CN105294604A - Propylene oxide production device - Google Patents
Propylene oxide production device Download PDFInfo
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- CN105294604A CN105294604A CN201410354596.5A CN201410354596A CN105294604A CN 105294604 A CN105294604 A CN 105294604A CN 201410354596 A CN201410354596 A CN 201410354596A CN 105294604 A CN105294604 A CN 105294604A
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Abstract
The invention relates to a propylene oxide production device and mainly solves the problem of high energy consumption in the prior art. Equipment including a reactor, a flash tank, a high-pressure propylene recovery tower, a low-pressure propylene recovery tower and depropanizer are adopted to better solve the problem. The propylene oxide production device can be used for propylene recovery industrial production of propylene oxide devices.
Description
Technical field
The present invention relates to a kind of device producing 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 device of production propylene oxide newly.The device avoids the use of cryogenic coolant, have energy consumption low, 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 solution used in the present invention is as follows: a kind of device producing propylene oxide, comprising:
Reactor, for reacting by raw material hydrogen peroxide isopropyl benzene and propylene to the liquid phase stream generated containing propylene oxide and propylene; 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 being separated with the liquid phase stream of propylene containing propylene oxide described, thus obtain the first light component stream at tower top, obtain the first heavy constituent logistics in tower reactor, in the middle part of tower, side line obtains side-stream; Described side-stream is divided into the first side-stream and the second side-stream; The entrance of described high pressure propylene recovery tower is connected with described liquid phase stream pipeline, tower top outlet is connected with the first light component stream pipeline, tower reactor outlet is connected with the first heavy constituent logistics pipeline, be connected with side-stream pipeline in the middle part of tower, described side-stream pipeline communicates with the first side-stream pipeline and the second side-stream pipeline;
Depropanizing tower, is separated it for the first side-stream of accepting from described high pressure propylene recovery tower side line, thus obtains the second light component stream at tower top, obtain the second heavy constituent logistics containing propane and discharged in tower reactor; The entrance of described depropanizing tower is connected with the first side-stream 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;
Flash tank, is separated it for the first heavy constituent logistics of accepting from described high pressure propylene recovery tower tower reactor, thus obtains the 3rd light component stream at tank deck, at the bottom of tank, obtain triple component streams; The entrance of described flash tank is connected with described first heavy constituent logistics pipeline, and roof door is connected with the 3rd light component stream pipeline, and tank bottom outlet is connected with triple component streams pipeline;
Low pressure propylene recovery tower, for accepting the 3rd light component stream and triple component streams from described flash tank, obtains the 4th light component stream at tower top, obtains the quadruple component streams containing propylene oxide and arrange outside it in tower reactor; Described low pressure propylene recovery tower centre entrance is connected with the 3rd light component stream pipeline, and tower top first tower tray entrance is connected with triple component streams pipeline, and tower top outlet is connected with the 4th light component stream pipeline, and tower reactor outlet is connected with quadruple component streams pipeline;
Described second side-stream pipeline and the second light component stream pipeline, all communicate with described Propylene pipes.
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 0.01 ~ 0.2MPa 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 in the liquid phase stream of propylene and propylene oxide, 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%.
In technique scheme, preferably, described high pressure propylene recovery tower tower top service temperature be 5 ~ 80 DEG C, tower reactor service temperature is 45 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
In technique scheme, preferably, the tower top service temperature of described low pressure propylene recovery tower is 10 ~ 50 DEG C, and tower reactor service temperature is 70 ~ 120 DEG C, and theoretical plate number is 10 ~ 50.
In technique scheme, preferably, described 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 working pressure of described flash tank counts 0.5 ~ 1.5MPa with gauge pressure, and service temperature is 90 ~ 110 DEG C.
6, produce the device of propylene oxide according to claim 1, it is characterized in that described first side-stream weight is 0.05 ~ 0.5 of described side-stream weight.
In technique scheme, preferably, described low pressure propylene recovery column overhead the first layer tower tray is entered after described triple component streams is cooled to 10 ~ 50 DEG C again.
In technique scheme, preferably, described device also containing comprising compressor, in order to described high pressure propylene recovery tower tower reactor will be entered after described 4th light component stream supercharging again; Described suction port of compressor is connected with described 4th light component stream pipeline, exports and is connected with described high pressure propylene recovery tower tower reactor.
In technique scheme, preferably, described 4th light component stream is cooled to 10 ~ 40 DEG C and carries out liquid phase separation, and gas phase enters compressor again; The compression ratio of described compressor is 8 ~ 25, and top hole pressure counts 1.5 ~ 2.5MPa with gauge pressure, and temperature out is 10 ~ 120 DEG C.
In the present invention, the epoxidation reaction in the reactor 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.
In the inventive solutions, the most of propylene in raw material is recycled through high pressure propylene recovery tower, only has the propylene of 5 ~ 10% to obtain at depropanizing tower tower top.The propylene that high pressure propylene recovery tower reclaims is not from overhead extraction, but adopts the scheme of side take-off to be the CO/CO generated to remove reaction
2the light constituents such as the ethane that impurity and propylene feedstocks are brought into, avoid CO/CO
2enter reactive system by circulation propylene, improve the purity of circulation propylene.Low pressure propylene recovery tower adopts the reaction product liquid phase after adiabatic flash as the absorption liquid of gas phase, avoids the use of cryogenic coolant.Adopt a small amount of propylene to deliver to depropanizing tower and remove propane, avoid the accumulation of propane impurity in system of the inertia that propylene feedstocks is brought into.Adopt the present invention, both (prior art is compared to have reduced energy consumption, energy consumption 80% can be reduced), in turn ensure that the yield (can 99.9% be reached) of propylene, ensure that the purity requirement (can 95% be reached) of circulation propylene, ensure that the yield (can 99.9% be reached) of PO product, be applicable to different propylene feedstocks technical process, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is apparatus of the present invention schematic diagram.
In Fig. 1, I is reactor, II is high pressure propylene recovery tower, III is flash tank, and IV is low pressure propylene recovery tower, and V is compressor, VI is depropanizing tower, 1 is raw material hydrogen peroxide isopropyl benzene, and 2 is fresh propylene pipeline, and 3 is the liquid phase stream pipeline containing propylene and propylene oxide, 4 is that the first light component stream pipeline is (wherein for high pressure propylene recovery column overhead stream, containing CO, CO
2, ethane), 5 is that the first heavy constituent logistics pipeline is (wherein for the logistics of high pressure propylene recovery tower tower reactor, containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide and propylene), 6 is high pressure propylene recovery tower side-stream pipeline, 7 is the first side-stream pipeline, 8 is the second side-stream pipeline (being wherein high pressure propylene recovery tower Propylene recovery), 9 is the second light component stream pipeline (being wherein depropanizing tower recovered overhead propylene stream), 10 is the second heavy constituent logistics pipeline (being wherein depropanizing tower tower reactor propylene oxide stream), 11 is the 3rd light component stream pipeline (being wherein flash tank gaseous stream), 12 is that triple component streams pipeline is (wherein for flash tank liquid phase stream, containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide and a small amount of propylene), 13 is the 4th light component stream pipeline (being wherein low pressure propylene recovery column overhead stream), 14 is that quadruple component streams pipeline is (wherein for the logistics of low pressure propylene recovery tower tower reactor, crude propene oxide product, containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl benzene, propylene oxide), 15 is the 4th light component stream pipeline after supercharging.
In Fig. 1, raw material hydrogen peroxide isopropyl benzene reacts through pipeline 1 and fresh propylene the liquid phase stream generated containing propylene oxide and propylene in reactor I through pipeline 2.The described liquid phase stream containing propylene oxide and propylene is sent in the middle part of high pressure propylene recovery tower II through pipeline 3, after separation, the propylene that tower side line obtains is divided into two portions, major part propylene is sent epoxidation reaction system I back to through pipeline 8 and is participated in reaction, small portion propylene enters depropanizing tower VI through pipeline 7 and refines, the heavy constituent that tower reactor obtains is sent into adiabatic flash tank III through pipeline 5 and is separated, and the light constituent that tower top obtains is through the outer row of pipeline 4.Flash tank III pushes up the gas-phase product obtained and sends in the middle part of low pressure propylene recovery tower IV through pipeline 11, and the liquid product that flash tank III end obtains sends into the first layer tower tray through pipeline 12 as the absorption liquid of low pressure propylene recovery tower IV.The gas-phase propene of low pressure propylene recovery tower IV tower top sends into high pressure propylene recovery tower II tower reactor through pipeline 15 through pipeline 13 after compressor V supercharging, and low pressure propylene recovery tower IV tower reactor obtains not going subsequent separation system containing the epoxy propane reaction product of propylene through pipeline 14.The propane removed is arranged outward through pipeline 10 by depropanizing tower VI tower reactor, and the propylene of depropanizing tower VI recovered overhead is sent epoxidation reaction system back to through pipeline 9 and participated in reaction.
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 reacts through pipeline 1 and fresh propylene the liquid phase stream generated containing propylene oxide and propylene in reactor I through pipeline 2.The described liquid phase stream containing propylene oxide and propylene is sent in the middle part of high pressure propylene recovery tower II through pipeline 3, after separation, the propylene that tower side line obtains is divided into two portions, major part propylene is sent epoxidation reaction system I back to through pipeline 8 and is participated in reaction, small portion propylene enters depropanizing tower VI through pipeline 7 and refines, the heavy constituent that tower reactor obtains is sent into adiabatic flash tank III through pipeline 5 and is separated, and the light constituent that tower top obtains is through the outer row of pipeline 4.Flash tank III pushes up the gas-phase product obtained and sends in the middle part of low pressure propylene recovery tower IV through pipeline 11, and the liquid product that flash tank III end obtains sends into the first layer tower tray through pipeline 12 as the absorption liquid of low pressure propylene recovery tower IV.The gas-phase propene of low pressure propylene recovery tower IV tower top sends into high pressure propylene recovery tower II tower reactor through pipeline 15 through pipeline 13 after compressor V supercharging, and low pressure propylene recovery tower IV tower reactor obtains not going subsequent separation system containing the epoxy propane reaction product of propylene through pipeline 14.The propane removed is arranged outward through pipeline 10 by depropanizing tower VI tower reactor, and the propylene of depropanizing tower VI recovered overhead is sent epoxidation reaction system back to through pipeline 9 and participated in reaction.
Wherein, contain the liquid phase stream of propylene oxide and propylene in pipeline 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 counts 2.0MPa with gauge pressure, and tower top service temperature is 48 DEG C, and tower reactor service temperature is 102 DEG C, and theoretical plate number is 25 pieces.
The operational condition of low pressure propylene recovery tower is: working pressure counts 0.2MPa with gauge pressure, and tower top service temperature is 24 DEG C, and tower reactor service temperature is 106 DEG C, and theoretical plate number is 20 pieces.
The operational condition of depropanizing tower is: working pressure counts 2.0MPa with gauge pressure, and tower top service temperature is 51 DEG C, and tower reactor service temperature is 56 DEG C, and theoretical plate number is 50 pieces.
The logistics 5 entering depropanizing tower is 1:13 with the weight ratio of most of Propylene recovery logistics 6.
The operational condition of flash tank is: working pressure counts 0.7MPa with gauge pressure, and service temperature is 77 DEG C.
The operational condition of compressor is: compression ratio is 12, and top hole pressure counts 2.1MPa with gauge pressure, and temperature out is 124 DEG C.
Result is: high pressure propylene recovery column overhead take temperature be 32 DEG C water coolant 608 tons/hour as cryogen carry out propylene condensation reclaim, compressor work is 624kw.
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 92.5%.
[embodiment 2]
With [embodiment 1], just raw material and operational condition change.
Contain the liquid phase stream of propylene oxide and propylene in pipeline 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 counts 1.8MPa with gauge pressure, and tower top service temperature is 45 DEG C, and tower reactor service temperature is 124 DEG C, and theoretical plate number is 25 pieces.
The operational condition of low pressure propylene recovery tower is: working pressure counts 0.2MPa with gauge pressure, and tower top service temperature is 30 DEG C, and tower reactor service temperature is 119 DEG C, and theoretical plate number is 20 pieces.
The operational condition of depropanizing tower is: working pressure counts 2.0MPa with gauge pressure, and tower top service temperature is 51 DEG C, and tower reactor service temperature is 57 DEG C, and theoretical plate number is 50 pieces.
The logistics 7 entering depropanizing tower is 1:9 with the weight ratio of most of Propylene recovery logistics 6.
The operational condition of flash tank is: working pressure counts 0.7MPa with gauge pressure, and service temperature is 106 DEG C.
The operational condition of compressor is: compression ratio is 12, and top hole pressure counts 2.1MPa with gauge pressure, and temperature out is 124 DEG C.
Result is: high pressure propylene recovery column overhead take temperature be 32 DEG C water coolant 467 tons/hour as cryogen carry out propylene condensation reclaim, compressor work is 472kw.
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 92.5%.
[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 (9)
1. produce a device for propylene oxide, comprising:
Reactor, for reacting by raw material hydrogen peroxide isopropyl benzene and propylene to the liquid phase stream generated containing propylene oxide and propylene; 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 being separated with the liquid phase stream of propylene containing propylene oxide described, thus obtain the first light component stream at tower top, obtain the first heavy constituent logistics in tower reactor, in the middle part of tower, side line obtains side-stream; Described side-stream is divided into the first side-stream and the second side-stream; The entrance of described high pressure propylene recovery tower is connected with described liquid phase stream pipeline, tower top outlet is connected with the first light component stream pipeline, tower reactor outlet is connected with the first heavy constituent logistics pipeline, be connected with side-stream pipeline in the middle part of tower, described side-stream pipeline communicates with the first side-stream pipeline and the second side-stream pipeline;
Depropanizing tower, is separated it for the first side-stream of accepting from described high pressure propylene recovery tower side line, thus obtains the second light component stream at tower top, obtain the second heavy constituent logistics containing propane and discharged in tower reactor; The entrance of described depropanizing tower is connected with the first side-stream 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;
Flash tank, is separated it for the first heavy constituent logistics of accepting from described high pressure propylene recovery tower tower reactor, thus obtains the 3rd light component stream at tank deck, at the bottom of tank, obtain triple component streams; The entrance of described flash tank is connected with described first heavy constituent logistics pipeline, and roof door is connected with the 3rd light component stream pipeline, and tank bottom outlet is connected with triple component streams pipeline;
Low pressure propylene recovery tower, for accepting the 3rd light component stream and triple component streams from described flash tank, obtains the 4th light component stream at tower top, obtains the quadruple component streams containing propylene oxide and arrange outside it in tower reactor; Described low pressure propylene recovery tower centre entrance is connected with the 3rd light component stream pipeline, and tower top first tower tray entrance is connected with triple component streams pipeline, and tower top outlet is connected with the 4th light component stream pipeline, and tower reactor outlet is connected with quadruple component streams pipeline;
Described second side-stream pipeline and the second light component stream pipeline, all communicate with described Propylene pipes.
2. produce the device 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 0.01 ~ 0.2MPa with gauge pressure.
3. produce the device 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%.
4. produce the device of propylene oxide according to claim 1, contain described in it is characterized in that in the liquid phase stream of propylene and propylene oxide, 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%.
5. produce the device of propylene oxide according to claim 1, it is characterized in that described high pressure propylene recovery tower tower top service temperature be 5 ~ 80 DEG C, tower reactor service temperature is 45 ~ 120 DEG C, and theoretical plate number is 10 ~ 50;
The tower top service temperature of described low pressure propylene recovery tower is 10 ~ 50 DEG C, and tower reactor service temperature is 70 ~ 120 DEG C, and theoretical plate number is 10 ~ 50;
Described 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;
The working pressure of described flash tank counts 0.5 ~ 1.5MPa with gauge pressure, and service temperature is 90 ~ 110 DEG C.
6. produce the device of propylene oxide according to claim 1, it is characterized in that described first side-stream weight is 0.05 ~ 0.5 of described side-stream weight.
7. produce the device of propylene oxide according to claim 1, it is characterized in that entering described low pressure propylene recovery column overhead the first layer tower tray again after described triple component streams is cooled to 10 ~ 50 DEG C.
8. producing the device of propylene oxide according to claim 1, it is characterized in that described device also containing comprising compressor, in order to described high pressure propylene recovery tower tower reactor will be entered after described 4th light component stream supercharging again; Described suction port of compressor is connected with described 4th light component stream pipeline, exports and is connected with described high pressure propylene recovery tower tower reactor.
9. produce the device of propylene oxide according to claim 8, it is characterized in that described 4th light component stream is cooled to 10 ~ 40 DEG C and carries out liquid phase separation, gas phase enters compressor again; The compression ratio of described compressor is 8 ~ 25, and top hole pressure counts 1.5 ~ 2.5MPa with gauge pressure, and temperature out is 10 ~ 120 DEG C.
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| CN201410354596.5A CN105294604B (en) | 2014-07-24 | 2014-07-24 | Produce the device of expoxy propane |
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| CN201410354596.5A CN105294604B (en) | 2014-07-24 | 2014-07-24 | Produce the device of expoxy propane |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107261540A (en) * | 2017-07-04 | 2017-10-20 | 河南神马尼龙化工有限责任公司 | A kind of cyclohexanol Mead-Bauer recovery system |
| CN108033868A (en) * | 2017-12-28 | 2018-05-15 | 胜帮科技股份有限公司 | The separation and recovery system and method for propylene during a kind of HPPO methods production propylene oxide |
| CN109851574A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | The production method of propylene oxide |
| CN113461474A (en) * | 2021-06-30 | 2021-10-01 | 中国石油化工股份有限公司 | System and method for industrially and continuously preparing propylene oxide from propane |
| US11591303B2 (en) | 2017-11-30 | 2023-02-28 | China Petroleum & Chemical Corporation | Method and system for producing epoxyalkane |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001132004A (en) * | 1999-11-02 | 2001-05-15 | Toshihiro Hasegawa | Earthquake resistant placing method for raising of building and settlement correction work |
| CN1505616A (en) * | 2001-04-27 | 2004-06-16 | ס�ѻ�ѧ��ҵ��ʽ���� | Process for producing propylene oxide |
| CN100537553C (en) * | 2004-06-23 | 2009-09-09 | 住友化学株式会社 | Method of purifying propylene oxide |
-
2014
- 2014-07-24 CN CN201410354596.5A patent/CN105294604B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001132004A (en) * | 1999-11-02 | 2001-05-15 | Toshihiro Hasegawa | Earthquake resistant placing method for raising of building and settlement correction work |
| CN1505616A (en) * | 2001-04-27 | 2004-06-16 | ס�ѻ�ѧ��ҵ��ʽ���� | Process for producing propylene oxide |
| CN100537553C (en) * | 2004-06-23 | 2009-09-09 | 住友化学株式会社 | Method of purifying propylene oxide |
Non-Patent Citations (2)
| Title |
|---|
| 于剑昆等: "用异丙苯过氧化氢作氧化剂合成环氧丙烷的新技术", 《化学推进剂与高分子材料》 * |
| 李文忠: "CHP法生产CA 和PO的分离模拟与研究", 《中国优秀硕士学位论文工程科技1辑》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107261540A (en) * | 2017-07-04 | 2017-10-20 | 河南神马尼龙化工有限责任公司 | A kind of cyclohexanol Mead-Bauer recovery system |
| CN109851574A (en) * | 2017-11-30 | 2019-06-07 | 中国石油化工股份有限公司 | The production method of propylene oxide |
| CN109851574B (en) * | 2017-11-30 | 2021-05-11 | 中国石油化工股份有限公司 | Method for producing propylene oxide |
| US11591303B2 (en) | 2017-11-30 | 2023-02-28 | China Petroleum & Chemical Corporation | Method and system for producing epoxyalkane |
| CN108033868A (en) * | 2017-12-28 | 2018-05-15 | 胜帮科技股份有限公司 | The separation and recovery system and method for propylene during a kind of HPPO methods production propylene oxide |
| CN108033868B (en) * | 2017-12-28 | 2021-06-22 | 胜帮科技股份有限公司 | System and method for separating and recovering propylene in process of producing epoxypropane by HPPO method |
| CN113461474A (en) * | 2021-06-30 | 2021-10-01 | 中国石油化工股份有限公司 | System and method for industrially and continuously preparing propylene oxide from propane |
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