CN208803004U - Energy integrated-type propylene separation recyclable device in epoxidation technique - Google Patents
Energy integrated-type propylene separation recyclable device in epoxidation technique Download PDFInfo
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- CN208803004U CN208803004U CN201821264474.7U CN201821264474U CN208803004U CN 208803004 U CN208803004 U CN 208803004U CN 201821264474 U CN201821264474 U CN 201821264474U CN 208803004 U CN208803004 U CN 208803004U
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Abstract
The utility model provides energy integrated-type propylene separation recyclable device in epoxidation technique, the reaction under high pressure product of reaction member epoxidation reaction sequentially enters High Pressure Flash Unit, middle pressure processing unit, low-pressure flash in the device, the Rich propylene body operated under lower pressure enter injector pressed in processing gas phase injection pressurization after, the rich propylene gaseous mixture of formation enters high pressure compressor and is further compressed, and is subsequently sent to propylene separation refined unit and carries out propylene separation purification.The significant advantage that the propylene separation recyclable device of the utility model has energy consumption small can reduce the unit cost of production of product, improve product competitiveness, and product yield can be improved.
Description
Technical field
The utility model relates to a kind of from epoxidation product recycles the device of alkene, more specifically, the utility model
It is related to a kind of energy integrated-type separator for excessive propene separation and recovery in epoxidation of propylene production propylene oxide process.
Background technique
Propylene oxide is important Organic Chemicals, is that the third-largest propylene at present in addition to polypropylene and acrylonitrile spreads out
Biology.Its maximum purposes is synthesizing polyether glycol, and then manufactures polyurethane, in the distribution of the purposes in the U.S. and West Europe, this side
The purposes in face accounts for 60% and 70% or more respectively.Propylene oxide can also be used to manufacture nonionic surfactant and propenyl, third
Glycol, alcohol ether, propene carbonate, poly- Propanolamine, propionic aldehyde, synthetic glycerine, organic acid, synthetic resin, foamed plastics, plasticizer,
Emulsifier, wetting agent, detergent, fungicide, fumigant etc..Fine chemicals derived from propylene oxide is almost applied to all works
In industry department and daily life.
The production technology of propylene oxide mainly has chlorohydrination, conjugated oxidation (PO/SM method, P0/TAB method), isopropylbenzene direct
Oxidizing process (CHP method), hydrogen peroxide direct oxidation method and oxygen direct oxidation method.Wherein the major defect of chlorohydrination is that have to equipment
Corrode, it is very big to generate the largely waste water containing organic chloride, waste residue, environmental protection pressure in production process.Conjugated oxidation is compared
Chlorohydrination reduces environmental protection pressure, but its long flow path, investment height, joint product yield are high, and economic benefit is restricted very by joint product
Obviously.Several direct oxidation methods are that propylene and oxidant single step reaction are obtained ring under the catalytic action of special catalyst
The process of Ethylene Oxide.This mild reaction condition, product yield is high, and without other joint product, the three wastes are few, substantially without dirt
Dye, belongs to environmental-friendly process for cleanly preparing, which represent the developing direction of Synthesis of Propylene Oxide.
In various direct oxidation method Synthesis of Propylene Oxide, for the complete conversion for ensuring oxidant, in reaction process
Propylene feed is maintained and is higher than chemical reaction metering ratio, this part excessive propene is needed in subsequent separation process through separation essence
Again reactor is sent after system back to be reacted.Its energy consumption during separating and recovering is the important finger of device competitiveness
Mark.And during propylene separation recycling, often also along with the generation of the side reactions such as hydrolysis, and then lead to product yield
It reduces.
Patent CN201110434173 discloses a kind of process for separation and purification from the epoxidation product comprising propylene oxide.
The patent strips reaction product under low pressure or rectifying, isolates and passes through compressor compresses again containing propylene gas and enter subsequent processing
System.The shortcomings that scheme that the patent is announced, is, after low-pressure gas or rectifying, the mistake of atmospheric pressure containing propylene isolated
It is low, cause compressor assembly pressure ratio big, energy consumption is high.
Summary of the invention
In view of this, the utility model is directed to energy integrated-type propylene separation recyclable device in epoxidation technique, it should
Kind device has the advantages such as process is simple, separating energy consumption is low compared with the device of the existing Propylene recovery from epoxidation product,
Product yield can be improved, and the unit cost of production of product can be reduced, improve product competitiveness.
In order to achieve the above objectives, the technical solution of the utility model is achieved in that
Energy integrated-type propylene separation recyclable device in epoxidation technique, including reaction member, the preheating list being sequentially communicated
Member, flash vessel, middle pressure processing unit, low-pressure flash, crude separation unit and product purification unit, the flash vessel and No. 1
The connection of fractional distilling tube entrance, medium pressure processing unit are connected to injector first entrance, the low-pressure flash, rough segmentation
It is connected to injector second entrance from unit, the injector is connected to high pressure compressor entrance, No. 1 fractional distilling tube
Outlet, high-pressure compressor outlet are connected to propylene separation refined unit, and the propylene separation refined unit exports and reacts single
Member connection.
When above-mentioned propylene separation recyclable device works, high pressure sudden strain of a muscle is carried out under high pressure to reaction under high pressure product first
It steams, a part of propylene therein is first subjected to separating-purifying, obtains high pressure richness propylene, is avoided after reducing pressure again by propylene weight
The process of new compression and back high pressure, saves a part of energy consumption；And high pressure flash raffinate next carry out in pressure processing and low pressure
Flash distillation etc. operates, and pressure Rich propylene body in a part is isolated in pressure processing again in one side, reduces and needs to increase step by step from low pressure
It is pressed onto the amount of the gas of high pressure, reduces energy consumption, pressure processing gas phase injection is from low pressure flash and crude separation in another aspect
Low pressure Rich propylene body is pressurized low pressure Rich propylene body, forms the rich propylene that pressure is much larger than low pressure Rich propylene body
The rich propylene mixed pressure of mesolow need to be only reduced to high pressure by gaseous mixture, high pressure compressor, compared to more directly by gas by low pressure
It is compressed to high pressure, reduces the energy level difference before and after gas compression, and then is substantially reduced the energy consumption of compressor, while being avoided between grade
The application of feed type compressor reduces flow operations complexity.
Further, medium pressure processing unit is evaporator.
Further, medium pressure processing unit is flash vessel.
Further, the access of medium pressure processing unit and injector is equipped with No. 2 fractional distilling tubes.It is cold using part
Condenser centering pressure processing gas phase carries out partial condensation, and further the heavy constituent in removing in pressure processing gas phase, realizes middle pressure third
The further purification of alkene gas reduces the amount into the gas of injector, further reduces high pressure compressor and needs to compress
Gas amount, reduce the energy consumption of high pressure compressor, thereby reduce the energy consumption of overall flow.
Further, the access of the low-pressure flash and injector is equipped with No. 3 fractional distilling tubes.It is cold using part
Condenser presses evaporation gas phase to carry out partial condensation low pressure, further removes the heavy constituent in low pressure flash gas phase, realizes low pressure
The further purification of propylene gas reduces the amount into the gas of injector, and then reduces high pressure compressor and need to compress
Gas amount, reduce the energy consumption of high pressure compressor, thereby reduce the energy consumption of overall flow.
Further, the flash vessel is equipped with inert gas air inlet.It is logical to the liquid phase bottom of flash vessel when high pressure flash
Entering inert gas can be improved flash evaporation effect and process safety.
Further, internals are added with inside the flash vessel, the internals of addition include column plate, filler.Add in flash vessel
Add the internals such as column plate, filler that can optimize mass-transfer performance.
Compared with the existing technology, energy integrated-type propylene separation recycling dress in epoxidation technique described in the utility model
It sets, it is advantageous that:
The device of the utility model makes propylene by the way that reaction under high pressure product is carried out multi-layer processing in high, medium and low pressure
It is separated from reaction product under higher pressure condition as far as possible, and by the combination of injector and high pressure compressor to richness
Propylene gas carries out classification pressurization, and the energy grade before and after reduction gas compression is poor, final energy consumption can be greatly reduced, especially
It is the energy consumption of compressor, and then reduces the unit cost of product, improves product competitiveness.
In addition, reaction under high pressure product carries out preheating first and increases when the propylene separation recyclable device work of the utility model
Press flashing operation, the relatively existing method that propylene recovery is carried out by rectifying, without reflux course, when heat treatment required temperature
Spend relatively low, the processing of middle pressure thereafter and low pressure flash process required temperature are then successively lower, i.e. the propylene of the utility model
Recyclable device reduces the separation temperature in propylene separation removal process, effectively reduces in reaction product oxyalkylene in high temperature
Residence time under alcohol-containing aqueous environment can reduce the generation of the side reactions such as hydrolysis, and then improve the product of overall craft process
Yield.
Detailed description of the invention
The attached drawing for constituting a part of the utility model is used to provide a further understanding of the present invention, this is practical new
The illustrative embodiments and their description of type are not constituteed improper limits to the present invention for explaining the utility model.?
In attached drawing:
Fig. 1 is energy integrated-type propylene separation recyclable device figure in epoxidation technique described in the utility model embodiment 1；
Fig. 2 is energy integrated-type propylene separation recyclable device figure in epoxidation technique described in the utility model embodiment 2.
Description of symbols:
1- reaction under high pressure product；2- preheated reaction product；3- inert gas；4- high pressure flash gas phase；5- high pressure is dodged
Steam raffinate；6- high pressure flash lime set；7- high pressure flash fixed gas；Pressure processing gas phase in 8-；Pressure processing raffinate in 9-；10- low pressure
Flash gas phase；11- low pressure flash raffinate；12- crude separation Rich propylene；13- crude separation liquid phase；14- richness propylene gaseous mixture；15-
High-pressure compressor outlet gas；16- recycles propylene；Pressure processing lime set in 17-；Pressure processing fixed gas in 18-；19- low pressure flash is solidifying
Liquid；20- low pressure flash fixed gas；
A- reaction member；B- preheating unit；C- flash vessel；Processing unit is pressed in d-；E- low-pressure flash；F- crude separation
Unit；G- product purification unit；H-- injector；I- high pressure compressor；J- propylene separation refined unit；K-2 partial condensation
Device；M-3 fractional distilling tube；N-1 fractional distilling tube.
Specific embodiment
The utility model is described in detail below in conjunction with embodiment.
Embodiment 1:
As shown in Figure 1, energy integrated-type propylene separation recyclable device in epoxidation technique, including the reaction list being sequentially communicated
First a, preheating unit b, flash vessel c, middle pressure processing unit d, low-pressure flash e, crude separation unit f and product purification unit g,
Flash vessel c is connected to No. 1 fractional distilling tube n entrance, and middle pressure processing unit d is connected to injector h first entrance, low pressure flash list
First e, crude separation unit f are connected to injector h second entrance, and injector h is connected to high pressure compressor i entrance, and No. 1 part is cold
Condenser n outlet, high pressure compressor i outlet be connected to propylene separation refined unit j, propylene separation refined unit j outlet with instead
Unit a is answered to be connected to.Middle pressure processing unit d is evaporator.Flash vessel c is equipped with inert gas air inlet, and addition inside flash vessel c
There are internals, the internals of addition include column plate, filler.
When carrying out propylene separation recycling using above-mentioned apparatus, firstly, carrying out epoxidation reaction in reaction member a, reaction exists
It is carried out under high pressure, operating pressure 2.7MPaG；The reaction under high pressure product 1 that epoxidation reaction obtains is sent to preheating unit b and carries out in advance
Heat, preheated reaction product 2 enter flash vessel c and carry out high pressure flash, and 65 DEG C of preheating temperature, to the liquid of flash vessel c when flash distillation
Phase bottom is passed through one inert gas 3, finally obtains high pressure flash gas phase 4 and high pressure flash raffinate 5, and high pressure flash gas phase 4 is logical
After crossing No. 1 fractional distilling tube n progress partial condensation, high pressure flash lime set 6 and high pressure flash fixed gas 7 are obtained, high pressure flash is solidifying
Liquid 6 send to propylene separation refined unit j the further separation and purification operation for carrying out propylene, 7 discharge system of high pressure flash fixed gas.
High pressure flash raffinate 5 enters middle pressure processing unit d, further evaporates under the conditions of middle pressure, evaporating pressure
0.7MPaG, obtains middle pressure processing gas phase 8 and middle pressure processing raffinate 9 by 53 DEG C of evaporating temperature, and middle pressure processing gas phase 8 is sent to injector
h.Middle pressure processing raffinate 9 enters low-pressure flash e, flashes under low pressure, obtains low pressure flash gas phase 10 and low pressure flash
Raffinate 11, flashing pressure 0.1MPaG, low pressure flash raffinate 11 enter crude separation unit f, through crude separation step, i.e. rectifying, vapour
Mention and etc., crude separation Rich propylene 12 and crude separation liquid phase 13 are obtained, crude separation liquid phase 13 is sent to product purification unit g and carried out
The separation and purification operation of product, byproduct.The low pressure flash gas phase 10 and crude separation unit f that low-pressure flash e is generated generate
Crude separation Rich propylene 12 send to injector h, rich propylene gaseous mixture 14 is formed after pressure processing 8 injection of gas phase in, is obtained
Rich propylene gaseous mixture 14 be subsequently sent to high pressure compressor i, 2.3MPaG is compressed to by high pressure compressor i, obtained high pressure compressed
Machine, which is worked off one's feeling vent one's spleen, 15 is subsequently sent to propylene separation refined unit j.The circulation propylene obtained through propylene separation refined unit j separating-purifying
16 are sent to reaction member a.
Form evaporator used by evaporation element at different levels can be selected Kettel formula, falling film type, rise membrane type in aforesaid operations
Equal multiple types, the using effect of the utility model do not limit to the selection of form evaporator；Propylene separation refined unit j is optional
With a variety of separating-purifying modes such as conventional rectification, thermal coupling rectifying, absorption and desorption, the content of the present invention is not intended to limit propylene point
Concrete form from refined unit j.
Epoxidation product is separated and recovered using process flow shown in embodiment 1, compressor and overall energy consumption are saved
18%.
Embodiment 2:
As shown in Fig. 2, energy integrated-type propylene separation recyclable device in epoxidation technique, including the reaction list being sequentially communicated
First a, preheating unit b, flash vessel c, middle pressure processing unit d, low-pressure flash e, crude separation unit f and product purification unit g,
Flash vessel c is connected to No. 1 fractional distilling tube n entrance, and middle pressure processing unit d is connected to injector h first entrance, low pressure flash list
First e, crude separation unit f are connected to injector h second entrance, and injector h is connected to high pressure compressor i entrance, and No. 1 part is cold
Condenser n outlet, high pressure compressor i outlet be connected to propylene separation refined unit j, propylene separation refined unit j outlet with instead
Unit a is answered to be connected to.Flash vessel c is equipped with inert gas air inlet, and middle pressure processing unit d is flash vessel.Middle pressure processing unit d and spray
The access of emitter h is equipped with No. 3 partial condensations equipped with the access of No. 2 fractional distilling tube k, low-pressure flash e and injector h
Device m.
When carrying out propylene separation recycling using above-mentioned apparatus, firstly, carrying out epoxidation reaction in reaction member a, reaction exists
It is carried out under high pressure, operating pressure 2.7MPaG；The reaction under high pressure product 1 that epoxidation reaction obtains is sent to preheating unit b and carries out in advance
Heat, preheated reaction product 2 enter flash vessel c and carry out high pressure flash, and 65 DEG C of preheating temperature, to the liquid of flash vessel c when flash distillation
Phase bottom is passed through one inert gas 3, finally obtains high pressure flash gas phase 4 and high pressure flash raffinate 5, and high pressure flash gas phase 4 is logical
After crossing No. 1 fractional distilling tube n progress partial condensation, high pressure flash lime set 6 and high pressure flash fixed gas 7 are obtained, high pressure flash is solidifying
Liquid 6 send to propylene separation refined unit j the further separation and purification operation for carrying out propylene, 7 discharge system of high pressure flash fixed gas.
High pressure flash raffinate 5 enters middle pressure processing unit d, further flashes under the conditions of middle pressure, flashing pressure
0.7MPaG obtains middle pressure processing gas phase 8 and middle pressure processing raffinate 9, and middle pressure processing gas phase 8 is through No. 2 fractional distilling tube k carry out portions
Middle pressure processing fixed gas 18 and middle pressure processing lime set 17 are obtained after dividing condensation, middle pressure processing fixed gas 18 is sent to injector h, middle pressure
Processing lime set 17 returns to middle pressure processing unit d.Middle pressure processing raffinate 9 enters low-pressure flash e, flashes, obtains under low pressure
To low pressure flash gas phase 10 and low pressure flash raffinate 11, flashing pressure 0.1MPaG, low pressure flash gas phase 10 is through No. 3 partial condensations
Device m obtains low pressure flash fixed gas 20 and low pressure flash lime set 19 after carrying out partial condensation, and low pressure flash fixed gas 20 is sent to spray
Emitter h, low pressure flash lime set 19 return to low-pressure flash.Low pressure flash raffinate 11 enters crude separation unit f, through crude separation
Step, i.e. rectifying, stripping and etc., obtain crude separation Rich propylene 12 and crude separation liquid phase 13, crude separation liquid phase 13 is sent to production
Product refined unit g carries out the separation and purification operation of product, byproduct.Low pressure flash fixed gas 20 from low-pressure flash e
It send with the crude separation Rich propylene 12 from crude separation unit f to injector h, is formed after pressure processing 18 injection of fixed gas in
Rich propylene gaseous mixture 14, obtained rich propylene gaseous mixture 14 are subsequently sent to high pressure compressor i, are compressed to by high pressure compressor i
2.3MPaG, obtained high-pressure compressor outlet gas 15 are subsequently sent to propylene separation refined unit j.Through propylene separation refined unit j
The circulation propylene 16 that separating-purifying obtains is sent to reaction member a.
Form evaporator used by evaporation element at different levels can be selected Kettel formula, falling film type, rise membrane type in aforesaid operations
Equal multiple types, the using effect of the utility model do not limit to the selection of form evaporator；Propylene separation refined unit j is optional
With a variety of separating-purifying modes such as conventional rectification, thermal coupling rectifying, absorption and desorption, the content of the present invention is not intended to limit propylene point
Concrete form from refined unit j.
Epoxidation product is separated and recovered using process flow shown in embodiment 2, compressor and overall energy consumption are saved
20%.
The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this
Within the spirit and principle of utility model, any modification, equivalent replacement, improvement and so on should be included in the utility model
Protection scope within.
Claims (7)
1. energy integrated-type propylene separation recyclable device in epoxidation technique, it is characterised in that: including the reaction list being sequentially communicated
First (a), preheating unit (b), flash vessel (c), middle pressure processing unit (d), low-pressure flash (e), crude separation unit (f) and production
Product refined unit (g), the flash vessel (c) are connected to No. 1 fractional distilling tube (n) entrance, medium pressure processing unit (d) and spray
The connection of emitter (h) first entrance, the low-pressure flash (e), crude separation unit (f) connect with injector (h) second entrance
Logical, the injector (h) is connected to high pressure compressor (i) entrance, No. 1 fractional distilling tube (n) outlet, high pressure compressor
(i) outlet is connected to propylene separation refined unit (j), and propylene separation refined unit (j) outlet connects with reaction member (a)
It is logical.
2. energy integrated-type propylene separation recyclable device in epoxidation technique according to claim 1, it is characterised in that: institute
Stating middle pressure processing unit (d) is evaporator.
3. energy integrated-type propylene separation recyclable device in epoxidation technique according to claim 1, it is characterised in that: institute
Stating middle pressure processing unit (d) is flash vessel.
4. energy integrated-type propylene separation recyclable device in epoxidation technique according to claim 1, it is characterised in that: institute
The access for stating pressure processing unit (d) and injector (h) is equipped with No. 2 fractional distilling tubes (k).
5. energy integrated-type propylene separation recyclable device in epoxidation technique according to claim 1, it is characterised in that: institute
The access for stating low-pressure flash (e) and injector (h) is equipped with No. 3 fractional distilling tubes (m).
6. energy integrated-type propylene separation recyclable device in epoxidation technique according to claim 1, it is characterised in that: institute
Flash vessel (c) is stated equipped with inert gas air inlet.
7. energy integrated-type propylene separation recyclable device in epoxidation technique according to claim 1, it is characterised in that: institute
It states added with internals inside flash vessel (c), the internals of addition include column plate, filler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821264474.7U CN208803004U (en) | 2018-08-07 | 2018-08-07 | Energy integrated-type propylene separation recyclable device in epoxidation technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821264474.7U CN208803004U (en) | 2018-08-07 | 2018-08-07 | Energy integrated-type propylene separation recyclable device in epoxidation technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208803004U true CN208803004U (en) | 2019-04-30 |
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ID=66231413
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821264474.7U Active CN208803004U (en) | 2018-08-07 | 2018-08-07 | Energy integrated-type propylene separation recyclable device in epoxidation technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208803004U (en) |
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2018
- 2018-08-07 CN CN201821264474.7U patent/CN208803004U/en active Active
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