CN207102568U - A kind of aromatisation plant modification into isomerization unit - Google Patents
A kind of aromatisation plant modification into isomerization unit Download PDFInfo
- Publication number
- CN207102568U CN207102568U CN201720907943.1U CN201720907943U CN207102568U CN 207102568 U CN207102568 U CN 207102568U CN 201720907943 U CN201720907943 U CN 201720907943U CN 207102568 U CN207102568 U CN 207102568U
- Authority
- CN
- China
- Prior art keywords
- weight
- removing column
- aromatisation
- reaction product
- isomerization unit
- 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.)
- Expired - Fee Related
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provide a kind of aromatisation plant modification into isomerization unit, including reactor and weight-removing column, head tank is connected to the reactor, and the reactor is connected to the weight-removing column, and the weight-removing column is connected respectively to isomery oil product tank and the products pot of carbon four.A kind of aromatisation plant modification provided by the utility model into isomerization unit, not only solve the problem of aromatisation device is idle for a long time, the problem of also solving the raw materials for production deficiency of current methyl tertiary butyl ether(MTBE) device.
Description
Technical field
The utility model is related to isomerization production technical field, more particularly to a kind of aromatisation plant modification into isomerization
Device.
Background technology
In recent years, the benefit of methyl tertiary butyl ether(MTBE) production was considerable, but the raw material of methyl tertiary butyl ether(MTBE) production compares
It is more in short supply, the long period full production of methyl tertbutyl ether production equipment can not be met, therefore, how cost-effective production
Raw material needed for enough methyl tertiary butyl ether(MTBE) production, it is the most important thing of current methyl tertiary butyl ether(MTBE) production.
Utility model content
Technical problem to be solved in the utility model be to provide a kind of aromatisation plant modification into isomerization unit, with
Reach the purpose for being capable of the required raw material of the enough methyl tertiary butyl ether(MTBE) production of cost-effective production.
In order to solve the above technical problems, the utility model provide a kind of aromatisation plant modification into isomerization unit,
Including reactor and weight-removing column, head tank sequentially passes through the first feed preheater, the second feed preheater, the heat exchange of the first input and output material
Device, the second input and output material heat exchanger and heating furnace are connected to the reactor, and the reactor sequentially passes through the heat exchange of the second input and output material
Device, the first input and output material heat exchanger, reaction product water cooler, reaction product knockout drum, liquid phase feeding pump, weight-removing column input and output material
Heat exchanger is connected with the weight-removing column, and the reaction product knockout drum also sequentially passes through suction port of compressor liquid separation tank, rich gas
Compressor, compressor outlet liquid separation tank are connected with the weight-removing column, and the weight-removing column sequentially passes through weight-removing column bottom reboiler, de- weight
Tower input and output material heat exchanger, weight-removing column base oil reactor product cooler, oil product delivery pump are connected to isomery oil product tank, the weight-removing column
Sequentially pass through weight-removing column top cooler, weight-removing column top return tank, weight-removing column top reflux pump and be connected to the products pot of carbon four.
Further, the suction port of compressor liquid separation tank is connected to the reaction product gas-liquid separation by liquid-phase reflux pump
Tank.
Further, the compressor outlet liquid separation tank connects the reaction product knockout drum.
Further, the compressor outlet liquid separation tank connects the reaction product water cooler.
Further, weight-removing column top return tank connects the weight-removing column.
Further, the gaseous phase outlet of weight-removing column bottom reboiler connects the weight-removing column.
A kind of aromatisation plant modification provided by the utility model into isomerization unit, be by aromatisation plant modification and
Into solving the problems, such as that aromatisation device is idle for a long time, improve the utilization rate of device, saved resource, improve economy
Benefit.Also, a kind of aromatisation plant modification provided by the utility model into isomerization unit, with carbon four after iso-butane, ether,
The high material of alkene carbon fourth class carbon four is that raw material cost-effective can produce the required original of enough methyl tertiary butyl ether(MTBE) production
Material, the i.e. product of carbon four, solve the problems, such as the raw materials for production deficiency of current methyl tertiary butyl ether(MTBE) device, promote methyl tertbutyl
The production operating of ether.
Brief description of the drawings
Fig. 1 be the utility model embodiment provide aromatisation plant modification into isomerization unit structural representation.
Embodiment
Referring to Fig. 1, a kind of aromatisation plant modification that the utility model embodiment provides into isomerization unit, main bag
Include reactor 106 and weight-removing column 115.Wherein, head tank 100 sequentially passes through the first feed preheater 101, the second feed preheater
102nd, the first input and output material heat exchanger 103, the second input and output material heat exchanger 104 and heating furnace 105 are connected to reactor 106.Reactor
106 sequentially pass through the second input and output material heat exchanger 104, the first input and output material heat exchanger 103, reaction product water cooler 107, reaction product
Knockout drum 108, liquid phase feeding pump 109, weight-removing column input and output material heat exchanger 113 are connected with weight-removing column 115.Reaction product gas-liquid
Knockout drum 108 also sequentially passes through suction port of compressor liquid separation tank 110, rich gas compressor 111, compressor outlet liquid separation tank 112 and institute
Weight-removing column 115 is stated to connect.Weight-removing column 115 sequentially passes through weight-removing column bottom reboiler 116, weight-removing column input and output material heat exchanger 113, de- weight
Bottom of towe oil product cooler 117, oil product delivery pump 118 are connected to isomery oil product tank 123.Weight-removing column 115 also sequentially passes through
Weight-removing column top cooler 120, weight-removing column top return tank 119, weight-removing column top reflux pump 121 are connected to the products pot 122 of carbon four.
Carbon four, the high raw material of alkene carbon fourth class carbon four are first successively by former by first after iso-butane, ether in head tank 100
The preheating temperature of 101 and second feed preheater of material preheater 102 is raised to 200 DEG C, then by the He of the first input and output material heat exchanger 103
The reaction product that second input and output material heat exchanger 104 is 290 DEG C with the temperature for carrying out autoreactor 106 carries out heat exchange and further risen
Temperature, temperature is raised to 253 DEG C, then heating-up temperature is raised to 280 DEG C in heating furnace 105, into reactor 106 in reacted.
In reactor 106 290 DEG C caused by reaction, 0.2MPa reaction product discharged from the bottom of reactor 106, first pass through
Second input and output material heat exchanger 104 and the raw material of carbon four from head tank 100 carry out heat exchange temperature and drop to 240 DEG C, then by the
One input and output material heat exchanger 103 and the raw material of carbon four heat exchange again from head tank 100, temperature drop to 124 DEG C, 124 DEG C again
Reaction product by reaction product water cooler 107 further cooling after enter reaction product knockout drum 108 in enter promoting the circulation of qi
Liquid separates.
The liquid phase separated in reaction product knockout drum 108 is pressurizeed through liquid phase feeding pump 109, with 0.68t/h's
Flow enters weight-removing column input and output material heat exchanger 113, with dividing from the liquid phase of weight-removing column 115 in weight-removing column input and output material heat exchanger 113
100 DEG C, which are reduced to, from thing progress heat-exchange temperature is discharged into weight-removing column 115.The gas phase separated in reaction product knockout drum 108
The liquid phase being mingled with gas phase is isolated into suction port of compressor liquid separation tank 110, liquid phase is separated in suction port of compressor liquid separation tank 110
Gas phase be compressed into rich gas compressor 111, temperature drop to 76 DEG C, air pressure be raised to 0.7MPa, the gas phase enters compressor
Outlet liquid separation tank 112 further separates enters weight-removing column 115 after the liquid phase in gas phase with 21.65t/h flow.
Into the gas phase in weight-removing column 115 and liquid phase, caused isomery oil enters from the bottom of weight-removing column 115 after separation
Weight-removing column bottom reboiler 116 enters in weight-removing column input and output material heat exchanger 113 with carrying out autoreaction after isolating the gas wherein carried
Temperature is changed into 100 DEG C after the liquid phase separated in product knockout drum 108 is exchanged heat, and 100 DEG C of isomery oil enters back into
Cool down in weight-removing column base oil reactor product cooler 117, temperature be reduced to 40 DEG C, pressure be changed into 0.6MPa, finally by oil product delivery pump
118 are pressed onto in isomery oil product tank 123 with 1.8t/h flow.
The product of carbon four caused by being separated in weight-removing column 115 is with 49 DEG C of temperature, 0.5MPa pressure at the top of weight-removing column 115
Discharge, 40 DEG C are cooled to by weight-removing column top cooler 120, are changed into by the product temperature of weight-removing column top 119 carbon of return tank four
40 DEG C, pressure be changed into 0.45MPa, the products pot 122 of carbon four is most pressed onto with 18.9t/h flow through weight-removing column top reflux pump 121 afterwards
In, the raw material as MTBE devices (i.e. methyl tertiary butyl ether(MTBE) device) production methyl tertiary butyl ether(MTBE).
In order that the liquid phase that suction port of compressor liquid separation tank 110 and compressor outlet liquid separation tank 112 are separated can be effective
Recycling, suction port of compressor liquid separation tank 110 is connected to reaction product knockout drum 108 by liquid-phase reflux pump 114,
Compressor outlet liquid separation tank 112 is also connected with reaction product knockout drum 108.Separated in suction port of compressor liquid separation tank 110
The liquid phase gone out is pressed back into reaction product knockout drum 108 by liquid-phase reflux pump 114 and carries out gas-liquid separation again, meanwhile,
The liquid phase isolated in compressor outlet liquid separation tank 112 also returns to reaction product knockout drum 108 and carries out gas-liquid point again
From.
Compressor outlet liquid separation tank 112 is directly connected to reaction product water cooler 107, can be by compressor outlet liquid separation tank
A part of gas in 112 is sent into reaction product water cooler 107 and cooled down again.
Weight-removing column 115 is directly connected to weight-removing column top return tank 119, and the product of carbon four discharged in weight-removing column 115 can be direct
It is discharged into after weight-removing column top return tank 119 flows back and arranges into the products pot 122 of carbon four, (i.e. methyl tertiary butyl ether(MTBE) fills as MTBE devices
Put) production methyl tertiary butyl ether(MTBE) raw material..
In addition, the gaseous phase outlet connection weight-removing column 115 of weight-removing column bottom reboiler 116, can be by weight-removing column bottom reboiler 116
Caused gas phase is directly discharged into weight-removing column 115 and further separated.
A kind of aromatisation plant modification provided by the utility model into isomerization unit, be by aromatisation plant modification and
Into solving the problems, such as that aromatisation device is idle for a long time, improve the utilization rate of device, saved resource, improve economy
Benefit.Also, a kind of aromatisation plant modification provided by the utility model into isomerization unit, with carbon four after iso-butane, ether,
The high material of alkene carbon fourth class carbon four is that raw material cost-effective can produce the required original of enough methyl tertiary butyl ether(MTBE) production
Material, the i.e. product of carbon four, solve the problems, such as the raw materials for production deficiency of current methyl tertiary butyl ether(MTBE) device, promote methyl tertbutyl
The production operating of ether.
It should be noted last that above embodiment is only illustrating the technical solution of the utility model rather than limit
System, although the utility model is described in detail with reference to example, it will be understood by those within the art that, can be right
The technical solution of the utility model is modified or equivalent substitution, without departing from the spirit and model of technical solutions of the utility model
Enclose, it all should cover among right of the present utility model.
Claims (6)
1. a kind of aromatisation plant modification into isomerization unit, it is characterised in that：Including reactor (106) and weight-removing column
(115), head tank (100) sequentially passes through the first feed preheater (101), the second feed preheater (102), the first input and output material and changed
Hot device (103), the second input and output material heat exchanger (104) and heating furnace (105) are connected to the reactor (106), the reactor
(106) sequentially pass through the second input and output material heat exchanger (104), the first input and output material heat exchanger (103), reaction product water cooler (107),
Reaction product knockout drum (108), liquid phase feeding pump (109), weight-removing column input and output material heat exchanger (113) and the weight-removing column
(115) connect, the reaction product knockout drum (108) also sequentially passes through suction port of compressor liquid separation tank (110), rich gas compression
Machine (111), compressor outlet liquid separation tank (112) are connected with the weight-removing column (115), and the weight-removing column (115) sequentially passes through de-
Weight tower bottom reboiler (116), weight-removing column input and output material heat exchanger (113), weight-removing column base oil reactor product cooler (117), oil product are defeated
Send pump (118) to be connected to isomery oil product tank (123), the weight-removing column (115) sequentially pass through weight-removing column top cooler (120),
Weight-removing column top return tank (119), weight-removing column top reflux pump (121) are connected to the products pot of carbon four (122).
2. aromatisation plant modification according to claim 1 into isomerization unit, it is characterised in that：The compressor enters
Mouth liquid separation tank (110) is connected to the reaction product knockout drum (108) by liquid-phase reflux pump (114).
3. aromatisation plant modification according to claim 1 into isomerization unit, it is characterised in that：The compressor goes out
Mouth liquid separation tank (112) connects the reaction product knockout drum (108).
4. aromatisation plant modification according to claim 1 into isomerization unit, it is characterised in that：The compressor goes out
Mouth liquid separation tank (112) connects the reaction product water cooler (107).
5. aromatisation plant modification according to claim 1 into isomerization unit, it is characterised in that：The weight-removing column top
Return tank (119) connects the weight-removing column (115).
6. aromatisation plant modification according to claim 1 into isomerization unit, it is characterised in that：The weight-removing column bottom
The gaseous phase outlet of reboiler (116) connects the weight-removing column (115).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720907943.1U CN207102568U (en) | 2017-07-25 | 2017-07-25 | A kind of aromatisation plant modification into isomerization unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720907943.1U CN207102568U (en) | 2017-07-25 | 2017-07-25 | A kind of aromatisation plant modification into isomerization unit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207102568U true CN207102568U (en) | 2018-03-16 |
Family
ID=61586004
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720907943.1U Expired - Fee Related CN207102568U (en) | 2017-07-25 | 2017-07-25 | A kind of aromatisation plant modification into isomerization unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207102568U (en) |
-
2017
- 2017-07-25 CN CN201720907943.1U patent/CN207102568U/en not_active Expired - Fee Related
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204162631U (en) | A kind of xylene production system | |
| CN102504330A (en) | Method for preparing polyolefin wax | |
| CN103896280B (en) | A kind of operation method of polysilicon cold hydrogenation | |
| CN204434297U (en) | Prepare the system of trichlorosilane | |
| CN205035303U (en) | Consecutive reaction device of N - methyl carboxamide | |
| CN104370740A (en) | Production method of isobornyl acetate | |
| CN207102568U (en) | A kind of aromatisation plant modification into isomerization unit | |
| CN106748631A (en) | A kind of monochloro methane energy-saving processing technique and device | |
| CN103288601A (en) | Cyclohexanol distillation method | |
| CN109020824A (en) | A kind of formamide separation system and formamide separating technology | |
| CN219355282U (en) | Heat exchange device for cyclohexene extraction and rectification | |
| CN102134080B (en) | Heat-pump energy-saving separating device for extracting trichlorosilane by adopting static mixing booster and method | |
| CN102502697B (en) | Method for recovering ammonia in morpholine solution | |
| CN207247960U (en) | A kind of coke powder cooler | |
| CN208414288U (en) | A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide | |
| CN107056577A (en) | The technique of pseudocumene in a kind of next door tower heat pump distillation separation C9 aromatic | |
| CN102583395A (en) | Heat pump rectification method for refining trichlorosilane | |
| CN105566051A (en) | Disproportionated reaction product separation and heat exchange system and processing method thereof | |
| CN105950216A (en) | Method for producing chlorinated paraffin-70 with bubbling agitating gas cooling or heating method | |
| CN209161884U (en) | A kind of system that cyclohexane dehydrogenation prepares cyclohexene | |
| CN204939338U (en) | A kind of reactive system of coking crude benzene hydrogenation technique | |
| CN103819507B (en) | A kind of ethrel resets technique | |
| CN105498264A (en) | Paraxylene disproportionated product fractionation system and processing method thereof | |
| CN206214823U (en) | A kind of continuous vacuum crystallization system of black titanium liquid | |
| CN218089444U (en) | Device for extracting and purifying carbon tetraolefin |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20180316 Termination date: 20180725 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |