformation efficiency is 84%, and the selectivity that generates isopropyl acetate is 99.3%.
Embodiment 6:
According to the condition of embodiment 4 the H type macroporous resin catalyzer of non-modified is carried out longevity test, continuous operation 400 hours, catalyst activity is changed to 51% from 84%.
Embodiment 7:
Remove catalyzer and change into SO
4 2-/ ZrO
2Outside the super acidic catalyst, other are with embodiment 1.The result is: the acetate transformation efficiency is 61%, and the selectivity of the isopropyl acetate of generation is 99.1%.
Embodiment 8:
Except that catalyzer was changed into load phosphotungstic acid or load phospho-molybdic acid or load silicotungstic acid or P-Mo-Wo acid catalyzer, other were with embodiment 1, and the result is: the acetate transformation efficiency is more than 80%, and the selectivity that generates isopropyl acetate is 98.0%～99%.
Embodiment 9:
Except that catalyzer was changed into the load phosphoric acid catalyst, other were with embodiment 1, and the result is: the acetate transformation efficiency is 91%, and the selectivity of the isopropyl acetate of generation is 99.1%.When adopting this catalyzer, activity of such catalysts can descend rapidly owing to the loss of active ingredient.
Embodiment 10:
The 2ml HD-1 modified resin catalyst of packing in as embodiment 1 described reactive system, under 95 ℃ of temperature, the acetate air speed is 1.1h
-1Condition under, continuous operation 1000 hours, the initial activity of catalyzer can reach 83% (acetate transformation efficiency), the rear catalyst activity still can reach 73～75% in 1000 hours, active fall is about 10%, the selectivity that generates isopropyl acetate is greater than 99%, and do not change with the variation in reaction times.
Embodiment 11
The heteropolyacid of silica gel load (comprising phospho-wolframic acid, phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) Preparation of catalysts method is: bead silica gel is carried out pre-treatment, and detailed process is through overpickling, washing, drying and roasting; Phospho-wolframic acid (or phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) is dissolved in is mixed with 5～10% solution in the suitable quantity of water, add the saturated absorption of bead silica gel, drop goes redundant solution then, 110～130 ℃ dry 24 hours down.Being heated to 110 ℃ before the heteropolyacid catalyst of this silica gel load uses under the condition of logical nitrogen handled 3～5 hours.
Embodiment 12
The preparation method of modified resin catalyst is: with 10 gram ordinary gel resins or macroporous resins with 95% alcohol immersion and washing three times, dry for standby (to sodium type resin, after washing, also need to carry out acid and exchange, wash then, dry) with 10% sulfuric acid; 10mg Platinic chloride and 0.2 gram phospho-wolframic acid (or phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) are dissolved in 6～10ml water, add the saturated absorption of above-mentioned pretreated resin, 110～130 ℃ of oven dry 24 hours down.Being heated to 110 ℃ before this modified resin catalyst uses under the condition of logical nitrogen handled 3～5 hours.
Claims (8)
1, a kind of synthesizing isopropyl acetate, it is characterized in that: with acetate and propylene is raw material, use solid catalyst, adopt fixed-bed reactor, under propylene self pressure, react in the mode of gas-liquid-solid phase reaction, synthesis of acetic acid isopropyl ester under the low pressure adopts earlier successive reaction-fractionated mode to obtain thick isopropyl acetate product, obtains content greater than 99% ethyl ester isopropyl ester product through rectifying then; Its processing condition are: 80～125 ℃ of temperature of reaction, propylene pressure are 0.8～1.4Mpa, and acetic acid liquid charging air speed is: 1.0～2.8h
-1, propylene gas charging air speed is 80～108h
-1, acid/alkene mol ratio is 1: 1.15～1.80.
2, synthesizing isopropyl acetate according to claim 1 is characterized in that: described processing condition the best is: temperature of reaction is 90～125 ℃, and pressure is 0.9～1.3Mpa, and the acetic acid feed air speed is 1.0～1.5h
-1, the propylene feed air speed is 80～100h
-1, acetate and propylene mol ratio are: 1: 1.15～1.6.
3, the catalyzer that adopts in the isopropyl acetate synthesis technique described in a kind of claim 1, it is characterized in that: this catalyzer is a solid catalyst, comprise silica gel or activated carbon supported heteropolyacid (comprising phospho-wolframic acid, phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) catalyzer, silica gel load phosphoric acid catalyst, modified resin catalyst and super acidic catalyst.
4, catalyzer according to claim 3 is characterized in that: the solid catalyst of better performances is silica gel or Catalyzed by Heteropolyacid Supported on Actived Carbon agent and modified resin catalyst.
5, catalyzer according to claim 3, it is characterized in that: the preparation method of described silica gel or activated carbon supported heteropolyacid catalyst is dissolved in heteropolyacid (comprising phospho-wolframic acid, phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) to be mixed with 3～10% solution in the suitable quantity of water, add silica gel or the absorption of pretreated active carbon equivalent through preroasting, drying is 24～48 hours under 110～200 ℃ of temperature, promptly makes silica gel or Catalyzed by Heteropolyacid Supported on Actived Carbon agent.
6, catalyzer according to claim 3, it is characterized in that: the preparation method of described modified resin catalyst quantitatively takes by weighing Platinic chloride or palladium chloride and heteropolyacid (comprising phospho-wolframic acid, phospho-molybdic acid, P-Mo-Wo acid, silicotungstic acid) to be dissolved in certain water gaging, add quantitative resin catalyst, make its saturated absorption, drying is 24～48 hours under 110～130 ℃ of temperature, the content of the metal in the exchange is ten thousand/to 5/10000ths, the content of heteropolyacid is 0.1～1%.
7, catalyzer according to claim 3, it is characterized in that: the super acidic catalyst preparation method is under agitation condition, in 5～10% zirconyl chloride solution, add ammoniacal liquor, reach 10～10.5, wore out 24～36 hours under the room temperature until pH value, extremely detect less than chlorion with the deionized water repetitive scrubbing, suction filtration, drying are handled drying with the sulphuric acid soln of 0.3～0.5mol/l again, at 500～650 ℃ of roasting temperatures, promptly obtain described super acidic catalyst then.
8, catalyzer according to claim 3, it is characterized in that: the preparation method of the phosphoric acid catalyst of described silica gel load adds the saturated absorption of silica gel in 10～15% phosphoric acid solution, can make the phosphoric acid catalyst of silica gel load then 110～130 ℃ of following dryings.
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| CN 03126847 CN1260203C (en) | 2003-06-13 | 2003-06-13 | Process for synthesizing isopropyl acetate and method for preparing its catalyst |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009006815A1 (en) * | 2007-07-11 | 2009-01-15 | Hunan Zhongchuang Chemical Co., Ltd | A method of protecting catalyst used for preparing low fatty ester |
| CN100463896C (en) * | 2007-02-02 | 2009-02-25 | 胡先念 | Preparation method of low-grade aliphatic ester |
| US7741527B2 (en) | 2004-07-16 | 2010-06-22 | Nippon Oil Corporation | Solid phosphoric acid catalyst and method for dimerization of olefin using the same |
| CN102757341A (en) * | 2011-04-27 | 2012-10-31 | 中国石油化工集团公司 | Preparation method of ethyl acetate and/or isopropyl acetate |
| CN104744248A (en) * | 2013-12-31 | 2015-07-01 | 湖南中创化工股份有限公司 | Method and device for preparing isopropyl acetate through reaction of propylene and acetic acid |
| CN109456179A (en) * | 2017-09-06 | 2019-03-12 | 中国科学院大连化学物理研究所 | A kind of method that oil refinery dry gas prepares ethyl acetate |
| CN113117750A (en) * | 2021-03-17 | 2021-07-16 | 南京福昌环保有限公司 | Preparation and application of continuous esterification composite catalyst for acrylic acid and ester waste oil recovery device |
-
2003
- 2003-06-13 CN CN 03126847 patent/CN1260203C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7741527B2 (en) | 2004-07-16 | 2010-06-22 | Nippon Oil Corporation | Solid phosphoric acid catalyst and method for dimerization of olefin using the same |
| CN100463896C (en) * | 2007-02-02 | 2009-02-25 | 胡先念 | Preparation method of low-grade aliphatic ester |
| WO2009006815A1 (en) * | 2007-07-11 | 2009-01-15 | Hunan Zhongchuang Chemical Co., Ltd | A method of protecting catalyst used for preparing low fatty ester |
| CN102757341A (en) * | 2011-04-27 | 2012-10-31 | 中国石油化工集团公司 | Preparation method of ethyl acetate and/or isopropyl acetate |
| CN104744248A (en) * | 2013-12-31 | 2015-07-01 | 湖南中创化工股份有限公司 | Method and device for preparing isopropyl acetate through reaction of propylene and acetic acid |
| CN109456179A (en) * | 2017-09-06 | 2019-03-12 | 中国科学院大连化学物理研究所 | A kind of method that oil refinery dry gas prepares ethyl acetate |
| CN113117750A (en) * | 2021-03-17 | 2021-07-16 | 南京福昌环保有限公司 | Preparation and application of continuous esterification composite catalyst for acrylic acid and ester waste oil recovery device |
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| CN1260203C (en) | 2006-06-21 |
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Assignee: Guangdong DE Lian Group Co., Ltd Assignor: South China University of Technology Contract fulfillment period: 2007.5.25 to 2012.5.24 contract change Contract record no.: 2009440001140 Denomination of invention: Process for synthesizing isopropyl acetate and method for preparing its catalyst Granted publication date: 20060621 License type: Exclusive license Record date: 2009.8.7 |
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