CN105985215A - Cracking system for preparing high-purity isobutene from propylene glycol tert-butyl ether - Google Patents
Cracking system for preparing high-purity isobutene from propylene glycol tert-butyl ether Download PDFInfo
- Publication number
- CN105985215A CN105985215A CN201510076111.5A CN201510076111A CN105985215A CN 105985215 A CN105985215 A CN 105985215A CN 201510076111 A CN201510076111 A CN 201510076111A CN 105985215 A CN105985215 A CN 105985215A
- Authority
- CN
- China
- Prior art keywords
- pipeline
- propylene glycol
- isobutene
- butyl ether
- reactor
- 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.)
- Pending
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention especially relates to a cracking system for preparing high-purity isobutene from propylene glycol tert-butyl ether, belonging to the field of preparation of isobutene. The cracking system is characterized in that one end of a first pipeline is connected with a feed heater while the other end of the first pipeline is connected with the top end of a reactor; one end of a second pipeline is connected with the bottom end of the reactor while the other end of the second pipeline is connected with a reaction product cooler; one end of a third pipeline is connected with the reaction product cooler while the other end of the third pipeline is connected with a flash tank; one end of a fourth pipeline is connected with the flash tank while the other end of the fourth pipeline is connected with a compressor; and one end of a fifth pipeline is connected with the compressor while the other end of the fifth pipeline is connected with a separating tower. The cracking system is low in cracking temperature, energy consumption, investment and operation cost, does not need washing and uses few towers.
Description
Technical field
The invention belongs to isobutene. preparation system field, particularly relate to a kind of propylene glycol t-butyl ether high purity isobutene. of utilizing
Cracking system.
Background technology
The method of method many employings methyl tertiary butyl ether(MTBE) cracking of existing high purity isobutene..Concrete producing process is refined methyl
Tertbutyl ether reacts through cracking reactor, and product utilizes through Methanol Recovery Posterior circle through washing methanol removal, washing water,
Washing gas phase carries out de-light and de-weight by compressor after being pressurizeed, and then obtains high-purity isobutene. product.It is main that this device exists
Shortcoming is that cracking temperature is high, and washing load is big, and Methanol Recovery energy consumption is high, and tower is more, invest higher, operating cost is bigger.
Summary of the invention
The present invention is directed to above-mentioned technical problem, it is provided that a kind of cracking temperature is low, it is not necessary to washing, and energy consumption is low, and tower is less, throws
Provide the cracking system utilizing propylene glycol t-butyl ether high purity isobutene. relatively low, that operating cost is less.
The technical solution adopted in the present invention is: a kind of cracking system utilizing propylene glycol t-butyl ether high purity isobutene., its
It is characterised by: include feed heater, reactor, product cooler, flash tank, compressor, knockout tower, the first pipe
Road, the second pipeline, the 3rd pipeline, the 4th pipeline, the 5th pipeline, one end of described first pipeline and described feed heater phase
Connecting and its other end is connected with the top of described reactor, one end of described second pipeline is connected also with the bottom of described reactor
And its other end is connected with described product cooler, one end of described 3rd pipeline is connected also with described product cooler
And its other end is connected with described flash tank, one end of described 4th pipeline is connected with described flash tank and its other end is with described
Compressor is connected, and one end of described 5th pipeline is connected with described compressor and its other end is connected with described knockout tower.
Reaction pressure in described reactor is 0.05MPa.
Cracking reaction temperature in described reactor 140 DEG C.
The invention have the benefit that
1, cracking reaction temperature 140 DEG C, cracking temperature is low, reduces heating dielectric dissipation；
2, major part propylene glycol is separated by flash tank, reduces the scale of knockout tower；
3, tradition device for making needs 6 towers, and the present invention is reduced to 1 tower and a flash tank, and it is attached to decrease other
The quantity of genus equipment (heat exchanger, container, pump, instrument etc.)；
4, product enters atmospheric flashing tank, is circulated from tank bottoms discharge by major part propylene glycol, and tank deck is thick isobutene. warp
Entering knockout tower after compressor pressurization, owing to propylene glycol and by-product thereof are very big with the boiling point difference of isobutene., isobutene. easily divides
From, thus decrease the energy consumption of the number of plates and tower, and the purity of isobutene. is up to more than 99.9%；
5, compared with tradition methyl tertiary butyl ether(MTBE) cracking apparatus, it is not necessary to the steps such as washing, alcohol recovery, equipment needed thereby reduces, enters one
Step decreases energy consumption and investment, and operating cost is less.
Accompanying drawing explanation
Fig. 1 is the principle schematic of the present invention.
Detailed description of the invention
The invention will be further described below in conjunction with the accompanying drawings:
In figure, 1-feed heater, 2-reactor, 3-product cooler, 4-flash tank, 5-compressor, 6-knockout tower,
7-the first pipeline, 8-the second pipeline, 9-the 3rd pipeline, 10-the 4th pipeline, 11-the 5th pipeline.
Embodiment
As it is shown in figure 1, a kind of cracking system utilizing propylene glycol t-butyl ether high purity isobutene., including feed heater 1,
Reactor 2, product cooler 3, flash tank 4, compressor 5, knockout tower the 6, first pipeline the 7, second pipeline 8,
Three pipeline the 9, the 4th pipeline the 10, the 5th pipelines 11, one end of the first pipeline 7 is connected with feed heater 1 and its other end
Being connected with the top of reactor 2, one end of the second pipeline 8 is connected with the bottom of reactor 2 and its other end and product
Cooler 3 is connected, and one end of the 3rd pipeline 9 is connected with product cooler 3 and its other end is connected with flash tank 4,
One end of 4th pipeline 10 is connected with flash tank 4 and its other end is connected with compressor 5, one end of the 5th pipeline 11 and pressure
Contracting machine 5 is connected and its other end is connected with knockout tower 6.
Reaction pressure in reactor 2 is 0.05MPa.
Cracking reaction temperature in reactor 2 140 DEG C.
Operation principle:
1) refined propylene glycol t-butyl ether first passes around after feed heater 1 is heated to reaction temperature, enters reactor 2,
Reaction pressure is 0.05MPa (g), is cracked to form propylene glycol alcohol and isobutene., and cracking conversion ratio is more than 99%；
3) pyrolysis product is after product cooler 3 is lowered the temperature, and gas-liquid two-phase enters flash tank 4, the tank bottoms general of flash tank 4
Propylene glycol (containing unreacted propylene glycol t-butyl ether and a small amount of isobutene .) is separated, and as raw material of etherification, tank deck obtains the most different
Butylene；
4) thick isobutene. enters knockout tower 6 after compressor 5 pressurizes；
5) bottom thick propylene glycol at the bottom of knockout tower 6 tower and flash tank 4, propylene glycol is incorporated as raw material of etherification, and it is high that tower top obtains product
Pure isobutene..
Implement above-mentioned flow process, obtain high-purity isobutene. product composition and be shown in Table 1, polymer grade index can be met.
Table 1 isobutene. product specification table
With tradition methyl tertiary butyl ether(MTBE) cracker contrast, the isobutene. production scale of this equipment reaches 50,000 tons/year, can save
Recirculated water 185 ton/ton isobutene., steam saving 0.8t/ ton isobutene., save electricity 56kwh/ ton isobutene.；With tradition methyl
Tertbutyl ether cracking technology is compared, and isobutene. processing charges reduces by 516 yuan/ton of isobutene .s, and concrete outcome is shown in Table 2, table 3.
Table 2 uses present device processing charges (50,000 tons/year of isobutene. scales)
Table 3 tradition methyl tertiary butyl ether(MTBE) cracking apparatus processing charges (50,000 tons/year of isobutene. scales)
Above 1 embodiment of the present invention is described in detail, but described content has been only presently preferred embodiments of the present invention, no
The practical range for limiting the present invention can be considered.All impartial changes made according to the present patent application scope and improvement etc., all should
Within still belonging to the patent covering scope of the present invention.
Claims (3)
- null1. the cracking system utilizing propylene glycol t-butyl ether high purity isobutene.，It is characterized in that: include feed heater、Reactor、Product cooler、Flash tank、Compressor、Knockout tower、First pipeline、Second pipeline、3rd pipeline、4th pipeline、5th pipeline，One end of described first pipeline is connected with described feed heater and its other end is connected with the top of described reactor，One end of described second pipeline is connected with the bottom of described reactor and its other end is connected with described product cooler，One end of described 3rd pipeline is connected with described product cooler and its other end is connected with described flash tank，One end of described 4th pipeline is connected with described flash tank and its other end is connected with described compressor，One end of described 5th pipeline is connected with described compressor and its other end is connected with described knockout tower.
- A kind of cracking system utilizing propylene glycol t-butyl ether high purity isobutene. the most according to claim 1, it is characterised in that: the reaction pressure in described reactor is 0.05MPa.
- A kind of cracking system utilizing propylene glycol t-butyl ether high purity isobutene. the most according to claim 1, it is characterised in that: the cracking reaction temperature in described reactor 140 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510076111.5A CN105985215A (en) | 2015-02-12 | 2015-02-12 | Cracking system for preparing high-purity isobutene from propylene glycol tert-butyl ether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510076111.5A CN105985215A (en) | 2015-02-12 | 2015-02-12 | Cracking system for preparing high-purity isobutene from propylene glycol tert-butyl ether |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105985215A true CN105985215A (en) | 2016-10-05 |
Family
ID=57041204
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510076111.5A Pending CN105985215A (en) | 2015-02-12 | 2015-02-12 | Cracking system for preparing high-purity isobutene from propylene glycol tert-butyl ether |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105985215A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920026A (en) * | 2019-12-05 | 2021-06-08 | 湖南中创化工股份有限公司 | Preparation method and device of propylene glycol primary mono-tert-butyl ether |
| CN112920025A (en) * | 2019-12-05 | 2021-06-08 | 湖南中创化工股份有限公司 | Preparation method and device of propylene glycol primary mono-tert-butyl ether |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101003458A (en) * | 2006-01-19 | 2007-07-25 | 中国石油化工股份有限公司 | Method for preparing propylene by dehydrogenating propane |
| CN101358147A (en) * | 2007-07-31 | 2009-02-04 | 中国石油化工股份有限公司 | Method for producing clean gasoline by naphtha upgrading |
| CN101724432A (en) * | 2008-10-31 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing high-octane gasoline by light hydrocarbon non-hydrogenation modification |
| CN102807465A (en) * | 2011-05-31 | 2012-12-05 | 中国石油化工股份有限公司 | Method for producing propane and gasoline by using butane |
-
2015
- 2015-02-12 CN CN201510076111.5A patent/CN105985215A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101003458A (en) * | 2006-01-19 | 2007-07-25 | 中国石油化工股份有限公司 | Method for preparing propylene by dehydrogenating propane |
| CN101358147A (en) * | 2007-07-31 | 2009-02-04 | 中国石油化工股份有限公司 | Method for producing clean gasoline by naphtha upgrading |
| CN101724432A (en) * | 2008-10-31 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing high-octane gasoline by light hydrocarbon non-hydrogenation modification |
| CN102807465A (en) * | 2011-05-31 | 2012-12-05 | 中国石油化工股份有限公司 | Method for producing propane and gasoline by using butane |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920026A (en) * | 2019-12-05 | 2021-06-08 | 湖南中创化工股份有限公司 | Preparation method and device of propylene glycol primary mono-tert-butyl ether |
| CN112920025A (en) * | 2019-12-05 | 2021-06-08 | 湖南中创化工股份有限公司 | Preparation method and device of propylene glycol primary mono-tert-butyl ether |
| CN112920026B (en) * | 2019-12-05 | 2023-08-18 | 湖南中创化工股份有限公司 | Preparation method and device of propylene glycol primary mono-tert-butyl ether |
| CN112920025B (en) * | 2019-12-05 | 2023-08-18 | 湖南中创化工股份有限公司 | Preparation method and device of propylene glycol primary mono-tert-butyl ether |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105037094B (en) | A kind of energy coupling rectificating method of acetate preparation of ethanol by hydrogenating | |
| CN203710716U (en) | Device for improving recycling rate of alcohol ketone components in refining process of cyclohexanone | |
| CN105348098B (en) | Method for rectifying and separating methyl formate, methanol and water by intermittent reaction | |
| CN105985215A (en) | Cracking system for preparing high-purity isobutene from propylene glycol tert-butyl ether | |
| CN101381273A (en) | Method for preparing isobutene by tert-butanol and apparatus | |
| CN106831360B (en) | Process method for continuously preparing β -naphthyl methyl ether | |
| CN104072359A (en) | Device and method for preparing propionic anhydride through reactive distillation of acetic anhydride and propionic acid | |
| CN109939457A (en) | The preparation method and device of isoamyl acetate | |
| CN203264320U (en) | Vacuum reduced-pressure distillation device | |
| CN109627145A (en) | A kind of high-efficiency low energy consumption sodium methoxide equipment for purifying | |
| CN107162909B (en) | A kind of thermal coupling methods and device that vinyl acetate is refined | |
| CN105693468B (en) | Isopropyl acetate hydrogenization method production ethanol and the post-processing approach of isopropanol | |
| CN204589030U (en) | A kind of cracking system utilizing propylene glycol t-butyl ether high purity iso-butylene | |
| CN103242896B (en) | Reduced pressure distillation method with low energy consumption and deep total distillation rate | |
| CN105061134B (en) | A kind of method and device for separating high-purity longifolene | |
| CN103755532B (en) | Chloromethyl ether continuous production system and production process utilizing same | |
| CN103739423A (en) | Process for recovering C5 from etherified liquefied gas | |
| CN112409181A (en) | Dimethyl oxalate rectifying device for coal chemical industry | |
| CN109776314B (en) | Preparation method of cinnamate | |
| CN102408319A (en) | Production process of p-hydroxyanisole | |
| CN103865657B (en) | A kind of production technique adopting chemical synthesis to prepare biofuel | |
| CN205061982U (en) | Methyl alcohol system lighter hydrocarbons process systems that energy integration utilized | |
| CN214032309U (en) | Dimethyl oxalate rectifying device for coal chemical industry | |
| CN204897786U (en) | Methyl tert butyl ether production facility | |
| CN204589028U (en) | The high-purity iso-butylene system of a kind of methyl tertiary butyl ether cracking |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20161005 |