CN105294604B - Produce the device of expoxy propane - Google Patents
Produce the device of expoxy propane Download PDFInfo
- Publication number
- CN105294604B CN105294604B CN201410354596.5A CN201410354596A CN105294604B CN 105294604 B CN105294604 B CN 105294604B CN 201410354596 A CN201410354596 A CN 201410354596A CN 105294604 B CN105294604 B CN 105294604B
- Authority
- CN
- China
- Prior art keywords
- tower
- stream
- pipeline
- propylene
- expoxy propane
- 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.)
- Active
Links
Abstract
The present invention relates to a kind of device for producing expoxy propane, mainly solves the problems, such as that prior art has high energy consumption.The present invention preferably solves the problem by using the equipment containing reactor, flash tank, high pressure propylene recovery tower, low pressure propylene recovery tower and depropanizing tower, in the industrial production available for propylene oxide unit Propylene recovery.
Description
Technical field
The present invention relates to a kind of device for producing expoxy propane.
Background technology
Expoxy propane (PO) is very important Organic Chemicals, be in acryloyl derivative yield be only second to polypropylene and
The third-largest Organic chemical products of acrylonitrile, mainly for the production of polyethers, propane diols, isopropanolamine, non-polyether polyalcohol etc., enter
And unsaturated polyester resin, polyurethane, surfactant, fire retardant etc. are produced, it is widely used in chemical industry, light industry, medicine, food
The industries such as product, weaving, there is far-reaching influence to chemical industry and the national economic development.With expoxy propane purposes expansion and
The growth of downstream product dosage, make the demand in expoxy propane market increasing.
At present the method for industrial production expoxy propane mainly have chlorohydrination, have joint product conjugated oxidation (PO/SM methods and
PO/MTBE methods or PO/TBA methods) and cumyl hydroperoxide method (CHP methods) without joint product.Chlorohydrination is due in production process
Middle to produce substantial amounts of chlorine-contained wastewater, environmental pollution and equipment corrosion are serious；The conjugated oxidation for having joint product overcomes chlorohydrination
The shortcomings of pollution and corrosion, but long flow path, investment is big, co-product is more, and joint product market have impact on epoxy third to a certain extent
The production of alkane.CHP methods are due to polluting developing direction that is small and having turned into Producing Process of Propylene Oxide without joint product generation.
Propylene oxide compound is prepared by cumyl hydroperoxide (CHP) and propylene in the presence of fixed-bed catalytic oxidant layer
Technology be known, mainly include three courses of reaction：(1) air-oxidation cumyl hydroperoxide；(2)CHP
Epoxidation reaction production expoxy propane (PO) and alpha, alpha-dimethyl benzyl alcohol (DMBA) occurs in the presence of heterogeneous catalyst with propylene；
(3) hydrogenolysis generation isopropylbenzene occurs in the presence of a catalyst for DMBA and H2, and isopropylbenzene is recycled to oxidation operation production CHP.
To improve CHP conversion ratio, generally make propylene excessive, if n (propylene)/n (CHP) mol ratio is 5~20, therefore reaction product
In have the propylene of a large amount of excess, to improve epoxidation efficiency and reducing PO refined load, it is desirable to by the propylene in reaction product
Recycled, and circulate propylene to need higher purity, remove necessary impurity, while avoid inert component in cyclic system
Accumulated in system.
Document CN1505616A discloses a kind of preparation method of expoxy propane, including propylene is existed with cumene hydroperoxide
The step of reaction obtains expoxy propane in the presence of catalyst, and the reactant mixture for obtaining above-mentioned reactions steps are distilled simultaneously
The step of propylene unreacted from distillation recovered overhead, the bottom temperature of wherein destilling tower is set to 200 DEG C or lower.This method
In, tower reactor goes out thick PO products, and tower top goes out propylene.Because PO has thermal sensitivity, general industry production control bottom temperature is not higher than
130 DEG C, that is, the operating pressure of rectifying column is defined, cause tower top operation temperature to be less than less than 40 DEG C, the cold of routine can not be used
But water does cryogen, and the cryogen of a large amount of lower temperatures need to be used to carry out the condensation recovery of propylene, causes the difficulty of industrial operation, energy consumption
It is high.
The content of the invention
The technical problems to be solved by the invention are that prior art has the problem of high energy consumption, there is provided a kind of new production ring
The device of Ethylene Oxide.The device avoids the use of cryogenic coolant, has energy consumption low, and propylene recovery rate is high, and propane removing is thorough,
Product propylene high income, the characteristics of low equipment investment, flow is simple, and industrializing implementation is strong.
In order to solve the above technical problems, the technical solution adopted by the present invention is as follows：A kind of device for producing expoxy propane, bag
Include：
Reactor, for the liquid phase thing containing expoxy propane and propylene by raw material hydrogen peroxide isopropylbenzene and propylene reaction generation
Stream；The reactor inlet is connected with cumyl hydroperoxide pipeline and Propylene pipes, the reactor outlet and the liquid phase
Logistics pipeline is connected；
High pressure propylene recovery tower, for being separated to the liquid phase stream containing expoxy propane and propylene, so as in tower
Top obtains the first light component stream, obtains the first heavy constituent logistics in tower reactor, side line obtains side-stream in the middle part of tower；The side line
Logistics is divided into the first side-stream and the second side-stream；The entrance of the high pressure propylene recovery tower and the liquid phase stream pipeline
It is connected, 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, in the middle part of tower
It is connected with side-stream pipeline, the side-stream pipeline communicates with the first side-stream pipeline and the second side-stream pipeline；
Depropanizing tower, for receiving the first side-stream from the high pressure propylene recovery tower side line and dividing it
From so as in tower top obtain the second light component stream, obtaining the second heavy constituent logistics containing propane in tower reactor and discharge it；Institute
The entrance for stating depropanizing tower is connected with the first side-stream pipeline, and tower top outlet is connected with the second light component stream pipeline, tower reactor
Outlet is connected with the second heavy constituent logistics pipeline；
Flash tank, for receiving the first heavy constituent logistics from the high pressure propylene recovery tower tower reactor and dividing it
From so as in tank deck obtain the 3rd light component stream, triple component streams are obtained in tank bottom；The entrance of the flash tank and institute
State the first heavy constituent logistics pipeline to be connected, roof door is connected with the 3rd light component stream pipeline, tank bottom outlet and the 3rd restructuring
Logistics pipeline is divided to be connected；
Low pressure propylene recovery tower, for receiving from the 3rd light component stream of the flash tank and the 3rd heavy constituent thing
Stream, the 4th light component stream is obtained in tower top, is obtained the quadruple component streams containing expoxy propane in tower reactor and will be arranged outside it；Institute
State low pressure propylene recovery tower centre entrance with the 3rd light component stream pipeline to be connected, tower top the first tower tray entrance and the 3rd heavy constituent
Logistics pipeline is connected, and tower top outlet is connected with the 4th light component stream pipeline, tower reactor outlet and quadruple component streams pipeline phase
Even；
The second side-stream pipeline and the second light component stream pipeline, are all communicated with the Propylene pipes.
In above-mentioned technical proposal, it is preferable that the operating pressure of the high pressure propylene recovery tower is calculated as 1.5 with gauge pressure~
2.5MPa, the operating pressure of the low pressure propylene recovery tower are calculated as 0.01~0.2MPa with gauge pressure.
In above-mentioned technical proposal, it is preferable that the raw material hydrogen peroxide isopropylbenzene is obtained by cumene oxidation, is
The mixture of hydrogen oxide isopropylbenzene and isopropylbenzene；In the mixture, the weight percent concentration of cumyl hydroperoxide is 20
~80%.
In above-mentioned technical proposal, it is preferable that in the liquid phase stream containing propylene and expoxy propane, with percentage by weight
Meter, α, the content of alpha-alpha-dimethyl benzylalcohol are 19~50%, and the content of isopropylbenzene is 10~70%, the content of expoxy propane for 5~
20%, the content of propylene is 5~60%, and the content of propane is 0~10%.
In above-mentioned technical proposal, it is preferable that the tower top operation temperature of the high pressure propylene recovery tower is 5~80 DEG C, tower
Kettle operation temperature is 45~120 DEG C, and theoretical cam curve is 10~50.
In above-mentioned technical proposal, it is preferable that the tower top operation temperature of the low pressure propylene recovery tower is 10~50 DEG C, tower reactor
Operation temperature is 70~120 DEG C, and theoretical cam curve is 10~50.
In above-mentioned technical proposal, it is preferable that the depropanizing tower operating pressure is calculated as 1.5~2.5MPa, tower top with gauge pressure
Operation temperature is 40~65 DEG C, and tower reactor operation temperature is 40~65 DEG C, and theoretical cam curve is 10~80.
In above-mentioned technical proposal, it is preferable that the operating pressure of the flash tank is calculated as 0.5~1.5MPa with gauge pressure, operation
Temperature is 90~110 DEG C.
6th, the device of expoxy propane is produced according to claim 1, it is characterised in that the first side-stream weight
It is the 0.05~0.5 of the side-stream weight.
In above-mentioned technical proposal, it is preferable that triple component streams enter back into described low after being cooled to 10~50 DEG C
Press propylene recovery column overhead first layer tower tray.
In above-mentioned technical proposal, it is preferable that described device is also containing including compressor, to by the 4th light component stream
The high pressure propylene recovery tower tower reactor is entered back into after supercharging；The suction port of compressor and the 4th light component stream pipeline phase
Even, outlet is connected with the high pressure propylene recovery tower tower reactor.
In above-mentioned technical proposal, it is preferable that the 4th light component stream is cooled to 10~40 DEG C of progress gas-liquid phase separations,
Gas phase enters back into compressor；The compression ratio of the compressor is 8~25, and outlet pressure is calculated as 1.5~2.5MPa with gauge pressure, outlet
Temperature is 10~120 DEG C.
In the present invention, the epoxidation reaction in the reactor of cumyl hydroperoxide and propylene is to be known in the art
's.Usually, reaction temperature is 40~120 DEG C, and reaction pressure is 3.5~6.8MPa, and propylene/CHP mol ratios are 5~20, CHP
Air speed is 0.2~1.2 hour -1.Catalyst used can be the SiO 2 molecular sieve catalyst of titaniferous.
In the inventive solutions, most of propylene in raw material is recycled through high pressure propylene recovery tower, and only 5
~10% propylene obtains in depropanizing tower tower top.The propylene of high pressure propylene recovery tower recovery is not from overhead extraction, but is adopted
It is for the CO/CO of elimination reaction generation with the scheme of side take-off2The light components such as the ethane that impurity and propylene feedstocks are brought into, keep away
Exempt from CO/CO2Enter reaction system by circulating propylene, improve the purity of circulation propylene.Low pressure propylene recovery tower is dodged using adiabatic
Absorbing liquid of the reaction product liquid phase as gas phase after steaming, avoids the use of cryogenic coolant.De- third is delivered to using a small amount of propylene
Alkane tower removes propane, avoids the accumulation of inert propane impurity that propylene feedstocks bring into system.Using the present invention, both reduced
Energy consumption (prior art is compared, and can reduce energy consumption 80%), the yield (up to 99.9%) of propylene is in turn ensure that, ensure that circulation
The purity requirement (up to 95%) of propylene, the yield (up to 99.9%) of PO products is ensure that, suitable for different propylene feedstocks works
Skill flow, achieve preferable technique effect.
Brief description of the drawings
Fig. 1 is apparatus of the present invention schematic diagram.
I is reactor in Fig. 1, and II is high pressure propylene recovery tower, and III is flash tank, and IV is low pressure propylene recovery tower, and V is
Compressor, VI is depropanizing tower, and 1 is raw material hydrogen peroxide isopropylbenzene, and 2 be fresh propylene pipeline, and 3 be containing propylene and expoxy propane
Liquid phase stream pipeline, 4 be that the first light component stream pipeline (is wherein high pressure propylene recovery column overhead stream, containing CO, CO2, second
Alkane), 5 be that the first heavy constituent logistics pipeline (is wherein high pressure propylene recovery tower tower reactor logistics, containing α, alpha-alpha-dimethyl benzylalcohol, isopropyl
Benzene, expoxy propane and propylene), 6 be high pressure propylene recovery tower side-stream pipeline, and 7 be the first side-stream pipeline, and 8 be second
Side-stream pipeline (being wherein high pressure propylene recovery tower Propylene recovery), 9 be that the second light component stream pipeline (is wherein depropanization
The logistics of column overhead Propylene recovery), 10 be the second heavy constituent logistics pipeline (being wherein depropanizing tower tower reactor propylene oxide stream), and 11 be
Three light component stream pipelines (being wherein flash tank gaseous stream), 12 be that triple component streams pipelines (are wherein flash tank liquid
Phase logistics, containing α, alpha-alpha-dimethyl benzylalcohol, isopropylbenzene, expoxy propane and a small amount of propylene), 13 be the 4th light component stream pipeline (its
In be low pressure propylene recovery column overhead stream), 14 be that quadruple component streams pipeline (is wherein low pressure propylene recovery tower tower reactor thing
Stream, crude propene oxide product, containing α, alpha-alpha-dimethyl benzylalcohol, isopropylbenzene, expoxy propane), 15 be the 4th light component thing after supercharging
Flow tube road.
In Fig. 1, raw material hydrogen peroxide isopropylbenzene reacts generation in reactor I through pipeline 2 through pipeline 1 and fresh propylene and contained
The liquid phase stream of expoxy propane and propylene.The liquid phase stream containing expoxy propane and propylene is sent into high pressure propylene through pipeline 3 and returned
The middle part of tower II is received, after separation, the propylene that tower side line obtains is divided into two parts, and most of propylene sends epoxidation reaction back to through pipeline 8
System I participates in reaction, and fraction propylene is refined through pipeline 7 into depropanizing tower VI, the restructuring lease making pipeline 5 that tower reactor obtains
It is sent into adiabatic flash tank III to be separated, the light component that tower top obtains outside pipeline 4 through arranging.Flash tank III pushes up obtained gas-phase product
The middle part of low pressure propylene recovery tower IV is sent into through pipeline 11, the liquid product that the bottom of flash tank III obtains is used as low pressure propylene through pipeline 12
The absorbing liquid of recovery tower IV is sent into first layer tower tray.The gas-phase propene of the tower top of low pressure propylene recovery tower IV is through pipeline 13 through compressor
The tower reactor of high pressure propylene recovery tower II is sent into through pipeline 15 after V supercharging, the tower reactor of low pressure propylene recovery tower IV obtains the ring without propylene
Ethylene Oxide reaction product goes subsequent separation system through pipeline 14.The tower reactor of depropanizing tower VI will arrange through pipeline 10 outside the propane of removing,
The propylene of the recovered overhead of depropanizing tower VI sends epoxidation reaction system back to through pipeline 9 and participates in reaction.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Embodiment
【Embodiment 1】
As shown in figure 1, by taking 100,000 tons/year of PO devices as an example, raw material hydrogen peroxide isopropylbenzene is through pipeline 1 and fresh propylene
Liquid phase stream of the generation containing expoxy propane and propylene is reacted in reactor I through pipeline 2.The liquid containing expoxy propane and propylene
Phase logistics is sent into the middle part of high pressure propylene recovery tower II through pipeline 3, and after separation, the propylene that tower side line obtains is divided into two parts, big portion
Divide propylene to send epoxidation reaction system I back to through pipeline 8 and participate in reaction, fraction propylene is carried out through pipeline 7 into depropanizing tower VI
Refined, the restructuring lease making pipeline 5 that tower reactor obtains is sent into adiabatic flash tank III and separated, and the light component that tower top obtains is through pipeline 4
Outer row.Flash tank III pushes up obtained gas-phase product and is sent into the middle part of low pressure propylene recovery tower IV through pipeline 11, and the bottom of flash tank III obtains
Liquid product through pipeline 12 as low pressure propylene recovery tower IV absorbing liquid be sent into first layer tower tray.Low pressure propylene recovery tower IV
The gas-phase propene of tower top is sent into the tower reactor of high pressure propylene recovery tower II, low pressure third after the supercharging of compressor V through pipeline 13 through pipeline 15
The tower reactor of alkene recovery tower IV obtains the epoxy propane reaction product without propylene and goes subsequent separation system through pipeline 14.Depropanizing tower VI
Tower reactor will arrange through pipeline 10 outside the propane of removing, and the propylene of the recovered overhead of depropanizing tower VI sends epoxidation reaction system back to through pipeline 9
System participates in reaction.
Wherein, the liquid phase stream containing expoxy propane and propylene in pipeline 3, by weight percentage, α, alpha-alpha-dimethyl benzylalcohol
Content be 26%, the content of isopropylbenzene is 6%, and the content of expoxy propane is 10%, and the content of propylene is 55%, and propane contains
Measure as 3%.
The operating condition of high pressure propylene recovery tower is：Operating pressure is calculated as 2.0MPa with gauge pressure, and tower top operation temperature is 48
DEG C, tower reactor operation temperature is 102 DEG C, and theoretical cam curve is 25 pieces.
The operating condition of low pressure propylene recovery tower is：Operating pressure is calculated as 0.2MPa with gauge pressure, and tower top operation temperature is 24
DEG C, tower reactor operation temperature is 106 DEG C, and theoretical cam curve is 20 pieces.
The operating condition of depropanizing tower is：Operating pressure is calculated as 2.0MPa with gauge pressure, and tower top operation temperature is 51 DEG C, tower reactor
Operation temperature is 56 DEG C, and theoretical cam curve is 50 pieces.
Weight ratio into logistics 5 Yu the most of Propylene recovery logistics 6 of depropanizing tower is 1:13.
The operating condition of flash tank is：Operating pressure is calculated as 0.7MPa with gauge pressure, and operation temperature is 77 DEG C.
The operating condition of compressor is：Compression ratio is 12, and outlet pressure is calculated as 2.1MPa, outlet temperature 124 with gauge pressure
℃。
As a result it is：The ton hour of cooling water 608 that high pressure propylene recovery column overhead takes temperature to be 32 DEG C makees cryogen and carries out third
The condensation recovery of alkene, compressor work 624kw.
The yield of propylene is 99.9%, and the yield for 95%, PO products of Propylene recovery purity is 99.9%.Its mesohigh
Propylene recovery column overhead propylene recovery rate is 92.5%.
【Embodiment 2】
Together【Embodiment 1】, simply raw material and operating condition change.
Liquid phase stream containing expoxy propane and propylene in pipeline 3, by weight percentage, α, the content of alpha-alpha-dimethyl benzylalcohol
For 26%, the content of isopropylbenzene is 21.5%, and the content of expoxy propane is 10.5%, and the content of propylene is 39%, and propane contains
Measure as 2%.
The operating condition of high pressure propylene recovery tower is：Operating pressure is calculated as 1.8MPa with gauge pressure, and tower top operation temperature is 45
DEG C, tower reactor operation temperature is 124 DEG C, and theoretical cam curve is 25 pieces.
The operating condition of low pressure propylene recovery tower is：Operating pressure is calculated as 0.2MPa with gauge pressure, and tower top operation temperature is 30
DEG C, tower reactor operation temperature is 119 DEG C, and theoretical cam curve is 20 pieces.
The operating condition of depropanizing tower is：Operating pressure is calculated as 2.0MPa with gauge pressure, and tower top operation temperature is 51 DEG C, tower reactor
Operation temperature is 57 DEG C, and theoretical cam curve is 50 pieces.
Weight ratio into logistics 7 Yu the most of Propylene recovery logistics 6 of depropanizing tower is 1:9.
The operating condition of flash tank is：Operating pressure is calculated as 0.7MPa with gauge pressure, and operation temperature is 106 DEG C.
The operating condition of compressor is：Compression ratio is 12, and outlet pressure is calculated as 2.1MPa, outlet temperature 124 with gauge pressure
℃。
As a result it is：The ton hour of cooling water 467 that high pressure propylene recovery column overhead takes temperature to be 32 DEG C makees cryogen and carries out third
The condensation recovery of alkene, compressor work 472kw.
The yield of propylene is 99.9%, and the yield for 95%, PO products of Propylene recovery purity is 99.9%.Its mesohigh
Propylene recovery column overhead propylene recovery rate is 92.5%.
【Comparative example 1】
Together【Embodiment 1】Raw material enter a destilling tower, from the distillation unreacted propylene of recovered overhead, tower reactor goes out thick PO
Product.
The operating condition of destilling tower is：Operating pressure is 0.3MPa, and tower top operation temperature is -12 DEG C, tower reactor operation temperature
For 120 DEG C, theoretical cam curve is 30 pieces.
As a result it is：Tower top uses temperature as -20 DEG C of the ton hour of cryogen 92.5.
Claims (9)
1. a kind of device for producing expoxy propane, including：
Reactor, for the liquid phase stream containing expoxy propane and propylene by raw material hydrogen peroxide isopropylbenzene and propylene reaction generation；
The reactor inlet is connected with cumyl hydroperoxide pipeline and Propylene pipes, the reactor outlet and the liquid phase stream
Pipeline is connected；
High pressure propylene recovery tower, for being separated to the liquid phase stream containing expoxy propane and propylene, so as to be obtained in tower top
To the first light component stream, the first heavy constituent logistics is obtained in tower reactor, side line obtains side-stream in the middle part of tower；The side-stream
It is divided into the first side-stream and the second side-stream；The entrance of the high pressure propylene recovery tower and the liquid phase stream pipeline phase
Even, 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, tower middle part and
Side-stream pipeline is connected, and the side-stream pipeline communicates with the first side-stream pipeline and the second side-stream pipeline；
Depropanizing tower, for receiving the first side-stream from the high pressure propylene recovery tower side line and it being separated,
So as to obtain the second light component stream in tower top, obtain the second heavy constituent logistics containing propane in tower reactor and discharge it；It is described
The entrance of 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 goes out
Mouth is connected with the second heavy constituent logistics pipeline；
Flash tank, for receiving the first heavy constituent logistics from the high pressure propylene recovery tower tower reactor and it being separated,
So as to obtain the 3rd light component stream in tank deck, triple component streams are obtained in tank bottom；The entrance of the flash tank with it is described
First heavy constituent logistics pipeline is connected, and roof door is connected with the 3rd light component stream pipeline, tank bottom outlet and the 3rd heavy constituent
Logistics pipeline is connected；
Low pressure propylene recovery tower, for receiving from the 3rd light component stream of the flash tank and triple component streams,
Tower top obtains the 4th light component stream, obtains the quadruple component streams containing expoxy propane in tower reactor and will be arranged outside it；It is described low
Pressure propylene recovery tower centre entrance is connected with the 3rd light component stream pipeline, tower top the first tower tray entrance and triple component streams
Pipeline is connected, and tower top outlet is connected with the 4th light component stream pipeline, and tower reactor outlet is connected with quadruple component streams pipeline；
The second side-stream pipeline and the second light component stream pipeline, are all communicated with the Propylene pipes.
2. the device of expoxy propane is produced according to claim 1, it is characterised in that the operation of the high pressure propylene recovery tower
Pressure is calculated as 1.5~2.5MPa with gauge pressure, and the operating pressure of the low pressure propylene recovery tower is calculated as 0.01~0.2MPa with gauge pressure.
3. the device of expoxy propane is produced according to claim 1, it is characterised in that the raw material hydrogen peroxide isopropylbenzene is
Obtained by cumene oxidation, be the mixture of cumyl hydroperoxide and isopropylbenzene；In the mixture, hydrogen peroxide isopropyl
The weight percent concentration of benzene is 20~80%.
4. the device of expoxy propane is produced according to claim 1, it is characterised in that the liquid containing propylene and expoxy propane
In phase logistics, by weight percentage, α, the content of alpha-alpha-dimethyl benzylalcohol is 19~50%, the content of isopropylbenzene for 10~
70%, the content of expoxy propane is 5~20%, and the content of propylene is 5~60%, and the content of propane is 0~10%.
5. the device of expoxy propane is produced according to claim 1, it is characterised in that the tower of the high pressure propylene recovery tower
It is 5~80 DEG C to push up operation temperature, and tower reactor operation temperature is 45~120 DEG C, and theoretical cam curve is 10~50；
The tower top operation temperature of the low pressure propylene recovery tower is 10~50 DEG C, and tower reactor operation temperature is 70~120 DEG C, theoretical tower
Plate number is 10~50；
The depropanizing tower operating pressure is calculated as 1.5~2.5MPa with gauge pressure, and tower top operation temperature is 40~65 DEG C, tower reactor operation
Temperature is 40~65 DEG C, and theoretical cam curve is 10~80；
The operating pressure of the flash tank is calculated as 0.5~1.5MPa with gauge pressure, and operation temperature is 90~110 DEG C.
6. the device of expoxy propane is produced according to claim 1, it is characterised in that the first side-stream weight is institute
State the 0.05~0.5 of side-stream weight.
7. the device of expoxy propane is produced according to claim 1, it is characterised in that triple component streams are cooled to
The low pressure propylene recovery column overhead first layer tower tray is entered back into after 10~50 DEG C.
8. the device of expoxy propane is produced according to claim 1, it is characterised in that described device also containing compressor is included, is used
So that the high pressure propylene recovery tower tower reactor will be entered back into after the 4th light component stream supercharging；The suction port of compressor with it is described
4th light component stream pipeline is connected, and outlet is connected with the high pressure propylene recovery tower tower reactor.
9. the device of expoxy propane is produced according to claim 8, it is characterised in that the 4th light component stream is cooled to
10~40 DEG C of progress gas-liquid phase separations, gas phase enter back into compressor；The compression ratio of the compressor be 8~25, outlet pressure with
Gauge pressure is calculated as 1.5~2.5MPa, and outlet temperature is 10~120 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410354596.5A CN105294604B (en) | 2014-07-24 | 2014-07-24 | Produce the device of expoxy propane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410354596.5A CN105294604B (en) | 2014-07-24 | 2014-07-24 | Produce the device of expoxy propane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105294604A CN105294604A (en) | 2016-02-03 |
| CN105294604B true CN105294604B (en) | 2017-12-15 |
Family
ID=55192520
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410354596.5A Active CN105294604B (en) | 2014-07-24 | 2014-07-24 | Produce the device of expoxy propane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105294604B (en) |
Families Citing this family (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 |
| 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 |
| PT3719008T (en) | 2017-11-30 | 2023-03-23 | China Petroleum & Chem Corp | Alkylene oxide production method and production system |
| 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 |
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 |
|---|
| CHP法生产CA 和PO的分离模拟与研究;李文忠;《中国优秀硕士学位论文工程科技1辑》;20090430;B016-98 * |
| 用异丙苯过氧化氢作氧化剂合成环氧丙烷的新技术;于剑昆等;《化学推进剂与高分子材料》;20070531;第5卷(第5期);1-8 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105294604A (en) | 2016-02-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105272941B (en) | The production method of propylene oxide | |
| CN105294604B (en) | Produce the device of expoxy propane | |
| CN105503492B (en) | A kind of MTP devices and its new separating technology | |
| TWI660942B (en) | Method and device for recovering refined propylene | |
| CN110467595A (en) | A kind of no sulfuric acid process metaformaldehyde synthesizer and its synthesis route | |
| CN105980338B (en) | By the method for the raw material production 1,3-butadiene comprising ethyl alcohol | |
| CN111847453B (en) | Device and process for preparing ultra-pure carbon monoxide | |
| CN104292066A (en) | Preparation method for high purity isobutylene | |
| CN114702375B (en) | Separation system and method for acetaldehyde product prepared from ethanol | |
| CN104557478A (en) | Method for preparing tert-butyl ether | |
| CN105315234B (en) | The method for producing expoxy propane | |
| CN105439792B (en) | The method of the refined propylene of recovery | |
| CN105315238B (en) | The production equipment of expoxy propane | |
| CN105272808B (en) | The equipment of propylene recovery | |
| CN105330504B (en) | Reclaim the device of refined propylene | |
| CN103772174B (en) | The method that acetone is prepared in aqueous isopropanol low-temperature gaseous phase dehydrogenation | |
| CN105272806B (en) | The method of propylene recovery | |
| CN205740823U (en) | A kind of MTP device | |
| CN105585468B (en) | A method of cyclopentanone is prepared by raw material of cyclopentene | |
| CN107285977A (en) | A kind of system and device that normal butane is prepared by the positive structure of iso-butane | |
| CN102489220B (en) | Continuous oxidation method and device for preparing oxalic acid | |
| CN105272939A (en) | Epoxy propane production method | |
| CN109134175B (en) | Process and device for preparing high-purity isobutene through MTBE pyrolysis | |
| CN109701360B (en) | Device and method for removing and utilizing carbon dioxide in low-carbon olefin and acetic acid co-oxidation product gas | |
| CN105294379B (en) | Propylene recovery equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |