CN1534030A - Production method of epoxy chloropropane - Google Patents
Production method of epoxy chloropropane Download PDFInfo
- Publication number
- CN1534030A CN1534030A CNA031211534A CN03121153A CN1534030A CN 1534030 A CN1534030 A CN 1534030A CN A031211534 A CNA031211534 A CN A031211534A CN 03121153 A CN03121153 A CN 03121153A CN 1534030 A CN1534030 A CN 1534030A
- Authority
- CN
- China
- Prior art keywords
- solvent
- reactor
- propenyl chloride
- reaction
- epoxy chloropropane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Epoxy Compounds (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
A process for preparing the epoxy chloropropane includes reacting between chloropropene, H2O2, solvent and granular Ti-Si molecular sieve catalyst, filtering, separating to obtain the product, and returning the excessive chloropropene and separated solvent back to reactor. Its advantages are simple process, easy control of reaction temp, high utilization of H2O2, and less energy consumption.
Description
Technical field
The present invention relates to the muriatic preparation method of a kind of epoxy.More particularly, the present invention is that the direct epoxidation of a kind of chloro-alkenes prepares the muriatic method of epoxy.
Background technology
Epoxy chloropropane is owing to contain active epoxy group(ing) and chlorine atom in its molecule, thereby chemical property is quite active, become a kind of important basic Organic Chemicals 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 is raw material production with the propylene, and production method mainly contains propenyl chloride method and vinyl carbinol method.The propenyl chloride method claims high-temperature chlorination again, is the main method of producing epoxy chloropropane, technical maturity, and production process is flexible.But also there are some serious defectives in the propenyl chloride method, and many as by product, energy consumption is big, and equipment corrosion is serious, the equipment maintenance cost height, and 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 to raise significantly.The vinyl carbinol method claims the allyl acetate method again, compare with the propenyl chloride method, material consumption, energy consumption, amount of by-products and wastewater flow rate all 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 the maintenance of the equipment and the disposal of three wastes still accounts for more than 100% of gross investment.
In order to solve corrosion and the environmental issue in the epoxy chloropropane production process effectively, US4,833,260 disclose a kind of is catalyzer with the HTS, directly alkene (comprising haloolefin) is carried out epoxidation with hydrogen peroxide and produce the epoxide method.Because have strong polar compound such as water or alcohol in the reaction system, the catalysis ring-opening reaction will partly take place in the epoxide of generation, reduce the yield of epoxide.For this reason, US4,824,976, CN1319099 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 bigger, and heat-obtaining is untimely, easy temperature runaway, the invalid rate of decomposition of increase hydrogen peroxide, therefore, CN1219536A slows down reaction by add solid inert diluents in catalyzer, be beneficial to temperature control, but the useful volume of reactor descends obviously.In addition, in this reaction system, catalyst Ti-si molecular sieves is a solid, and propenyl chloride and hydrogen peroxide do not dissolve mutually, needs a kind of solvent as solvent, makes it mutual dissolving, contacts with catalyzer simultaneously, guarantees to react and carries out fast.
EP0659473A1 discloses a kind of trickle-bed reactor and method thereof that is used for chloro propylene epoxidation, catalyzer divides four sections to be filled in the 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.Epoxidation reaction with propylene is an example, under the reaction pressure more than the 1.25MPa, the mode that reaction mass is gas-liquid two-phase and 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 and replenish reinforced process, be that the reacted reactant of each section is after an indirect cooler 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, the working pressure height, temperature is controlled and is relied on the realization of systemic circulation material, needs also after reaction finishes that solvent is evaporated separation and recycles with realization, and therefore, energy consumption is very high.In addition, granules of catalyst is too big, has increased diffusional resistance, has reduced the effective rate of utilization of catalyzer.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of flow process is simple, energy consumption the is low direct epoxidation of propenyl chloride to prepare the method for epoxy chloropropane.
Method provided by the invention comprises: propenyl chloride, hydrogen peroxide, solvent and titanium-silicon molecular sieve catalyst fine particle are put into reactor and are reacted, solvent and unreacted propenyl chloride directly turn back to reactor through fractionator, slurries in the reactor after filtering, the gained clear liquid obtains the epoxy chloropropane product through separation, the concentrated slurry that gained contains catalyzer returns reactor, and isolated solvent and propenyl chloride also return reactor continuation use from clear liquid.
Method technical process provided by the invention is simple, utilizes reacting heat evaporation to separate remaining reactants and solvent, and temperature of reaction control has steadily effectively prevented the hydrogen peroxide thermolysis, hydrogen peroxide utilization ratio height, and energy consumption is low.
Description of drawings
Accompanying drawing is the production method synoptic diagram of epoxy chloropropane provided by the invention.
Embodiment
Method provided by the invention comprises: propenyl chloride, hydrogen peroxide, solvent and titanium-silicon molecular sieve catalyst fine particle are put into reactor and are reacted, solvent and unreacted propenyl chloride directly turn back to reactor through fractionator, slurries in the reactor after filtering, the gained clear liquid obtains the epoxy chloropropane product through separation, the concentrated slurry that gained contains catalyzer returns reactor, and isolated solvent and propenyl chloride also return reactor continuation use from clear liquid.
Described hydrogen peroxide is that hydrogen peroxide can be pure product, but considers that from security standpoint and economic angle preferably use the aqueous solution of hydrogen peroxide, its concentration is selected from 5%～90%, preferred 10%～60%.
Described solvent is selected from alcohol, ketone, acid, ester, particular methanol, ethanol, propyl alcohol, butanols, acetone and methylethylketone etc.These solvents also have evaporation heat-obtaining function except that having the pointed dissolving function of prior art, utilize the purpose of separating solvent, control reaction temperature thereby reach.
Described HTS is the general name that titanium atom replaces a class zeolite of a part of Siliciumatom in the lattice framework.This class material is well known in the prior art, as the titanium-containing zeolite with the MFI topological framework that is similar to the ZSM-5 aluminosilicate zeolite be TS-1, titanium-containing zeolite with the MEL topological framework that is similar to the ZSM-11 aluminosilicate zeolite is TS-2 and has and the molecular sieve containing titanium of mordenite, ZSM-12, MCM-41 and ZSM-48 isomorphous skeleton structure etc. wherein preferred TS-1 and TS-2.The used catalyzer of the present invention can be that the former powder of these zeolites directly uses, and also can be used behind spray shaping by the former powder of these zeolites.The used tackiness agent of spray shaping is generally selected non-acid colloidal sol for use, these colloidal sols can be selected from a kind of in titanium dioxide, silicon-dioxide, zirconium white, aluminum oxide and silica-alumina, the silica-titania etc., also can more used non-acid clays, if you would take off stone, kaolin, wilkinite and sepiolite.The granules of catalyst size range is 500～0.02 μ m, preferred 200～0.2 μ m.
In the reactor mol ratio of propenyl chloride and solvent be 1: 5～1: 30 preferred 1: 8～1: 20.The concentration of propenyl chloride should be higher more than 1 times than the concentration of hydrogen peroxide in the reactor.Reaction conditions is as follows: 45～100 ℃ preferred 55～80 ℃ of temperature of reaction, and the reaction absolute pressure is the preferred 0.1～1.0MPa of 0.1～2.0MPa; Mass space velocity is counted 0.05～8h with propenyl chloride during the liquid of charging
-1Preferred 0.1～6h
-1Catalyst levels is 1～60 heavy % of solvent preferred 3～30 heavy %.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but not thereby limiting the invention.
Accompanying drawing is the production method synoptic diagram of epoxy chloropropane provided by the invention.
Earlier thin granules of catalyst is put into reactor 1, propenyl chloride, hydrogen peroxide and solvent enter in the reactor 1 through pipeline 8 and react, the reaction liberated heat makes solvent and the vaporization of unreacted propenyl chloride enter the distillation tower 2 that is arranged in reactor 1 top through pipeline 9, solvent that fractionates out and propenyl chloride are back in the reactor 1 through pipeline 11, and the noncondensable gas at distillation tower 2 tops is through pipeline 10 emptyings.Slurries in the reactor 1 overflow in the strainer 3 through pipeline 12, after slurries concentrate after filtration, underflow liquid enters catalyzer tundish 4 through pipeline 13, behind solvent and propenyl chloride dilution from pipeline 18, returns reactor 1 through pipeline 14, pump 5, pipeline 15 successively and continues to use; The clear liquid that comes out from strainer 3 enters distillation tower 6 through pipeline 16, and solvent that distills out and propenyl chloride turn back to reactor 1 through pipeline 14, pump 5, pipeline 15 successively with catalyzer after pipeline 18 removes catalyzer tundish 4 dilute catalysts; The tower still component of distillation tower 6 enters distillation tower 7 through pipeline 17, and thick product is told through pipeline 19 from cat head, and by product is told through pipeline 20 from the tower still.
The present invention can realize propenyl chloride and the direct epoxidation continuous production of hydrogen peroxide epoxy chloropropane.Compared with prior art, advantage of the present invention is in particular in:
(1) adopts the direct epoxidation of hydrogen peroxide, fundamentally solved heavy corrosion and pollution problem that chlorohydrination technology exists;
(2) adopt the solvent evaporation heat-obtaining, temperature of reaction control steadily can effectively prevent the hydrogen peroxide thermolysis, hydrogen peroxide utilization ratio height;
(3) utilize reacting heat evaporation to separate remaining reactants and solvent, energy consumption is low;
(4) technical process is simple, reduces investment outlay.
The following examples will give further instruction to present method, but therefore not limit present method.
The used catalyzer trade mark is HTS among the embodiment, builds feldspar oiling worker limited-liability company by the Hunan and produces, and its active ingredient is TS-1.
Hydrogen peroxide conversion is defined as follows among the embodiment:
The transformation efficiency of hydrogen peroxide=[(n
0-n
r)/n
0] * 100%, wherein, n
0The charging mole number of representation unit time hydrogen peroxide, n
rRepresent remaining mole number,
According to reaction equation, because the hydroperoxidation of 1 molecule generates the epoxy chloropropane of 1 molecule, therefore, the selectivity definition that hydroperoxidation generates epoxy chloropropane is:
The epoxidised selectivity of hydrogen peroxide=[n
E/ (n
0-n
r)] * 100%
Wherein, n
EThe representative ring terms of oxide moles.
Embodiment 1
Used catalyzer is the former powder of HTS in the test, and the granules of catalyst size range is 300～0.02 μ m, and reaction raw materials is 27% industrial hydrogen peroxide and the industrial propenyl chloride of content more than 97%, and solvent is an analytical pure methyl alcohol.Methyl alcohol and propenyl chloride 15: 1 in molar ratio, with add the catalyzer that accounts for the heavy % of methyl alcohol 8 join in the reactor, under the pressure (absolute pressure) of 0.13MPa, be warmed up to 65 ℃, the question response system steadily after, 1: 1 in molar ratio ratio adds propenyl chloride and hydrogen peroxide, the mass space velocity 1.5h of propenyl chloride
-1The result: hydrogen peroxide conversion is 100%, and the epoxidised selectivity of hydrogen peroxide is 97.5%.
Used catalyzer is a binding agent for adopting silicon sol, the HTS of spray shaping, and the granules of catalyst size range is 300～0.02 μ m, reaction raw materials and solvent are with example 1.18: 1 in molar ratio ratio of methyl alcohol and propenyl chloride, with add the catalyzer that accounts for the heavy % of methyl alcohol 15 join in the reactor reaction device, under the pressure (absolute pressure) of 0.15MPa, be warmed up to 70 ℃, after the question response system is steady, 1: 1 in molar ratio ratio adds propenyl chloride and hydrogen peroxide, the mass space velocity 2.5h of propenyl chloride
-1Reaction result: hydrogen peroxide conversion is 100%, and the epoxidised selectivity of hydrogen peroxide is 96.1%.
Claims (7)
1, a kind of production method of epoxy chloropropane, it is characterized in that this method comprises: propenyl chloride, hydrogen peroxide, solvent and titanium-silicon molecular sieve catalyst fine particle are put into reactor and are reacted, solvent and unreacted propenyl chloride directly turn back to reactor through fractionator, slurries in the reactor after filtering, the gained clear liquid obtains the epoxy chloropropane product through separation, the concentrated slurry that gained contains catalyzer returns reactor, and isolated solvent and propenyl chloride also return reactor continuation use from clear liquid.
2,, it is characterized in that described solvent is alcohol, ketone, acid or ester according to the method for claim 1.
3,, it is characterized in that described solvent is methyl alcohol, ethanol, propyl alcohol, butanols, acetone or methylethylketone according to the method for claim 1 or 2.
4,, it is characterized in that described granules of catalyst size range is 500～0.02 μ m according to the method for claim 1.
5,, it is characterized in that the mol ratio of propenyl chloride and solvent is 1: 5～1: 30 in the reactor according to the method for claim 1.
6,, it is characterized in that described catalyst levels is 1～60 heavy % of solvent according to the method for claim 1.
7,, it is characterized in that reaction conditions is according to the method for claim 1: 45～100 ℃ of temperature of reaction, the reaction absolute pressure is 0.1～2.0MPa, mass space velocity is counted 0.05～8h with propenyl chloride during the liquid of charging
-1
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03121153 CN1275952C (en) | 2003-03-28 | 2003-03-28 | Production method of epoxy chloropropane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03121153 CN1275952C (en) | 2003-03-28 | 2003-03-28 | Production method of epoxy chloropropane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1534030A true CN1534030A (en) | 2004-10-06 |
| CN1275952C CN1275952C (en) | 2006-09-20 |
Family
ID=34285593
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03121153 Expired - Lifetime CN1275952C (en) | 2003-03-28 | 2003-03-28 | Production method of epoxy chloropropane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1275952C (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100412038C (en) * | 2004-10-27 | 2008-08-20 | 中国科学院大连化学物理研究所 | Homogeneous catalysis low boiling point olefin hydrogen peroxide continuous reaction method and system |
| CN101279958B (en) * | 2007-04-04 | 2011-01-19 | 中国石油化工股份有限公司上海石油化工研究院 | Method for preparing epoxy chloropropane by epoxidation of propylene chloride |
| CN102101848A (en) * | 2010-10-27 | 2011-06-22 | 中国石油化工股份有限公司 | Method for producing epichlorohydrin |
| CN102190635A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Method for producing epoxy chloropropane |
| CN102477018A (en) * | 2010-11-30 | 2012-05-30 | 中国科学院大连化学物理研究所 | Continuous production device for preparing epichlorohydrin by using hydrogen peroxide to oxidize chloropropene under conditions of normal pressure and no solvent |
| CN101279961B (en) * | 2007-04-04 | 2013-05-08 | 中国石油化工股份有限公司 | Method for preparing epoxy chloropropane by epoxidation of propylene chloride |
| CN103288781A (en) * | 2012-02-29 | 2013-09-11 | 中国石油化工股份有限公司 | Method for preparing epoxy chloropropane |
| CN104003961A (en) * | 2013-02-27 | 2014-08-27 | 中国石油化工股份有限公司 | Method for continuous extraction of epichlorohydrin |
| CN106800541A (en) * | 2017-01-19 | 2017-06-06 | 济南大学 | A kind of method that utilization new catalyst prepares epoxychloropropane |
| CN108794429A (en) * | 2017-05-02 | 2018-11-13 | 王圣洁 | Manufacturing device and manufacturing method for producing epoxy chloropropane by reacting chloropropene with hydrogen peroxide |
| CN110482756A (en) * | 2019-07-25 | 2019-11-22 | 江苏扬农化工集团有限公司 | A kind of method of epoxychloropropane utilization of wastewater resource |
| CN111116520A (en) * | 2019-12-12 | 2020-05-08 | 中国科学院大连化学物理研究所 | Process for producing epichlorohydrin by using titanium silicalite molecular sieve as catalyst to oxidize chloropropene |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103159703B (en) * | 2011-12-16 | 2014-09-03 | 中国科学院大连化学物理研究所 | Method of continuously producing epichlorohydrin by directly epoxidizing chloropropene |
-
2003
- 2003-03-28 CN CN 03121153 patent/CN1275952C/en not_active Expired - Lifetime
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100412038C (en) * | 2004-10-27 | 2008-08-20 | 中国科学院大连化学物理研究所 | Homogeneous catalysis low boiling point olefin hydrogen peroxide continuous reaction method and system |
| CN101279958B (en) * | 2007-04-04 | 2011-01-19 | 中国石油化工股份有限公司上海石油化工研究院 | Method for preparing epoxy chloropropane by epoxidation of propylene chloride |
| CN101279961B (en) * | 2007-04-04 | 2013-05-08 | 中国石油化工股份有限公司 | Method for preparing epoxy chloropropane by epoxidation of propylene chloride |
| CN102190635A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Method for producing epoxy chloropropane |
| CN102190635B (en) * | 2010-03-03 | 2013-06-05 | 中国石油化工股份有限公司 | Method for producing epoxy chloropropane |
| CN102101848A (en) * | 2010-10-27 | 2011-06-22 | 中国石油化工股份有限公司 | Method for producing epichlorohydrin |
| CN102477018A (en) * | 2010-11-30 | 2012-05-30 | 中国科学院大连化学物理研究所 | Continuous production device for preparing epichlorohydrin by using hydrogen peroxide to oxidize chloropropene under conditions of normal pressure and no solvent |
| CN102477018B (en) * | 2010-11-30 | 2013-08-14 | 中国科学院大连化学物理研究所 | Continuous production device for preparing epichlorohydrin by using hydrogen peroxide to oxidize chloropropene under conditions of normal pressure and no solvent |
| CN103288781A (en) * | 2012-02-29 | 2013-09-11 | 中国石油化工股份有限公司 | Method for preparing epoxy chloropropane |
| CN103288781B (en) * | 2012-02-29 | 2015-04-29 | 中国石油化工股份有限公司 | Method for preparing epoxy chloropropane |
| CN104003961A (en) * | 2013-02-27 | 2014-08-27 | 中国石油化工股份有限公司 | Method for continuous extraction of epichlorohydrin |
| CN104003961B (en) * | 2013-02-27 | 2016-05-25 | 中国石油化工股份有限公司 | A kind of method of continuous extraction epoxychloropropane |
| CN106800541A (en) * | 2017-01-19 | 2017-06-06 | 济南大学 | A kind of method that utilization new catalyst prepares epoxychloropropane |
| CN108794429A (en) * | 2017-05-02 | 2018-11-13 | 王圣洁 | Manufacturing device and manufacturing method for producing epoxy chloropropane by reacting chloropropene with hydrogen peroxide |
| CN110482756A (en) * | 2019-07-25 | 2019-11-22 | 江苏扬农化工集团有限公司 | A kind of method of epoxychloropropane utilization of wastewater resource |
| CN111116520A (en) * | 2019-12-12 | 2020-05-08 | 中国科学院大连化学物理研究所 | Process for producing epichlorohydrin by using titanium silicalite molecular sieve as catalyst to oxidize chloropropene |
| CN111116520B (en) * | 2019-12-12 | 2023-10-20 | 中国科学院大连化学物理研究所 | Process for producing epichlorohydrin by oxidizing chloropropene with titanium-silicon molecular sieve as catalyst |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1275952C (en) | 2006-09-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1275952C (en) | Production method of epoxy chloropropane | |
| CN101371989B (en) | Titanium silicon molecular sieve catalyst as well as preparation method and use thereof | |
| CN1230427C (en) | Method for production of propylene oxide | |
| CN1114495C (en) | Process for preparing composite catalyst and its application | |
| CN1444576A (en) | Method for production of propylene oxide | |
| CN1845888A (en) | Method of preparing dichloropropanols from glycerine | |
| CN1109883A (en) | Integrated process for epoxide production | |
| CN1252014A (en) | Catalyst compositions derived from titanium-containing molecular sieves | |
| CN1769277A (en) | Epichlorohydrin production process | |
| CN101172970A (en) | Method for producing epoxychloropropane | |
| CN1274680C (en) | Direct epoxidation process using a mixed catalyst system pretreated with a bromide containing agent | |
| CN1245395C (en) | Oxirane production using a peroxidized compound | |
| CN1249042C (en) | Suspension catalyst distillation process for epoxidizing alkene directly | |
| CN102190636B (en) | Method for preparing epoxy chloropropane by cyclizing chloropropene | |
| US6723861B2 (en) | Method for producing oxirane | |
| CN1286826C (en) | Catalytic distillation method of olefine direct epoxidation | |
| DE60223702T2 (en) | EPOXY DENSITY PHASE | |
| CN102442979B (en) | Preparation method of epoxypropane | |
| CN1255393C (en) | Direct epoxidation process using a mixed catalyst system | |
| CN110357835B (en) | Preparation method of epichlorohydrin | |
| CN102190637A (en) | Production method of epichlorohydrin | |
| JP2003507374A (en) | Method for preparing alkylene oxide | |
| CN110128313B (en) | Process for preparing tert-butyl hydroperoxide | |
| CN102372683A (en) | Method for preparing epichlorohydrin through chloropropene epoxidation | |
| EP1914228B1 (en) | Process for producing glycidyl 2-hydroxyisobutyrate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20060920 |
|
| CX01 | Expiry of patent term |