CN208414288U - A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide - Google Patents
A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide Download PDFInfo
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- CN208414288U CN208414288U CN201820981487.XU CN201820981487U CN208414288U CN 208414288 U CN208414288 U CN 208414288U CN 201820981487 U CN201820981487 U CN 201820981487U CN 208414288 U CN208414288 U CN 208414288U
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Abstract
The utility model discloses the differential pressure thermocouple propylene refining separation system in a kind of production of propylene oxide, the tower top of depropanizing tower is connected with the first pipeline, and the tower top of depropanizing tower is connected by the tower bottom of compressor and depropenizer.The first reboiler and heat exchanger have been arranged in parallel on 4th pipeline of the tower top of depropenizer, first reboiler and heat exchanger are connect with the import of return tank respectively, the outlet of return tank and the import of reflux pump connect, the outlet of reflux pump is connect with the first valve, the one outlet of first valve and the tower top of depropenizer connect, another outlet is for producing propylene product.The tower bottom of depropanizing tower is arranged in first reboiler, and the tower bottom of depropanizing tower is connect with the bottom and top of the first reboiler respectively.Propylene/propane separation system is related to phase transformation during solving prior art propylene refining workshop section purification propylene, leads to the problem that energy consumption is high.The propylene/propane separation system of the utility model is not related to phase transition process, and process operation cost significantly reduces.
Description
Technical field
The utility model relates to the differential pressure heats in Producing Process of Propylene Oxide field more particularly to a kind of production of propylene oxide
Even propylene refining separation system.
Background technique
The propane generated in crude refinement processes is primarily present in liquefied petroleum gas, for a long time, liquefied petroleum gas quilt
It is bound by fuel area, it is not high to show as serious waste of resources, added value.
Propylene oxide can be used as the raw material of production polyurethane, and market has openings is larger, produce ring by raw material of liquefied petroleum gas
Ethylene Oxide can widen petrochemical industry chain, improve refinery Project Economy Benefit and market competitiveness of enterprises.
As follows as the process program of raw material production propylene oxide using liquefied petroleum gas: firstly, dehydrogenating propane workshop section, liquefy stone
For oil gas in fixed bed reactors, control reaction temperature is 650 DEG C, and dehydrogenation reaction is carried out under the action of Gr-Al catalyst and is turned
Turn to propylene；The crude product of generation enters deep cooling workshop section, multiple repeatedly to freeze, and crude product is compressed to -95 DEG C, enters propylene after 1MPa
Refinement purifies propylene using differential pressure thermocouple refining system, and propylene, the methanol-water of purification carry TS-1 catalyst and equal three
Toluene carrying hydrofenating anthraquinone enters slurry bed reactor and sufficiently reacts generation propylene oxide (PO) and byproduct, by separation work
Section, product coarse centrifugal station, product purification workshop section, by-product processing section and regenerative section, organic phase weight after dry activation
It is utilized again, the propylene oxide and byproduct propylene glycol monomethyl ether of acquisition are for sale as product.
In traditional production technology, propane obtains crude propylene product through dehydrogenation section, and crude propylene product is cold in deep cooling workshop section
But to phase transformation, condition needed for reaching propylene refining workshop section, because propylene and propane boiling point are closer to, using common treating column
(its tower top is equipped with condenser, and tower reactor is equipped with reboiler) separation is related to the mixed system of phase transformation, and process condition is harsh, tower top
Condenser and tower reactor reboiler meet the normal operating of process system to consume a large amount of public work medium as cost.Significantly
The investment of the operating cost and equipment for increasing system, maintenance cost, be unfavorable for efficiently, production energy-saving.
For above-mentioned technological problems, how to be optimized in production of propylene oxide by the change of process technology scheme
Propylene refining separation system, the problem of becoming urgent need to resolve.
Utility model content
The purpose of this utility model is to provide the differential pressure thermocouple propylene refining separation system in a kind of production of propylene oxide,
Propylene/propane separation system is related to phase transformation during solving prior art propylene refining workshop section purification propylene, leads to energy consumption height
The problem of.The propylene/propane separation system of the utility model is not related to phase transition process, and process operation cost significantly reduces.
In order to achieve the above objectives, the utility model adopts the following technical solution:
The utility model provides the differential pressure thermocouple propylene refining separation system in a kind of production of propylene oxide, including de- third
Alkane tower, compressor, depropenizer, return tank, reflux pump and the first valve；
The tower top of depropanizing tower is connected with the first pipeline, and depropanizing tower is passed through mixture to be separated by the first pipeline；It is de-
The tower top of propane tower also passes through the second pipeline and the air inlet of compressor connects, and the gas outlet of compressor by third pipeline and takes off
The tower bottom of propylene tower connects；
The tower top of depropenizer is connected with the 4th pipeline, has been arranged in parallel the first reboiler and heat exchanger on the 4th pipeline,
First reboiler and heat exchanger are connect with the import of return tank respectively, and the outlet of return tank and the import of reflux pump connect, reflux
The outlet of pump is connect with the first valve, and the one outlet of the first valve is connected by the tower top of the 5th pipeline and depropenizer, the
Another outlet of one valve is for producing propylene product；
First reboiler is arranged in the tower bottom of depropanizing tower, the tower bottom of depropanizing tower respectively with the bottom of the first reboiler and
Top connection.
Further, the utility model is also characterized by:
The second valve is provided on 4th pipeline, the one outlet of the second valve is connect with the first reboiler；Second valve
Another outlet be connected with third valve, third valve is connect with heat exchanger, and heat exchanger is connect with return tank；First reboiler
It is connect respectively with third valve and return tank.
First valve and the second valve are triple valve.
Further include the second reboiler, the second reboiler is arranged in the tower bottom of depropanizing tower, the tower bottom of depropanizing tower respectively with
The bottom and top of second reboiler connect.
The tower bottom of depropanizing tower is connected with the 6th pipeline, and the 6th pipeline is equipped with column bottoms pump, and the 6th pipeline is de- for producing
Propylene mixtures.
Depropenizer tower bottom is connect through pipeline with the depropanizing tower tower top.
Compared with prior art, the utility model has technical effect beneficial below:
Differential pressure thermocouple propylene refining separation system in a kind of production of propylene oxide provided by the utility model, by will be former
The stripping section of propylene refining tower becomes depropanizing tower, former rectifying section is become depropenizer, and by depropanizing tower and de- third
Compressor is added between alkene tower, operation pressure difference is larger between efficiently solving two tower of depropanizing tower and depropenizer, realizes two towers
Differential pressure thermocouple separates propylene/propane mixture, is not related to phase transition process.Propylene/propane mixture to be separated enters depropanizing tower
Tower top is sent after the group lease making compressor boosting of depropanizing tower overhead extraction to depropenizer tower bottom, depropenizer overhead extraction
Heat transferring medium of the light component as heat exchanger and the first reboiler of depropanizing tower tower reactor, the light component for completing heat recovery are cold
But it after, send to return tank, is then sent after reflux pump boosts to depropenizer tower top, realize and flow stock heating efficiency in tower
Maximization.The utility model is novel in design rationally, and process operation cost significantly reduces, and technological operation efficiency significantly improves, and accords with
Close energy conservation type industrial development requirement.
Detailed description of the invention
Fig. 1 is that the structure of the differential pressure thermocouple propylene refining separation system in production of propylene oxide provided by the utility model is shown
It is intended to.
In figure: 1, depropanizing tower；2, the first reboiler；3, column bottoms pump；4, the second reboiler；5, the second valve；6, third
Valve；7, heat exchanger；8, return tank；9, compressor；10, depropenizer；11, reflux pump；12, the first valve.
Specific embodiment
The utility model is described in further detail with reference to the accompanying drawing:
Referring to Fig. 1, the utility model provides the differential pressure thermocouple propylene refining separation system in a kind of production of propylene oxide,
Including depropanizing tower 1, compressor 9, depropenizer 10, return tank 8, reflux pump 11 and the first valve 12.The tower of depropanizing tower 1
Top is connected with the first pipeline, and depropanizing tower 1 is passed through mixture to be separated by the first pipeline；The tower top of depropanizing tower 1 also passes through
Second pipeline is connect with the air inlet of compressor 9, and the gas outlet of compressor 9 is connected by the tower bottom of third pipeline and depropenizer 10
It connects.The tower top of depropenizer 10 is connected with the 4th pipeline, and the first reboiler 2 and heat exchanger 7 have been arranged in parallel on the 4th pipeline, the
One reboiler 2 and heat exchanger 7 are connect with the import of return tank 8 respectively, and the outlet of return tank 8 is connect with the import of reflux pump 11,
The outlet of reflux pump 11 is connect with the first valve 12, and the one outlet of the first valve 12 passes through the 5th pipeline and depropenizer 10
Tower top connection；Another outlet of first valve 12 is connect through pipeline with propylene product intermediate storage tank, for producing propylene product；
First reboiler 2 is arranged in the tower bottom of depropanizing tower 1, the tower bottom of depropanizing tower 1 bottom and top with the first reboiler 2 respectively
Connection.
Herein, the light component of 1 tower top of depropanizing tower is sent through third pipeline to de- third after compressor 9 boosts to 2.0MPa
The tower bottom of alkene tower 10.At 20.3 DEG C~22.8 DEG C, the bottom temperature of depropanizing tower 1 is controlled for the tower top temperature control of depropanizing tower 1
At 25.5 DEG C~27.5 DEG C, the tower top temperature control of depropenizer 10 is at 51.5 DEG C~54.6 DEG C, the tower reactor temperature of depropenizer 10
Degree control is at 22.1 DEG C~23.7 DEG C.
The utility model eliminates in traditional separation system and maintains overhead condenser and tower reactor reboiler using public work
Required energy consumption, the first reboiler by 10 overhead extraction light component of depropenizer as 1 tower reactor of heat exchanger 7 and depropanizing tower
2 heat transferring medium, complete heat recovery light component it is cooled after, send to return tank 8, then sent after the boosting of reflux pump 11 to
10 tower top of depropenizer realizes the maximization of stream stock heating efficiency in tower.The utility model is by depropanizing tower 1 and takes off
Energy thermal coupling between 10 liang of towers of propylene tower, can reduce process energy consumption expense nearly 40%, and energy-saving effect is good, have hot and cold public affairs
Few with engineering dosage, equipment investment expense is low, and process condition is mild, and system energy consumption is relatively low, heat inside system process
The many advantages such as coupling efficiency height, can effective raising Business Economic Benefit.
In the present invention, the tower top of depropenizer 10 is connected with the 4th pipeline, and has been arranged in parallel on the 4th pipeline
One reboiler 2 and heat exchanger 7, the first reboiler 2 and heat exchanger 7 are connect with the import of return tank 8 respectively, specific connection side
Formula are as follows: the second valve 5 is provided on the 4th pipeline, the one outlet of the second valve 5 is connect with the first reboiler 2；Second valve
Another outlet of door 5 is connected with third valve 6, and third valve 6 is connect with heat exchanger 7, and heat exchanger 7 is connect with return tank 8；The
One reboiler 2 is connect with third valve 6 and return tank 8 respectively.
Herein, it is adjusted into the heat transferring medium flow of the first reboiler 2 by the second valve 5, controls the first reboiler 2
Temperature be 25.5 DEG C~27.5 DEG C.Second valve 5 and third valve 6 are in series connection, the first reboiler 2 with carry out autospasy propylene
It after the light component of 10 tower top of tower exchanges heat between being flowed stock, is connect respectively with third valve 6, return tank 8 through pipeline, guarantees depropenizer
10 tower top light component temperature are 21.5 DEG C~23.2 DEG C.The feedforward-that the utility model is combined with the second valve 5 and third valve 6
Looped system improves thermal coupling utilization efficiency, increases the stability of process system.
In the present invention, the first valve 12 and the second valve 5 are triple valve.
The utility model further includes the second reboiler 4, and the tower bottom of depropanizing tower 1, depropanizing tower is arranged in the second reboiler 4
1 tower bottom is connect with the bottom and top of the second reboiler 4 respectively.The heat transferring medium of second reboiler 4 by system public work
Journey provides.
The tower bottom of the depropanizing tower 1 of the utility model is connected with the 6th pipeline, and the 6th pipeline is equipped with column bottoms pump 3, and the 6th
Pipeline is for producing de- propylene mixtures.
In the present invention, 10 tower bottom of depropenizer is connect through pipeline with 1 tower top of depropanizing tower, so that carrying out autospasy
The tower top that the tower bottom production of propylene tower 10 enters depropanizing tower 1 is separated.
The course of work of the utility model is as follows: the tower bottom extraction of propylene/propane mixture and depropenizer 10 to be separated
Object enters the 1st block of column plate of 1 tower top of depropanizing tower, and the totally 79 blocks of column plates of depropanizing tower 1 are adopted in the 79th block of column plate of 1 tower bottom of depropanizing tower
Propylene mixtures are taken off out, are sent through column bottoms pump 3 to next separative unit；In 9 liters of the group lease making compressor of 1 overhead extraction of depropanizing tower
After being depressed into 2.0MPa, send to the 99th block of column plate of 10 tower bottom of depropenizer, the 1st piece of column plate extraction light component of 10 tower top of depropenizer is made
For the heat transferring medium of the first reboiler 2 of 1 tower reactor of heat exchanger 7 and depropanizing tower, complete heat recovery light component it is cooled after,
It send to return tank 8, then send after the boosting of reflux pump 11 to the 1st block of column plate of 10 tower top of depropenizer.It should be noted that de- third
The number of plates of alkane tower 1 and depropenizer 10 can be configured according to the actual situation.
Claims (6)
1. the differential pressure thermocouple propylene refining separation system in a kind of production of propylene oxide, which is characterized in that including depropanizing tower
(1), compressor (9), depropenizer (10), return tank (8), reflux pump (11) and the first valve (12)；
The tower top of depropanizing tower (1) is connected with the first pipeline, and depropanizing tower (1) is passed through mixture to be separated by the first pipeline；
The tower top of depropanizing tower (1) also passes through the second pipeline and connect with the air inlet of compressor (9), and the gas outlet of compressor (9) passes through
Third pipeline is connect with the tower bottom of depropenizer (10)；
The tower top of depropenizer (10) is connected with the 4th pipeline, and the first reboiler (2) and heat exchange have been arranged in parallel on the 4th pipeline
Device (7), the first reboiler (2) and heat exchanger (7) are connect with the import of return tank (8) respectively, the outlet and reflux of return tank (8)
The import connection of (11) is pumped, the outlet of reflux pump (11) is connect with the first valve (12), and the one outlet of the first valve (12) is logical
It crosses the 5th pipeline to connect with the tower top of depropenizer (10), another outlet of the first valve (12) is for producing propylene product；
First reboiler (2) be arranged depropanizing tower (1) tower bottom, the tower bottom of depropanizing tower (1) respectively with the first reboiler (2)
Bottom and top connection.
2. the differential pressure thermocouple propylene refining separation system in production of propylene oxide according to claim 1, which is characterized in that
It is provided on 4th pipeline the second valve (5), the one outlet of the second valve (5) is connect with the first reboiler (2)；Second valve
(5) another outlet is connected with third valve (6), and third valve (6) is connect with heat exchanger (7)；First reboiler (2) is respectively
It is connect with third valve (6) and return tank (8).
3. the differential pressure thermocouple propylene refining separation system in production of propylene oxide according to claim 2, which is characterized in that
First valve (12) and the second valve (5) are triple valve.
4. the differential pressure thermocouple propylene refining separation system in production of propylene oxide according to claim 1, which is characterized in that
It further include the second reboiler (4), the tower bottom in depropanizing tower (1), the tower bottom point of depropanizing tower (1) is arranged in the second reboiler (4)
It is not connect with the bottom and top of the second reboiler (4).
5. the differential pressure thermocouple propylene refining separation system in production of propylene oxide according to claim 1, which is characterized in that
The tower bottom of depropanizing tower (1) is connected with the 6th pipeline, and the 6th pipeline is equipped with column bottoms pump (3), and the 6th pipeline is for producing de- third
Alkene mixture.
6. the differential pressure thermocouple propylene refining separation system in production of propylene oxide according to claim 1, which is characterized in that
Depropenizer (10) tower bottom is connect through pipeline with the depropanizing tower (1) tower top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820981487.XU CN208414288U (en) | 2018-06-25 | 2018-06-25 | A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820981487.XU CN208414288U (en) | 2018-06-25 | 2018-06-25 | A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide |
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| Publication Number | Publication Date |
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| CN208414288U true CN208414288U (en) | 2019-01-22 |
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| CN201820981487.XU Expired - Fee Related CN208414288U (en) | 2018-06-25 | 2018-06-25 | A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108586185A (en) * | 2018-06-25 | 2018-09-28 | 榆林学院 | A kind of differential pressure thermocouple propylene refining piece-rate system and separation method |
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2018
- 2018-06-25 CN CN201820981487.XU patent/CN208414288U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108586185A (en) * | 2018-06-25 | 2018-09-28 | 榆林学院 | A kind of differential pressure thermocouple propylene refining piece-rate system and separation method |
| CN108586185B (en) * | 2018-06-25 | 2023-11-17 | 榆林学院 | Differential pressure thermocouple propylene refining and separating system and separating method |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20190122 Termination date: 20190625 |
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| CF01 | Termination of patent right due to non-payment of annual fee |