CN105315238A - Production equipment of epoxypropane - Google Patents
Production equipment of epoxypropane Download PDFInfo
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- CN105315238A CN105315238A CN201410353931.XA CN201410353931A CN105315238A CN 105315238 A CN105315238 A CN 105315238A CN 201410353931 A CN201410353931 A CN 201410353931A CN 105315238 A CN105315238 A CN 105315238A
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Abstract
The invention relates to a production equipment of epoxypropane. The production equipment is mainly used for solving a problem of the prior art that energy consumption is high. The production equipment comprises a reactor, a high pressure propylene recovery tower, a low pressure propylene recovery tower, and a depropanizing tower, wherein operation pressure of the high pressure propylene recovery tower ranges from 0.5 to 3.5MPa as gage pressure, and operation pressure of the low pressure propylene recovery tower ranges from 0.1 to 0.4MPa as gage pressure. The production equipment is capable of solving the problem preferably, and can be applied to industrial production of epoxypropane.
Description
Technical field
The present invention relates to a kind of production unit of propylene oxide.
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) there is hydrogenolysis generation isopropyl benzene in the presence of a catalyst in DMBA and H2, and 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 production unit of new propylene oxide.It is low that this equipment 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 production unit of propylene oxide, comprising:
Reactor, generates containing α for raw material hydrogen peroxide isopropyl benzene and propylene being reacted, the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane; Described reactor inlet is connected with Propylene pipes with hydrogen phosphide cumene pipeline, and described reactor outlet is connected with described liquid phase stream pipeline;
High pressure propylene recovery tower, for containing α to described, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene are separated with the liquid phase stream of propane, thus obtain the first light component stream containing propylene at tower top, obtain containing α in tower reactor, the first heavy constituent logistics of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, on a small quantity propylene and propane; The entrance of described high pressure propylene recovery tower is connected with described liquid phase stream pipeline, and tower top outlet is connected with the first light component stream pipeline, and tower reactor outlet is connected with the first heavy constituent logistics pipeline;
Low pressure propylene recovery tower, for accept from described high pressure propylene recovery tower tower reactor containing α, first heavy constituent logistics of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, on a small quantity propylene and propane, thus obtain the second light component stream containing propylene at tower top, tower reactor obtains containing α, and the second heavy constituent logistics of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene and propylene oxide is also discharged; The entrance of described low pressure propylene recovery tower is connected with the first heavy constituent logistics pipeline, and tower top outlet is connected with the second light component stream pipeline, and tower reactor outlet is connected with the second heavy constituent logistics pipeline; Described second light component stream pipeline communicates with the first pipeline, for shunting a part of second light component stream;
Depropanizing tower, for accepting the by-passing portions from described second light component stream, and is separated it, thus obtains the 3rd light component stream at tower top, obtain triple component streams and discharged in tower reactor; The entrance of described depropanizing tower is connected with the first pipeline, and tower top outlet is connected with the 3rd light component stream pipeline, and tower reactor outlet is connected with triple component streams pipeline;
First light component stream pipeline, the second light component stream pipeline and the 3rd light component stream pipeline, all communicate with described Propylene pipes;
Wherein, the working pressure of described high pressure propylene recovery tower counts 0.5 ~ 3.5MPa with gauge pressure, and the working pressure of described low pressure propylene recovery tower counts 0.1 ~ 0.4MPa 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, the working pressure of described high pressure propylene recovery tower counts 1.5 ~ 2.5MPa 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 high pressure propylene recovery column overhead service temperature is 5 ~ 80 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 ~-8 DEG C, and tower reactor service temperature is 85 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
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 of described second light component stream is 0.1 ~ 0.5 of described second light component stream weight.
In the present invention, 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.
The propylene recovery purification apparatus containing high pressure propylene recovery tower, low pressure propylene recovery tower and depropanizing tower is adopted in the present invention, first liquid phase epoxidation propane reaction product enters high pressure propylene recovery tower and refines, in epoxidation product, the propylene of 60 ~ 95 % by weight is from recovered overhead, and tower reactor obtains the crude propene oxide product containing a small amount of propylene.Crude propene oxide product containing a small amount of propylene is sent into low pressure propylene recovery tower and is proceeded to refine, recovered overhead propylene, and tower reactor obtains not containing the crude propene oxide product of propylene.Through high pressure propylene recovery tower and low pressure propylene recovery tower, in raw material, the propylene of 99 ~ 100 % by weight is recycled.Low pressure propylene recovery column overhead stream divides two portions, a part becomes Propylene recovery, another part sends into depropanizing tower, to remove the propane impurity that fresh propylene brings recycle system of reaction into, depropanizing tower tower reactor obtains the propane removed, after high pressure propylene recovery tower and low pressure propylene recovery tower still unsegregated propylene from depropanizing tower removed overhead.Adopt the present invention, first the epoxidation logistics containing propylene is separated in high pressure propylene recovery tower, makes most of propylene from removed overhead, thus decreases the inlet amount of low pressure propylene recovery tower.Therefore, the condensation that high pressure propylene recovery column overhead takes conventional water coolant to carry out propylene as cryogen is reclaimed, and only has low pressure propylene recovery column overhead need adopt the cryogen of lower temperature.Compared with prior art, energy consumption 60% can be reduced.In addition, adopt the present invention, 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 schematic diagram of present device.
In Fig. 1, I is reactor, II is high pressure propylene recovery tower, III is low pressure propylene recovery tower, IV is depropanizing tower, 1 is raw material hydrogen peroxide isopropyl benzene pipeline, 2 is Propylene pipes, 3 for containing propylene oxide, the liquid phase stream pipeline of propylene and propane, 4 is the first light component stream pipeline (being wherein high pressure propylene recovery column overhead stream), 5 is the first heavy constituent logistics pipeline (being wherein the logistics of high pressure propylene recovery tower tower reactor), 6 is the second light component stream pipeline (being wherein low pressure propylene recovery column overhead stream), 7 is the first pipeline (wherein for going the by-passing portions logistics of depropanizing tower in low pressure propylene recovery column overhead stream on a small quantity), 8 is the second heavy constituent logistics pipeline (being wherein crude propene oxide product), 9 is the 3rd light component stream pipeline (being wherein depropanizing tower overhead stream), 10 is triple component streams pipeline (being wherein propane).
In Fig. 1, raw material hydrogen peroxide isopropyl benzene and fresh propylene are reacted and are generated containing α in reactor I, the liquid phase stream 3 of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane.Logistics 3 is sent into high pressure propylene recovery tower II and is separated, and tower top obtains logistics 4, and tower reactor obtains containing α, the logistics 5 of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, on a small quantity propylene and propane.The separation of low pressure propylene recovery tower III is sent in logistics 5, and tower top obtains logistics 6, and tower reactor obtains the crude propene oxide product stream 8 (containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene and propylene oxide) removing propylene.Propylene stream 6 points of two portions of low pressure propylene recovery tower III recovered overhead, a part of logistics 7 wherein enters depropanizing tower IV, and after separation, tower top obtains logistics 9, and tower reactor obtains propylene oxide stream 10.In high pressure propylene recovery column overhead stream 4, low pressure propylene recovery column overhead stream 6, removing enters the part of depropanizing tower and depropanizing tower overhead stream 9 and loops back reactor and participate 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 and fresh propylene are reacted and are generated containing α in reactor I, the liquid phase stream 3 of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane.Logistics 3 is sent into high pressure propylene recovery tower II and is separated, and tower top obtains logistics 4, and tower reactor obtains containing α, the logistics 5 of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, on a small quantity propylene and propane.The separation of low pressure propylene recovery tower III is sent in logistics 5, and tower top obtains logistics 6, and tower reactor obtains the crude propene oxide product stream 8 removing propylene.Propylene stream 6 points of two portions of low pressure propylene recovery tower III recovered overhead, a part of logistics 7 wherein enters depropanizing tower IV, and after separation, tower top obtains logistics 9, and tower reactor obtains propylene oxide stream 10.In high pressure propylene recovery column overhead stream 4, low pressure propylene recovery column overhead stream 6, removing enters the part of depropanizing tower and depropanizing tower overhead stream 9 and loops back reactor and participate 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 high pressure propylene recovery tower is: working pressure is 1.6MPa, and tower top service temperature is 40 DEG C, and tower reactor service temperature is 72 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 20 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 60 DEG C, and theoretical plate number is 50 pieces.
The logistics 7 entering depropanizing tower is 1:2.4 with the weight ratio of low pressure propylene recovery column overhead stream 6.
Result is: high pressure propylene recovery column overhead takes temperature to be that the condensation that the water coolant 575 tons/hour of 32 DEG C carries out propylene as cryogen is reclaimed, and low pressure propylene recovery column overhead adopts temperature to be the cryogen 29.3 tons/hour of-20 DEG C.
The yield of propylene is 99.9%, Propylene recovery purity be the yield of 95%, PO product be 99.9%.Its mesohigh propylene recovery column overhead propylene recovery rate is 70%.
[embodiment 2]
With [embodiment 1], just operational condition changes.
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 high pressure propylene recovery tower is: working pressure is 1.6MPa, and tower top service temperature is 40 DEG C, and tower reactor service temperature is 87 DEG C, and theoretical plate number is 25 pieces.
The operational condition of low pressure propylene recovery tower is: working pressure is 0.2MPa, and tower top service temperature is-20 DEG C, and tower reactor service temperature is 120 DEG C, and theoretical plate number is 20 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 58 DEG C, and theoretical plate number is 50 pieces.
The logistics 7 entering depropanizing tower is 1:3 with the weight ratio of low pressure propylene recovery column overhead stream 6.
Result is: high pressure propylene recovery column overhead takes temperature to be that the condensation that the water coolant 340 tons/hour of 32 DEG C carries out propylene as cryogen is reclaimed, and low pressure propylene recovery column overhead adopts temperature to be the cryogen 32 tons/hour of-30 DEG C.
The yield of propylene is 99.9%, Propylene recovery purity be the yield of 95%, PO product be 99.9%.Its mesohigh propylene recovery column overhead propylene recovery rate is 60%.
[comparative example 1]
With [embodiment 1], just epoxidation product enters an independent 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 (8)
1. a production unit for propylene oxide, comprising:
Reactor, generates containing α for raw material hydrogen peroxide isopropyl benzene and propylene being reacted, the liquid phase stream of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene and propane; Described reactor inlet is connected with Propylene pipes with hydrogen phosphide cumene pipeline, and described reactor outlet is connected with described liquid phase stream pipeline;
High pressure propylene recovery tower, for containing α to described, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, propylene are separated with the liquid phase stream of propane, thus obtain the first light component stream containing propylene at tower top, obtain containing α in tower reactor, the first heavy constituent logistics of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, on a small quantity propylene and propane; The entrance of described high pressure propylene recovery tower is connected with described liquid phase stream pipeline, and tower top outlet is connected with the first light component stream pipeline, and tower reactor outlet is connected with the first heavy constituent logistics pipeline;
Low pressure propylene recovery tower, for accept from described high pressure propylene recovery tower tower reactor containing α, first heavy constituent logistics of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide, on a small quantity propylene and propane, thus obtain the second light component stream containing propylene at tower top, tower reactor obtains containing α, and the second heavy constituent logistics of alpha-alpha-dimethyl benzylalcohol, isopropyl benzene and propylene oxide is also discharged; The entrance of described low pressure propylene recovery tower is connected with the first heavy constituent logistics pipeline, and tower top outlet is connected with the second light component stream pipeline, and tower reactor outlet is connected with the second heavy constituent logistics pipeline; Described second light component stream pipeline communicates with the first pipeline, for shunting a part of second light component stream;
Depropanizing tower, for accepting the by-passing portions from described second light component stream, and is separated it, thus obtains the 3rd light component stream at tower top, obtain triple component streams and discharged in tower reactor; The entrance of described depropanizing tower is connected with the first pipeline, and tower top outlet is connected with the 3rd light component stream pipeline, and tower reactor outlet is connected with triple component streams pipeline;
First light component stream pipeline, the second light component stream pipeline and the 3rd light component stream pipeline, all communicate with described Propylene pipes;
Wherein, the working pressure of described high pressure propylene recovery tower counts 0.5 ~ 3.5MPa with gauge pressure, and the working pressure of described low pressure propylene recovery tower counts 0.1 ~ 0.4MPa with gauge pressure.
2. the production unit of propylene oxide 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%.
3. the production unit of propylene oxide 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%.
4. the production unit of propylene oxide according to claim 1, it is characterized in that the working pressure of described high pressure propylene recovery tower counts 1.5 ~ 2.5MPa with gauge pressure, the working pressure of described low pressure propylene recovery tower counts 0.15 ~ 0.25MPa with gauge pressure.
5. the production unit of propylene oxide according to claim 1, it is characterized in that described high pressure propylene recovery column overhead service temperature is 5 ~ 80 DEG C, tower reactor service temperature is 45 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
6. the production unit of propylene oxide according to claim 1, it is characterized in that described low pressure propylene recovery column overhead service temperature is-30 ~-8 DEG C, tower reactor service temperature is 85 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
7. the production unit of propylene oxide 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.
8. the production unit of propylene oxide according to claim 1, is characterized in that the by-passing portions of described second light component stream is 0.1 ~ 0.5 of described second light component stream weight.
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| CN201410353931.XA CN105315238B (en) | 2014-07-24 | 2014-07-24 | The production equipment of expoxy propane |
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| CN201410353931.XA CN105315238B (en) | 2014-07-24 | 2014-07-24 | The production equipment of expoxy propane |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110483445A (en) * | 2019-08-28 | 2019-11-22 | 无锡智归科技有限公司 | The dewatering process of cumyl hydroperoxide and isopropylbenzene in a kind of production of propylene oxide device and its production process |
| CN112125870A (en) * | 2020-09-15 | 2020-12-25 | 中国石油化工股份有限公司 | CHPPO device and method for optimizing epoxidation reaction system |
| CN112159371A (en) * | 2020-09-15 | 2021-01-01 | 中国石油化工股份有限公司 | Equipment and method for improving conversion rate of reaction raw materials of CHPPO device |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1505616A (en) * | 2001-04-27 | 2004-06-16 | ס�ѻ�ѧ��ҵ��ʽ���� | Process for producing propylene oxide |
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2014
- 2014-07-24 CN CN201410353931.XA patent/CN105315238B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1505616A (en) * | 2001-04-27 | 2004-06-16 | ס�ѻ�ѧ��ҵ��ʽ���� | Process for producing propylene oxide |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110483445A (en) * | 2019-08-28 | 2019-11-22 | 无锡智归科技有限公司 | The dewatering process of cumyl hydroperoxide and isopropylbenzene in a kind of production of propylene oxide device and its production process |
| CN110483445B (en) * | 2019-08-28 | 2022-10-21 | 无锡智归科技有限公司 | Epoxypropane production device and dehydration process of cumene hydroperoxide and cumene in production process thereof |
| CN112125870A (en) * | 2020-09-15 | 2020-12-25 | 中国石油化工股份有限公司 | CHPPO device and method for optimizing epoxidation reaction system |
| CN112159371A (en) * | 2020-09-15 | 2021-01-01 | 中国石油化工股份有限公司 | Equipment and method for improving conversion rate of reaction raw materials of CHPPO device |
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