CN105272939A - Epoxy propane production method - Google Patents
Epoxy propane production method Download PDFInfo
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- CN105272939A CN105272939A CN201410353733.3A CN201410353733A CN105272939A CN 105272939 A CN105272939 A CN 105272939A CN 201410353733 A CN201410353733 A CN 201410353733A CN 105272939 A CN105272939 A CN 105272939A
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- propylene
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Abstract
The invention relates to an epoxy propane production method, and is used for mainly solving the problem of high energy consumption in the prior art. The problem is better solved through adopting the technical scheme that the epoxy propane production method comprises the steps: a liquid material flow is generated from cumyl hydroperoxide and propylene in a reactor; the liquid material flow goes into a flash tank, a first light component material flow is obtained at a tank top, and a first heavy component material flow is obtained at a tank bottom; the first light component material flow goes into a high pressure propylene recovery tower, a second light component material flow is obtained at a tower top, and a second heavy component material flow is obtained at a tower kettle; the first heavy component material flow goes into a low-pressure propylene recovery tower, a third light component material flow is obtained at a tower top, and a third heavy component material flow is obtained at a tower kettle; a part of the second light component material goes into a depropanizing tower, a fourth light component material flow is obtained at a tower top, and a fourth heavy component material flow is obtained at a tower kettle; and a part of the second light component material flow except the part going into the depropanizing tower, the third light component material flow and the fourth light component material flow circulate back to the reactor. The epoxy propane production method can be used for industrial production of recovery of propylene with an epoxy propane device.
Description
Technical field
The present invention relates to a kind of propylene oxide production process.
Background technology
Propylene oxide (PO) is very important Organic Chemicals, it is the third-largest Organic chemical products that in acryloyl derivative, output is only second to polypropylene and vinyl cyanide, mainly for the production of polyethers, propylene glycol, α-amino isopropyl alcohol, non-polyether polyvalent alcohol etc., and then produce unsaturated polyester resin, urethane, tensio-active agent, fire retardant etc., be widely used in the industries such as chemical industry, light industry, medicine, food, weaving, to chemical industry and the national economic development, there is far-reaching influence.Along with the expansion of propylene oxide purposes and the growth of downstream product consumption, make the demand in propylene oxide market increasing.
The method of current industrial production propylene oxide mainly contains chlorohydrination, has the conjugated oxidation of joint product (PO/SM method and PO/MTBE method or PO/TBA method) and without the hydrogen phosphide cumene method (CHP method) of joint product.Chlorohydrination owing to producing a large amount of chlorine-contained wastewaters in process of production, environmental pollution and equipment corrosion serious; Have the conjugated oxidation of joint product to overcome the shortcomings such as the pollution of chlorohydrination and corrosion, but long flow path, investment is large, co-product is many, joint product market have impact on the production of propylene oxide to a certain extent.CHP method is owing to polluting little and not having joint product to generate the developing direction having become Producing Process of Propylene Oxide.
The technology preparing propylene oxide compound by hydrogen phosphide cumene (CHP) and propylene under the existence of fixed-bed catalytic oxidant layer is known, mainly comprises three reaction process: (1) air-oxidation hydrogen phosphide cumene; (2) there is epoxidation reaction and produce propylene oxide (PO) and α, alpha-alpha-dimethyl benzylalcohol (DMBA) in CHP and propylene under heterogeneous catalyst exists; (3) DMBA and H
2hydrogenolysis occurs in the presence of a catalyst and generates isopropyl benzene, isopropyl benzene is recycled to oxidation operation and produces CHP.For improving the transformation efficiency of CHP, usually make propylene excessive, mol ratio as n (propylene)/n (CHP) is 5 ~ 20, therefore propylene excessive is in a large number had in reaction product, for improving the refining load of epoxidation efficiency and minimizing PO, require the propylene in reaction product to carry out recycle, and circulation propylene needs higher purity, remove necessary impurity, avoid inert component to accumulate in the recycle system simultaneously.
Document CN1505616A discloses a kind of preparation method of propylene oxide, comprise the step making propylene and cumene hydroperoxide be obtained by reacting propylene oxide in the presence of a catalyst, carry out distilling with the reaction mixture making above-mentioned reactions steps obtain and from the step of distillation recovered overhead unreacted propylene, wherein the bottom temperature of distillation tower is set to 200 DEG C or lower.In the method, tower reactor goes out thick PO product, and tower top goes out propylene.Because PO has thermo-sensitivity, general industry production control bottom temperature is not higher than 130 DEG C, namely the working pressure of rectifying tower is defined, cause tower top service temperature lower than less than 40 DEG C, conventional water coolant cannot be adopted to do cryogen, the condensation that the cryogen of a large amount of lower temperature need be used to carry out propylene is reclaimed, and cause the difficulty of industrial operation, energy consumption is high.
Summary of the invention
Technical problem to be solved by this invention is that prior art exists the high problem of energy consumption, provides a kind of new propylene oxide production process.It is low that the method has energy consumption, and propylene recovery rate is high, and propane removes thoroughly, and product propylene yield is high, low equipment investment, and flow process is simple, the feature that industrializing implementation is strong.
For solving the problems of the technologies described above, the technical scheme that the present invention takes is as follows: a kind of propylene oxide production process, comprises the following steps:
A) raw material hydrogen peroxide isopropyl benzene and propylene react in the reactor and generate containing α, the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane;
B) described containing α, the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane enters flash tank, and tank deck obtains the first light component stream, obtains the first heavy constituent logistics at the bottom of tank;
C) described first light component stream enters high pressure propylene recovery tower, and after separation, tower top obtains the second light component stream, and tower reactor obtains the second heavy constituent logistics; Described second heavy constituent logistics is arranged outward;
D) described first heavy constituent logistics enters low pressure propylene recovery tower, and after separation, tower top obtains the 3rd light component stream, and tower reactor obtains triple component streams; Described triple component streams is arranged outward;
E) described second light component stream is divided into two portions, and a part wherein enters depropanizing tower, and after separation, tower top obtains the 4th light component stream, and tower reactor obtains the quadruple component streams containing propane; Described quadruple component streams is arranged outward;
F) in described second light component stream, removing enters the part of depropanizing tower, described 3rd light component stream and described 4th light component stream and loops back reactor.
In technique scheme, preferably, the working pressure of described high pressure propylene recovery tower counts 0.1 ~ 1.0MPa with gauge pressure, and the working pressure of described low pressure propylene recovery tower counts 0.1 ~ 0.3MPa with gauge pressure.More preferably, the working pressure of described high pressure propylene recovery tower counts 0.5 ~ 0.9MPa with gauge pressure, and the working pressure of described low pressure propylene recovery tower counts 0.15 ~ 0.25MPa with gauge pressure.
In technique scheme, preferably, described raw material hydrogen peroxide isopropyl benzene is obtained by cumene oxidation, is the mixture of hydrogen phosphide cumene and isopropyl benzene; In described mixture, the weight percent concentration of hydrogen phosphide cumene is 20 ~ 80%.
In technique scheme, preferably, described containing α, in the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane, by weight percentage, α, the content of alpha-alpha-dimethyl benzylalcohol is 19 ~ 50%, and the content of isopropyl benzene is 10 ~ 70%, and the content of propylene oxide is 5 ~ 20%, the content of propylene is 5 ~ 60%, and the content of propane is 0 ~ 10%.
In technique scheme, preferably, described high pressure propylene recovery column overhead service temperature is-30 ~ 20 DEG C, and tower reactor service temperature is 45 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
In technique scheme, preferably, described low pressure propylene recovery column overhead service temperature is-30 ~-16 DEG C, and tower reactor service temperature is 85 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
In technique scheme, preferably, the service temperature of flash tank is 10 ~ 120 DEG C, and working pressure counts 0.1 ~ 5.0MPa with gauge pressure.
In technique scheme, preferably, depropanizing tower working pressure counts 1.5 ~ 2.5MPa with gauge pressure, and tower top service temperature is 40 ~ 65 DEG C, and tower reactor service temperature is 40 ~ 65 DEG C, and theoretical plate number is 10 ~ 80.
In technique scheme, preferably, the by-passing portions that described second light component stream enters depropanizing tower is 0.1 ~ 0.5 of described second light component stream weight.
In the inventive method, the epoxidation reaction of hydrogen phosphide cumene and propylene is for known in the art.Usually, temperature of reaction is 40 ~ 120 DEG C, and reaction pressure is 3.5 ~ 6.8MPa, and propylene/CHP mol ratio is 5 ~ 20, CHP air speed is 0.2 ~ 1.2 hour
-1.Catalyzer used can be the SiO 2 molecular sieve catalyzer of titaniferous.
Propylene recovery in the inventive method adopts the propylene recovery process for refining containing flash tank, high pressure propylene recovery tower, low pressure propylene recovery tower and depropanizing tower, first liquid phase epoxidation propane reaction product carries out preliminary separation by flash tank, and the propylene of the overwhelming majority flashes to gas phase.The propylene gas phase containing a small amount of propylene oxide that flash distillation obtains is sent into high pressure propylene recovery tower and is refined, and tower top obtains highly purified propylene (in raw material, the propylene of 50 ~ 98 % by weight is recycled at this), and tower reactor obtains propylene oxide heavy constituent.Because high pressure propylene recovery tower tower reactor is not containing isopropyl benzene and DMBA, under control bottom temperature is no more than 120 DEG C of situations, tower pressure can be improved, make tower top that the cryogen of comparatively high temps can be used to carry out condensation high-purity propylene.Meanwhile, from the propylene of recovered overhead, separate a part and send into depropanizing tower separation, to remove the propane impurity that fresh propylene brings recycle system of reaction into.Liquid-phase reaction product at the bottom of flash tank also surplus a small amount of propylene needs to recycle, and therefore sends into low pressure propylene recovery tower and proceeds to refine.Adopt the inventive method, in epoxidation product, the propylene of 50 ~ 98 % by weight obtains recovery by flash tank and high pressure propylene recovery tower, decreases the inlet amount of low pressure propylene recovery tower.Therefore, the condensation that high pressure propylene recovery column overhead can take the cryogen of comparatively high temps to carry out propylene is reclaimed, and only has low pressure propylene recovery column overhead need adopt the cryogen of lower temperature.Compared with prior art, energy consumption 55% can be reduced.In addition, adopt the inventive method, ensure that propylene and unreacted in hydrogen phosphide cumene epoxidation reaction being separated of propylene and product propylene completely, and be stripped of in raw material propylene the inert component propane of system of bringing into, the propylene capable of circulation time propylene ring oxidation reaction system reclaimed does reaction raw materials, both ensure that the yield (can 99.9% be reached) of propylene, ensure that the purity requirement (can 95% be reached) of circulation propylene and the yield (can 99.9% be reached) of PO product simultaneously, flow process is simple, low equipment investment, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the inventive method schematic flow sheet.
In Fig. 1, I is reactor, II is flash tank, III is high pressure propylene recovery tower, IV is low pressure propylene recovery tower, V is depropanizing tower, 1 is CHP raw material, 2 is fresh propylene, 3 for containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, the liquid phase stream of propylene and propane, 4 is flash tank top gas-phase product (the first light component stream, main containing propylene, propane and propylene oxide), 5 is (the first heavy constituent logistics of liquid product at the bottom of flash tank, main containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide and propylene), 6 is high pressure propylene recovery column overhead stream (the second light component stream, main containing propylene and propane), 7 is high pressure propylene recovery tower tower reactor logistics (the second heavy constituent logistics, containing propylene oxide), 8 for entering the by-passing portions of depropanizing tower in high pressure propylene recovery column overhead stream, 9 is depropanizing tower tower reactor propylene oxide stream (quadruple component streams), 10 is depropanizing tower recovered overhead propylene (the 4th light component stream), 11 is low pressure propylene recovery column overhead Propylene recovery (the 3rd light component stream), 12 is low pressure propylene recovery tower tower reactor logistics (triple component streams, main containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, in raw material, the PO of 10 ~ 90 is separated at this).
In Fig. 1, raw material hydrogen peroxide isopropyl benzene 1, fresh propylene 2 and circulation propylene 8,10,11 reacts the liquid phase stream 3 generated containing propylene oxide, propylene and propane in reactor I.Logistics 3 is sent into flash tank II and is separated, and the gas-phase product 4 that flash distillation tank deck obtains is sent into high pressure propylene recovery tower III and refined, and the liquid product 5 obtained at the bottom of flash tank is sent into low pressure propylene recovery tower IV and refined.High pressure propylene recovery tower III overhead stream is divided into two portions, and small portion logistics 8 (accounting for 0.1 ~ 0.5 of the second light component stream 6 weight) enters depropanizing tower V and refines.Depropanizing tower V tower top obtains propylene 10, and tower reactor removes propane 9.The logistics 12 that the logistics 7 that high pressure propylene recovery tower III tower reactor obtains and low pressure propylene recovery tower IV tower reactor obtain is crude propene oxide, sends into follow-up separation system.High pressure propylene recovery tower III overhead stream removes the by-passing portions 6, low pressure propylene recovery column overhead stream 11 and the depropanizing tower overhead stream 10 that enter depropanizing tower, loops back reactor and participates in reaction.Wherein, the overhead condenser of each tower all omits and does not draw.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
As shown in Figure 1, for the PO device of 100,000 tons/year, raw material hydrogen peroxide isopropyl benzene 1, fresh propylene 2 and circulation propylene 8,10,11 reacts the liquid phase stream 3 generated containing propylene oxide, propylene and propane in reactor I.Logistics 3 is sent into flash tank II and is separated, and the gas-phase product 4 that flash distillation tank deck obtains is sent into high pressure propylene recovery tower III and refined, and the liquid product 5 obtained at the bottom of flash tank is sent into low pressure propylene recovery tower IV and refined.High pressure propylene recovery tower III overhead stream is divided into two portions, and small portion logistics 8 enters depropanizing tower V and refines.Depropanizing tower V tower top obtains propylene, and tower reactor removes propane 9.The logistics 12 that the logistics 7 that high pressure propylene recovery tower III tower reactor obtains and low pressure propylene recovery tower IV tower reactor obtain is crude propene oxide, sends into follow-up separation system.High pressure propylene recovery tower III overhead stream removes the by-passing portions, low pressure propylene recovery column overhead stream and the depropanizing tower overhead stream that enter depropanizing tower, loops back reactor and participates in reaction.
Wherein, in liquid phase stream 3, by weight percentage, α, the content of alpha-alpha-dimethyl benzylalcohol is 26%, and the content of isopropyl benzene is 6%, and the content of propylene oxide is 10%, and the content of propylene is 55%, and the content of propane is 3%.
The operational condition of flash tank is: working pressure is 1.0MPa, and tower top service temperature is 58 DEG C.
The operational condition of high pressure propylene recovery tower is: working pressure is 0.9MPa, and tower top service temperature is 19 DEG C, and tower reactor service temperature is 116 DEG C, and theoretical plate number is 30 pieces.
The operational condition of low pressure propylene recovery tower is: working pressure is 0.3MPa, and tower top service temperature is-12 DEG C, and tower reactor service temperature is 120 DEG C, and theoretical plate number is 30 pieces.
The operational condition of depropanizing tower is: working pressure is 2.0MPa, and tower top service temperature is 51 DEG C, and tower reactor service temperature is 55 DEG C, and theoretical plate number is 50 pieces.
The logistics 8 entering depropanizing tower is 10% of high pressure propylene recovery column overhead stream 6 weight.
Result is: high pressure propylene recovery column overhead takes temperature to be that the condensation that the refrigerated water 774 tons/hour (by 10 DEG C of differential thermal calculations) of 9 DEG C carries out propylene as cryogen is reclaimed, and low pressure propylene recovery column overhead adopts temperature to be the cryogen 28.3 tons/hour (by 8 DEG C of differential thermal calculations) of-20 DEG C.
The yield of propylene is 99.9%, and the purity of Propylene recovery is the yield of 95%, PO product is 99.9%.Its mesohigh propylene recovery tower reclaims total propylene 82%.
[embodiment 2]
With [embodiment 1], just raw material and operational condition change.
In liquid phase stream 3, by weight percentage, α, the content of alpha-alpha-dimethyl benzylalcohol is 26%, and the content of isopropyl benzene is 21.5%, and the content of propylene oxide is 10.5%, and the content of propylene is 39%, and the content of propane is 2%.
The operational condition of flash tank is: working pressure is 2.0MPa, and tower top service temperature is 93 DEG C.
The operational condition of high pressure propylene recovery tower is: working pressure is 0.9MPa, and tower top service temperature is 19 DEG C, and tower reactor service temperature is 120 DEG C, and theoretical plate number is 25 pieces.
The operational condition of low pressure propylene recovery tower is: working pressure is 0.3MPa, and tower top service temperature is-12 DEG C, and tower reactor service temperature is 120 DEG C, and theoretical plate number is 30 pieces.
The operational condition of depropanizing tower is: working pressure is 2.0MPa, and tower top service temperature is 50 DEG C, and tower reactor service temperature is 55 DEG C, and theoretical plate number is 50 pieces.
The logistics 8 entering depropanizing tower is 25% of high pressure propylene recovery column overhead stream 6 weight.
Result is: high pressure propylene recovery column overhead takes temperature to be that the condensation that the refrigerated water 404 tons/hour (by 10 DEG C of differential thermal calculations) of 9 DEG C carries out propylene as cryogen is reclaimed, and low pressure propylene recovery column overhead adopts temperature to be the cryogen 32.6 tons/hour (by 8 DEG C of differential thermal calculations) of-20 DEG C.
The yield of propylene is 99.9%, and the purity of Propylene recovery is the yield of 95%, PO product is 99.9%.Its mesohigh propylene recovery tower reclaims total propylene 55%.
[comparative example 1]
Raw material with [embodiment 1] enters a distillation tower, and from the unreacted propylene of distillation recovered overhead, tower reactor goes out thick PO product.
The operational condition of distillation tower is: working pressure is 0.3MPa, and tower top service temperature is-12 DEG C, and tower reactor service temperature is 120 DEG C, and theoretical plate number is 30 pieces.
Result is: tower top employing temperature is the cryogen 92.5 tons/hour of-20 DEG C.
Claims (10)
1. a propylene oxide production process, comprises the following steps:
A) raw material hydrogen peroxide isopropyl benzene and propylene react in the reactor and generate containing α, the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane;
B) described containing α, the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane enters flash tank, and tank deck obtains the first light component stream, obtains the first heavy constituent logistics at the bottom of tank;
C) described first light component stream enters high pressure propylene recovery tower, and after separation, tower top obtains the second light component stream, and tower reactor obtains the second heavy constituent logistics; Described second heavy constituent logistics is arranged outward;
D) described first heavy constituent logistics enters low pressure propylene recovery tower, and after separation, tower top obtains the 3rd light component stream, and tower reactor obtains triple component streams; Described triple component streams is arranged outward;
E) described second light component stream is divided into two portions, and a part wherein enters depropanizing tower, and after separation, tower top obtains the 4th light component stream, and tower reactor obtains the quadruple component streams containing propane; Described quadruple component streams is arranged outward;
F) in described second light component stream, removing enters the part of depropanizing tower, described 3rd light component stream and described 4th light component stream and loops back reactor.
2. propylene oxide production process according to claim 1, it is characterized in that the working pressure of described high pressure propylene recovery tower counts 0.1 ~ 1.0MPa with gauge pressure, the working pressure of described low pressure propylene recovery tower counts 0.1 ~ 0.3MPa with gauge pressure.
3. propylene oxide production process according to claim 2, it is characterized in that the working pressure of described high pressure propylene recovery tower counts 0.5 ~ 0.9MPa with gauge pressure, the working pressure of described low pressure propylene recovery tower counts 0.15 ~ 0.25MPa with gauge pressure.
4. propylene oxide production process according to claim 1, it is characterized in that described raw material hydrogen peroxide isopropyl benzene is obtained by cumene oxidation, is the mixture of hydrogen phosphide cumene and isopropyl benzene; In described mixture, the weight percent concentration of hydrogen phosphide cumene is 20 ~ 80%.
5. propylene oxide production process according to claim 1, it is characterized in that described containing α, in the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane, by weight percentage, α, the content of alpha-alpha-dimethyl benzylalcohol is 19 ~ 50%, the content of isopropyl benzene is 10 ~ 70%, the content of propylene oxide is 5 ~ 20%, and the content of propylene is 5 ~ 60%, and the content of propane is 0 ~ 10%.
6. propylene oxide production process according to claim 1, it is characterized in that described high pressure propylene recovery column overhead service temperature is-30 ~ 20 DEG C, tower reactor service temperature is 45 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
7. propylene oxide production process according to claim 1, it is characterized in that described low pressure propylene recovery column overhead service temperature is-30 ~-16 DEG C, tower reactor service temperature is 85 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
8. propylene oxide production process according to claim 1, it is characterized in that the service temperature of flash tank is 10 ~ 120 DEG C, working pressure counts 0.1 ~ 5.0MPa with gauge pressure.
9. propylene oxide production process according to claim 1, it is characterized in that depropanizing tower working pressure counts 1.5 ~ 2.5MPa with gauge pressure, tower top service temperature is 40 ~ 65 DEG C, and tower reactor service temperature is 40 ~ 65 DEG C, and theoretical plate number is 10 ~ 80.
10. propylene oxide production process according to claim 1, is characterized in that the by-passing portions that described second light component stream enters depropanizing tower is 0.1 ~ 0.5 of described second light component stream weight.
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| CN201410353733.3A CN105272939A (en) | 2014-07-24 | 2014-07-24 | Epoxy propane production method |
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| CN201410353733.3A CN105272939A (en) | 2014-07-24 | 2014-07-24 | Epoxy propane production method |
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| CN109020926A (en) * | 2017-12-19 | 2018-12-18 | 华东理工大学 | A method of it separated from propylene gas-phase epoxidation product, purify propylene oxide |
| CN112479800A (en) * | 2020-12-10 | 2021-03-12 | 常州瑞华化工工程技术股份有限公司 | Energy-saving process for recycling circulating propylene |
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| CN112479800B (en) * | 2020-12-10 | 2023-06-16 | 常州瑞华化工工程技术股份有限公司 | Energy-saving process for recycling propylene |
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Application publication date: 20160127 |