CN102190635B - Method for producing epoxy chloropropane - Google Patents
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- CN102190635B CN102190635B CN2010101163046A CN201010116304A CN102190635B CN 102190635 B CN102190635 B CN 102190635B CN 2010101163046 A CN2010101163046 A CN 2010101163046A CN 201010116304 A CN201010116304 A CN 201010116304A CN 102190635 B CN102190635 B CN 102190635B
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Abstract
The invention relates to a method for producing epoxy chloropropane, which mainly solves the problems of complex process and high energy consumption since the existing reaction distillation technique for preparing epoxy chloropropane by epoxidating chloropropene needs to be implemented by a reaction distillation tower and a product separation tower. The method is implemented in a way that: chloropropene, hydrogen peroxide and solvent are subjected to epoxidation reaction in the tower body of a reaction distillation separation tower, and in the reaction process, the components are separated; the components on the tower top are condensed and totally refluxed; the solvent/chloropropene mixture is produced from the side stream of the separation tower; the epoxy chloropropane is produced from the tower bottom; and the hydrogen peroxide/solvent mixture enters from the top of the reaction section, and the chloropropene can enter from any position of the reaction section. The reaction distillation separation tower comprises a reaction distillation separation tower body, a tower top condenser and a tower bottom reboiler, wherein the reaction distillation separation tower body comprises a raw material feed port, a tower top feed port, a tower top discharge port, a tower bottom feed port, a tower bottom discharge port, a side stream production port, a partition board, a public rectifying section, a reaction section, a production side rectifying section and a public stripping section. The technical scheme well solves the problems, and can be used for industrial production of epoxy chloropropane.
Description
Technical field
The present invention relates to a kind of method that epoxy chloropropane is produced.
Background technology
Epoxy chloropropane is owing to containing active epoxy group(ing) and chlorine atom in its molecule, thereby chemical property is quite active, become a kind of important basic organic chemical industry raw material and intermediate, be widely used in synthetic epoxy resin, glycerine, chlorohydrin rubber, medicine, agricultural chemicals, tensio-active agent, glass reinforced plastic, ion exchange resin, coating and softening agent etc.At present, epoxy chloropropane be take propylene as raw material production, and production method mainly contains propenyl chloride method and allyl acetate-allyl alcohol method.The propenyl chloride method claims again high-temperature chlorination, is the main method of producing epoxy chloropropane, technical maturity, and production process is flexible.But also there are some serious defects in the propenyl chloride method, and as by product is many, energy consumption is large, and equipment corrosion is serious, and equipment maintenance cost is high, production process produces a large amount of CaCl that contains
2with the waste water of organochlorine, serious harm environment, the investment of administering waste water accounts for 15～20% of gross investment, thereby causes the production cost of epoxy chloropropane significantly to raise.Allyl acetate-allyl alcohol method claims again the allyl acetate method, with the propenyl chloride method, compare, material consumption, energy consumption, amount of by-products and wastewater flow rate have decline in various degree, but technical process is longer, the problem of equipment corrosion and a large amount of discharge of wastewater does not still solve, and the investment of maintenance of the equipment and the disposal of three wastes still accounts for more than 10% of gross investment.
In order effectively to solve corrosion and the environmental issue in the epoxy chloropropane production process, US4,833,260 disclose and a kind ofly take HTS as catalyzer, directly alkene (comprising haloolefin) are carried out to epoxidation with hydrogen peroxide and produce the epoxide method.Owing to there being the strong polar compounds such as water or alcohol in reaction system, the catalysis ring-opening reaction will partly occur in the epoxide of generation, reduce the yield of epoxide.For this reason, US4,824,976, CN1319099A and CN1131152A disclose some and improved the assist measure of epoxide yields, as added alkaline organic or inorganic compound etc.In addition, this class exothermic heat of reaction is larger, and heat-obtaining not in time, easy temperature runaway, the decomposition rate of increase hydrogen peroxide, therefore, CN1219536A, by adding solid inert diluents to alleviate reaction in catalyzer, is beneficial to temperature control, but the useful volume of reactor obviously descends.In addition, in this reaction system, catalyst Ti-si molecular sieves is solid, and propenyl chloride and hydrogen peroxide do not dissolve mutually, needs a kind of solvent as solvent, makes it mutual dissolving, with catalyzer, contacts, and guarantees to react and carries out fast simultaneously.
EP0659473A1 discloses a kind of trickle-bed reactor for chloro propylene epoxidation and method thereof, catalyzer divides four sections to be filled in trickle-bed reactor with oarse-grained form, intersegmental riser and the liquid collecting plate of being provided with, first three section of lathe bed is the main reaction section, and indirect cooler of every section peripheral hardware is with heat-obtaining.The epoxidation reaction of propylene of take is example, under reaction pressure more than 1.25MPa, the mode that reaction mass is gas-liquid two-phase stream is flowed downward and is reacted by the bed top, on the main reaction section, reaction mixture is carried out extraction, heat exchange, returned to and supplement reinforced process, be that each section reacted reactant is after an indirect cooler is cooling, a part loops back this section, and another part and fresh feed are mixed into next section.In order to improve the transformation efficiency of hydrogen peroxide, the feed liquid that enters the 4th section does not add fresh feed, product and tail gas by bed at the bottom of extraction.This reactor structure complexity, working pressure is high, and temperature is controlled dependence systemic circulation material and is realized, and reaction also needs after finishing solvent is evaporated to separate with realization to recycle, and therefore, energy consumption is very high.In addition, granules of catalyst is too large, has increased diffusional resistance, has reduced the effective rate of utilization of catalyzer.
The epoxy chloropropane of propenyl chloride Direct Epoxidation production at present is all to adopt the on-catalytic distil process, because this reaction is strong exothermal reaction, easily heat-obtaining not in time, produce temperature runaway, increase the decomposition rate of hydrogen peroxide, and then the reduction transformation efficiency, and, because ring-opening reaction easily further occurs the epoxy chloropropane generated, generate alcohols and ethers.In addition, adopt the conventional catalyst distil process to carry out chloro propylene epoxidation reaction epoxy chloropropane processed, need reactive distillation column and product separation tower two towers to realize, have flow process complexity and the high problem of energy consumption.
Summary of the invention
Technical problem to be solved by this invention is to need reactive distillation column and product separation tower two towers to realize in current preparing epichlorohydrin through chloropropene epoxidation reaction distillation technique, there are flow process complexity and the high problem of energy consumption, a kind of method that provides new epoxy chloropropane to produce, the method has flow process simply and the low characteristics of energy consumption.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows, a kind of method that epoxy chloropropane is produced, propenyl chloride, hydrogen peroxide and solvent are separated in tower and are carried out epoxidation reaction at reaction distillation, carry out the component separation in the time of reaction, tower top is total reflux after condensation, separate tower side line extraction solvent and propenyl chloride mixture, extraction epoxy chloropropane at the bottom of tower, the mixture of hydrogen peroxide and solvent enters from the conversion zone top, propenyl chloride can enter from the optional position of conversion zone, reaction distillation is separated tower and is comprised reaction distillation separation tower body, overhead condenser, and tower bottom reboiler, wherein reaction distillation is separated tower body and is comprised material inlet, the tower top opening for feed, the tower top discharge port, opening for feed at the bottom of tower, discharge port at the bottom of tower, side line is adopted discharge port, division plate, public rectifying section, conversion zone, extraction side rectifying section, and public stripping section.
In technique scheme, in reactive distillation column, division plate is separated into public rectifying section by tower body, conversion zone, extraction side rectifying section, and public stripping section; The feeding side of division plate is conversion zone, and the extraction side of division plate is extraction side rectifying section; Between division plate top and tower top feed inlet and outlet, zone is public rectifying section, at the bottom of division plate bottom and tower between feed inlet and outlet zone be public stripping section; Material inlet is at least one; Material inlet is positioned at conversion zone, and side line is adopted discharge port and is positioned at extraction side rectifying section; Overhead condenser connects the tower top feed inlet and outlet, after side line extraction vapor condensation, carries out total reflux; Tower bottom reboiler by tower at the bottom of feed inlet and outlet connect, tower bottom outlet liquid first part enters after the reboiler vaporization and sends into import at the bottom of tower, the second section extraction is as product, the weight ratio of first part and second section material is 1～15: 1; Described solvent is alcohol, ketone, acid or ester; Catalyzer is HTS; The control temperature of conversion zone is 30～60 ℃; It is that public theoretical number of plates of rectifying section is 2～50 that reaction distillation is separated tower, and public stripping section number of theoretical plate is 5～50, and it is 5～70 that conversion zone is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 5～70; The mol ratio of propenyl chloride and hydrogen peroxide is 1～30: 1; The mass ratio of solvent and hydrogen peroxide is 1～50: 1; The weight percentage of hydrogen peroxide is 1～80%; Solvent is preferably at least one in methyl alcohol, ethanol, propyl alcohol, acetone or methylethylketone; In HTS, the mol ratio of silicon-dioxide and titanium dioxide is 10～200: 1; The control temperature of conversion zone is preferably 35～50 ℃; It is that public theoretical number of plates of rectifying section is preferably 5～10 that reaction distillation is separated tower, and public stripping section number of theoretical plate is preferably 8～15, and conversion zone is equivalent to number of theoretical plate and is preferably 10～30, and extraction side theoretical number of plates of rectifying section is preferably 15～40; The mol ratio of propenyl chloride and hydrogen peroxide is preferably 4～10: 1; The mass ratio of solvent and hydrogen peroxide is preferably 5～20: 1; The weight percentage of hydrogen peroxide is preferably 15～50%, and at the bottom of reaction distillation separation tower tower, the weight ratio of first part and second section material is preferably 3～8: 1.
In the preparing epoxy chloropropane by epoxidation of propylene chloride process, reactive distillation column is only realized the epoxidation reaction function in essence, the tower top total reflux, the reactant propenyl chloride separates and must realize in the product separation tower with the product epoxy chloropropane, so classical inverse answers distil process to be necessary for the combined process flow of reactive distillation column and product separation tower.In the present invention, reaction distillation separation tower can complete separately reaction distillation and product separation process, realizes the effect of two towers unifications.Compare with traditional technology, compare with traditional technology, flow process is simple, and reaction distillation is separated tower alternative reaction distillation tower and product separation tower.Use the present invention in the situation that the operational conditions such as 38～43 ℃ of mass ratio 10: 1, the temperature of reaction of propenyl chloride and mol ratio 5: 1, solvent and the hydrogen peroxide of hydrogen peroxide, number of theoretical plate 65 are identical, total energy consumption saves 27.7%, has obtained technique effect preferably.
The accompanying drawing explanation
Fig. 1 is the process schematic representation that epoxy chloropropane is produced.
In Fig. 1,1 separates tower body for reaction distillation, and 2 is material inlet, 3 tower top discharge ports, 4 is the tower top opening for feed, 5 is discharge port at the bottom of tower, 6 is opening for feed at the bottom of tower, and 7 adopt discharge port for side line, and 8 is public rectifying section, 9 is conversion zone, and 10 is public stripping section, and 11 is extraction side rectifying section, 12 is division plate, and 13 is overhead condenser, and 14 is tower bottom reboiler, 15 is raw material, and 16 is the side line extraction, and 17 is extraction at the bottom of tower.
As shown in Figure 1, raw material 15 enters the material inlet 2 that reaction distillation is separated tower body 1, overhead vapours enters overhead condenser 13 from tower top discharge port 3, all reflux and enter tower top opening for feed 4 after condensation, part material is adopted discharge port side line extraction 16 from side line, at the bottom of tower, from discharge port 5 dischargings at the bottom of tower, a part is sent into after reboiler 14 evaporations and is entered opening for feed 6 at the bottom of tower, and a part is as extraction at the bottom of tower 17.
Below by specific embodiment, the present invention is further illustrated, and still, scope of the present invention has more than and is limited to the scope that embodiment covers.
Embodiment
[embodiment 1]
Press epichlorohydrin production process shown in Fig. 1, public theoretical number of plates of rectifying section is 5, and public stripping section number of theoretical plate is 10, and it is 25 that the conversion zone separation efficiency is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 25.The catalyzer of conversion zone filling is SiO
2/ TiO
2the HTS of mol ratio 80, the 1st theoretical stage that 30 % by weight hydrogen peroxide and carbinol mixture (methanol content 70 % by weight) enter conversion zone with 1.00 gram/minute flows (counted from top to bottom, as follows), propenyl chloride enters from the conversion zone bottom respectively with 2.00 gram/minute flows, the tower top total reflux, side line is from the 10th theoretical stage extraction 2.49 gram/minute of compartmented, all the other are from extraction at the bottom of tower, the weight ratio of first part and second section material is preferably 5: 1, it is 38～43 ℃ that catalyst reaction section is controlled temperature, after stable operation, there is no epoxy chloropropane in side line extraction stream thigh, at the bottom of tower, extraction is not containing propenyl chloride and methyl alcohol, energy consumption at the bottom of tower top and tower, and compare with comparative example and save energy consumption in Table 1.
[embodiment 2]
Press epichlorohydrin production process shown in Fig. 1, public stripping section number of theoretical plate is 30, and it is 45 that the conversion zone separation efficiency is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 45.The catalyzer of conversion zone filling is SiO
2/ TiO
2the HTS of mol ratio 180, 50 % by weight hydrogen peroxide and acetone mixture (acetone content 70 % by weight) are with 1.00 gram/minute flows, and propenyl chloride enters from the catalyst reaction section bottom with 12.00 gram/minute flows, side line is from the 40th theoretical stage extraction 12.36 gram/minute of compartmented, all the other are from extraction at the bottom of tower, the weight ratio of first part and second section material is preferably 1: 1, the catalyst reaction section temperature is 32～38 ℃, after stable operation, there is no epoxy chloropropane in side line extraction stream thigh, at the bottom of tower, extraction is not containing propenyl chloride and methyl alcohol, energy consumption at the bottom of tower top and tower, and compare with comparative example and save energy consumption in Table 1.
[embodiment 3]
Press epichlorohydrin production process shown in Fig. 1, public theoretical number of plates of rectifying section is 3, and public stripping section number of theoretical plate is 5, and it is 5 that the conversion zone separation efficiency is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 5.The catalyzer of conversion zone filling is SiO
2/ TiO
2the HTS of mol ratio 20, 2 % by weight hydrogen peroxide and ethyl acetate mixture (ethyl acetate content 50 % by weight) enter the 1st theoretical stage of conversion zone with 1.00 gram/minute flows, propenyl chloride enters from the catalyst reaction section bottom with 5.00 gram/minute flows, the tower top total reflux, side line is from the 3rd theoretical stage extraction 5.48 gram/minute of compartmented, all the other are from extraction at the bottom of tower, the weight ratio of first part and second section material is preferably 15: 1, the catalyst reaction section temperature is 37～42 ℃, after stable operation, there is no epoxy chloropropane in side line extraction stream thigh, at the bottom of tower, extraction is not containing propenyl chloride and methyl alcohol, energy consumption at the bottom of tower top and tower, and compare with comparative example and save energy consumption in Table 1.
[embodiment 4]
Press epichlorohydrin production process shown in Fig. 1, public theoretical number of plates of rectifying section is 10, and public stripping section number of theoretical plate is 15, and it is 20 that the conversion zone separation efficiency is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 20.The catalyzer of conversion zone filling is SiO
2/ TiO
2the HTS of mol ratio 60, 75 % by weight hydrogen peroxide and acetate mixture (acetic acid content 50 % by weight) enter the 1st theoretical stage of conversion zone with 1.00 gram/minute flows, propenyl chloride enters from the conversion zone bottom with 3.00 gram/minute flows, the tower top total reflux, side line is from the 20th theoretical stage extraction 3.46 gram/minute of compartmented, all the other are from extraction at the bottom of tower, the weight ratio of first part and second section material is preferably 8: 1, the catalyst reaction section temperature is 55～60 ℃, after stable operation, there is no epoxy chloropropane in side line extraction stream thigh, at the bottom of tower, extraction is not containing propenyl chloride and methyl alcohol, energy consumption at the bottom of tower top and tower, and compare with comparative example and save energy consumption in Table 1.
[embodiment 5]
Press epichlorohydrin production process shown in Fig. 1, public theoretical number of plates of rectifying section is 8, and public stripping section number of theoretical plate is 10, and it is 15 that the conversion zone separation efficiency is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 15.The catalyzer of conversion zone filling is SiO
2/ TiO
2the HTS of mol ratio 120, 40 % by weight hydrogen peroxide and acetone mixture (acetone content 20 % by weight) enter the 1st theoretical stage of conversion zone with 1.00 gram/minute flows, propenyl chloride enters from the catalyst reaction section bottom with 4.00 gram/minute flows, the tower top total reflux, side line is from the 10th theoretical stage extraction 3.48 gram/minute of compartmented, all the other are from extraction at the bottom of tower, the weight ratio of first part and second section material is preferably 10: 1, the catalyst reaction section temperature is 40～45 ℃, after stable operation, there is no epoxy chloropropane in side line extraction stream thigh, at the bottom of tower, extraction is not containing propenyl chloride and methyl alcohol, energy consumption at the bottom of tower top and tower, and compare with comparative example and save energy consumption in Table 1.
[embodiment 6]
Press epichlorohydrin production process shown in Fig. 1, public theoretical number of plates of rectifying section is 15, and public stripping section number of theoretical plate is 18, and it is 10 that the conversion zone separation efficiency is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 15.The catalyzer of conversion zone filling is SiO
2/ TiO
2the HTS of mol ratio 60, 40 % by weight hydrogen peroxide and butanols mixture (butanol content 20 % by weight) enter the 1st theoretical stage of conversion zone with 1.00 gram/minute flows, propenyl chloride enters from the catalyst reaction section bottom with 4.00 gram/minute flows, tower top total reflux side line is from the 10th theoretical stage extraction 3.48 gram/minute of compartmented, all the other are from extraction at the bottom of tower, the weight ratio of first part and second section material is preferably 7: 1, the catalyst reaction section temperature is 52～58 ℃, after stable operation, there is no epoxy chloropropane in side line extraction stream thigh, at the bottom of tower, extraction is not containing propenyl chloride and butanols, energy consumption at the bottom of tower top and tower, and compare with comparative example and save energy consumption in Table 1.
The energy consumption result of each embodiment of table 1
| Embodiment | Tower top energy consumption/thousand collection/hour | Energy consumption/kilojoule at the bottom of tower/hour | Total energy consumption reduction/% |
| 1 | -0.65 | 0.89 | 27.7 |
| 2 | -0.85 | 1.03 | 11.7 |
| 3 | -0.73 | 0.94 | 21.6 |
| 4 | -0.68 | 0.86 | 27.7 |
| 5 | -0.71 | 0.90 | 24.4 |
| 6 | -0.72 | 0.93 | 22.5 |
[comparative example 1]
Traditionally, flow process is that reactive distillation column and product separation tower two towers form.The reactive distillation column theoretical number of plates of rectifying section is 5, and it is 25 that the catalyst reaction section separation efficiency is equivalent to number of theoretical plate, and the stripping section number of theoretical plate is 10, and product separation tower theoretical number of plates of rectifying section is 15, and the stripping section number of theoretical plate is 10.Catalyzer is SiO
2/ TiO
2the HTS of mol ratio 80, the 10th theoretical stage that 30 % by weight hydrogen peroxide and carbinol mixture (methanol content 70 % by weight) enter reactive distillation column with 1.00 gram/minute flows (counted from top to bottom, as follows), propenyl chloride enters from the catalyst reaction section bottom with 2.00 gram/minute flows, the total reflux of reaction distillation column overhead, reactant and product all enter the product separation tower, the tower top total reflux, after stable operation, there is no epoxy chloropropane in product separation column overhead extraction stream thigh, at the bottom of tower, extraction is not containing propenyl chloride and methyl alcohol, reactive distillation column overhead condenser energy consumption be-0.38 kilojoule/hour, the tower bottom reboiler energy consumption be 0.34 kilojoule/hour, product separation column overhead condenser energy consumption be-0.54 kilojoule/hour, the tower bottom reboiler energy consumption be 0.87 kilojoule/hour.
Claims (8)
1. the method that an epoxy chloropropane is produced, propenyl chloride, hydrogen peroxide and solvent are separated in the tower tower body and be take HTS and carry out epoxidation reaction as catalyzer at reaction distillation, carry out the component separation in the time of reaction, tower top is total reflux after condensation, separate tower side line extraction solvent and propenyl chloride mixture, extraction epoxy chloropropane at the bottom of tower, the mixture of hydrogen peroxide and solvent enters from the conversion zone top, propenyl chloride can enter from the optional position of conversion zone, reaction distillation is separated tower and is comprised reaction distillation separation tower body, overhead condenser, and tower bottom reboiler, wherein reaction distillation is separated tower body and is comprised material inlet, the tower top opening for feed, the tower top discharge port, opening for feed at the bottom of tower, discharge port at the bottom of tower, side line is adopted discharge port, division plate, public rectifying section, conversion zone, extraction side rectifying section, and public stripping section.
2. the method that epoxy chloropropane is produced according to claim 1, is characterized in that in reactive distillation column, division plate is separated into public rectifying section by tower body, conversion zone, extraction side rectifying section, and public stripping section; The feeding side of division plate is conversion zone, and the extraction side of division plate is extraction side rectifying section; Between division plate top and tower top feed inlet and outlet, zone is public rectifying section, at the bottom of division plate bottom and tower between feed inlet and outlet zone be public stripping section.
3. the method that epoxy chloropropane is produced according to claim 1, is characterized in that material inlet is at least one.
4. according to the method for claim 1 and 2 described epoxy chloropropane productions, it is characterized in that material inlet is positioned at conversion zone, side line is adopted discharge port and is positioned at extraction side rectifying section; Side line adopts condenser that the tower top feed inlet and outlet is connected, and after the tower top outlet vapor condensation, carries out total reflux; Tower bottom reboiler by tower at the bottom of feed inlet and outlet connect, tower bottom outlet liquid first part enters after the reboiler vaporization and sends into import at the bottom of tower, the second section extraction is as product, the weight ratio of first part and second section material is 1～15: 1.
5. the method that epoxy chloropropane is produced according to claim 1, is characterized in that described solvent is for alcohol, ketone, acid or ester; The control temperature of conversion zone is 30～60 ℃.
6. the method that epoxy chloropropane is produced according to claim 1, it is characterized in that it is that public theoretical number of plates of rectifying section is 2～50 that described reaction distillation is separated tower, public stripping section number of theoretical plate is 5～50, it is 5～70 that conversion zone is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 5～70; The mol ratio of propenyl chloride and hydrogen peroxide is 1～30: 1; The mass ratio of solvent and hydrogen peroxide is 1～50: 1; The weight percentage of hydrogen peroxide is 1～80%.
7. the method that epoxy chloropropane is produced according to claim 5, is characterized in that described solvent is at least one in methyl alcohol, ethanol, propyl alcohol, acetone or methylethylketone; In described HTS, the mol ratio of silicon-dioxide and titanium dioxide is 10～200: 1; The control temperature of conversion zone is 35～50 ℃.
8. the method that epoxy chloropropane is produced according to claim 6, it is characterized in that it is that public theoretical number of plates of rectifying section is 5～10 that described reaction distillation is separated tower, public stripping section number of theoretical plate is 8～15, it is 10～30 that conversion zone is equivalent to number of theoretical plate, and extraction side theoretical number of plates of rectifying section is 15～30; The mol ratio of propenyl chloride and hydrogen peroxide is 4～10: 1; The mass ratio of solvent and hydrogen peroxide is 5～20: 1; The weight percentage of hydrogen peroxide is 15～50%.
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| CN2010101163046A CN102190635B (en) | 2010-03-03 | 2010-03-03 | Method for producing epoxy chloropropane |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1534030A (en) * | 2003-03-28 | 2004-10-06 | 中国石油化工股份有限公司 | Production method of epoxy chloropropane |
| CN1534031A (en) * | 2003-03-28 | 2004-10-06 | 中国石油化工股份有限公司 | Catalytic distillation method of olefine direct epoxidation |
| CN1542008A (en) * | 2003-04-29 | 2004-11-03 | 中国石油化工股份有限公司 | Suspension catalyst distillation process for epoxidizing alkene directly |
| CN101293882A (en) * | 2007-04-24 | 2008-10-29 | 中国石油化工股份有限公司 | Process for the separation of epoxychloropropane |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1534030A (en) * | 2003-03-28 | 2004-10-06 | 中国石油化工股份有限公司 | Production method of epoxy chloropropane |
| CN1534031A (en) * | 2003-03-28 | 2004-10-06 | 中国石油化工股份有限公司 | Catalytic distillation method of olefine direct epoxidation |
| CN1542008A (en) * | 2003-04-29 | 2004-11-03 | 中国石油化工股份有限公司 | Suspension catalyst distillation process for epoxidizing alkene directly |
| CN101293882A (en) * | 2007-04-24 | 2008-10-29 | 中国石油化工股份有限公司 | Process for the separation of epoxychloropropane |
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