CN105985211A - System for preparing high-purity isobutene through cracking of methyl tert-butyl ether - Google Patents
System for preparing high-purity isobutene through cracking of methyl tert-butyl ether Download PDFInfo
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- CN105985211A CN105985211A CN201510076113.4A CN201510076113A CN105985211A CN 105985211 A CN105985211 A CN 105985211A CN 201510076113 A CN201510076113 A CN 201510076113A CN 105985211 A CN105985211 A CN 105985211A
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Abstract
The invention especially relates to a system for preparing high-purity isobutene through cracking of methyl tert-butyl ether, belonging to the technical field of chemical processing equipment. The system comprises a feed-discharge heat exchanger; the feed-discharge heat exchanger is connected with a raw material feeding pipeline, a first connection pipeline, a second connection pipeline and a third connection pipeline; the first connection pipeline is connected with a cutting tower; the second connection pipeline is connected with a heat conduction oil heater; the third connection pipeline is connected with a reactor; the top of the cutting tower is connected with a fourth connection pipeline; the bottom of the cutting tower is connected with a crude methanol discharge pipeline; the fourth connection pipeline is connected with an extraction tower; the top of the extraction tower is connected with a fifth connection pipeline; the side surface of the extraction tower is connected with a process water circulation pipeline; the bottom of the extraction tower is connected with a sixth connection pipeline; the fifth connection pipeline is connected with a light-component-removing tower; the process water circulation pipeline is connected with a methanol recovery tower; and the top of the methanol recovery tower is connected with a methanol recovery pipeline.
Description
Technical field
The invention belongs to chemical industry technical field of processing equipment, particularly relate to a kind of methyl tertiary butyl ether(MTBE) cracking high-purity isobutene. system.
Background technology
Existing methyl tertiary butyl ether(MTBE) cracking high-purity isobutene. many employings low-pressure process, process is that refined MTBE reacts through cracking reactor, product is through washing methanol removal, washing water utilizes through Methanol Recovery Posterior circle, washing gas phase carries out de-light and de-weight by compressor after being pressurizeed, and then obtains high-purity isobutene. product.The major defect that this device exists is that washing load is big, and Methanol Recovery energy consumption is high, and tower is more, and needs compressor, invest higher, operating cost is bigger.
Summary of the invention
The present invention provides a kind of methyl tertiary butyl ether(MTBE) cracking high-purity isobutene. system, to solve the washing problem that load is big, cost is high proposed in above-mentioned background technology.
nullTechnical problem solved by the invention realizes by the following technical solutions: the present invention provides a kind of methyl tertiary butyl ether(MTBE) cracking high-purity isobutene. system，It is characterized in that: include input and output material heat exchanger，Described input and output material heat exchanger connects has raw material to enter pipeline、First connects pipeline、Second connects pipeline、3rd connects pipeline，Described first connects pipeline connection Cutting Tap，And it is connected to the side of Cutting Tap，Described second connects pipeline connection hotline heater，Described 3rd connects pipeline connection responds device，And it is connected to the bottom of reactor，Described second other end connecting pipeline is also connected with reactor，And it is connected to the top of reactor，Described Cutting Tap top connects the 4th connection pipeline，Connect bottom described Cutting Tap and have crude carbinol discharge tube，Described 4th connects pipeline connection extraction tower，Described extraction tower top connects the 5th connection pipeline，Described extraction tower side connects fresh water (FW) circulating line，Connect bottom described extraction tower and have the 6th connection pipeline，Described 5th connects pipeline connection lightness-removing column，And it is connected to the side of lightness-removing column，Described fresh water (FW) circulating line connects methanol distillation column，And it is connected to the bottom of methanol distillation column，Described 6th connects pipeline is connected with methanol distillation column，And it is connected to the side of methanol distillation column，The top of described methanol distillation column connects Methanol Recovery pipeline，The top of described lightness-removing column connects light component discharge line，The bottom of described lightness-removing column connects isobutene. discharge line.
The reaction pressure of described reactor is 0.55 ~ 0.65MPa.
The invention have the benefit that
1 product initially enters Cutting Tap and major part methanol therein and the most anti-MTBE is separated, and reduces the treating capacity of follow-up Methanol Recovery, thus reduces energy consumption.And reaction is reaction under high pressure, it is not required to compressor boosting, decreases investment.
2 pyrolysis products are without condensation cooling, and heat exchange is cooled to 95 DEG C, and product gas phase state is directly entered Cutting Tap, thus saves recirculated water and steam consumption.
3 need not compressor, reduce the consumption of electricity, save the energy.
4 traditional handicrafts need 6 towers, and the technical program is reduced to 4, and decreases the quantity of auxiliary device (heat exchanger, container, pump, instrument etc.).
5 see accompanying drawing 2, for the isobutene. product specification obtained by the technical program, can meet polymer grade index.
6 see accompanying drawing 3,4, contrast according to traditional handicraft, and 60,000 tons/year of isobutene. these devices of scale can reduce estimated budget investment 5,000,000 yuan.Saving recirculated water 175 ton/ton isobutene., steam saving 0.91t/ ton isobutene., save electricity 76kwh/ ton isobutene., compared with traditional handicraft, isobutene. processing charges reduces by 302 yuan/ton of isobutene .s.
Accompanying drawing explanation
Fig. 1 is the device systems schematic flow sheet of the present invention；
Fig. 2 is the isobutene. product specification obtained by the present invention；
Fig. 3 is to use the processing charges needed for the present invention detailed (60,000 tons/year of isobutene. scales)；
Fig. 4 is that the processing charges needed for traditional approach is detailed (60,000 tons/year of isobutene. scales).
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention is described further:
In figure, 1-input and output material heat exchanger, 2-hotline heater, 3-reactor, 4-Cutting Tap, 5-extraction tower, 6-methanol distillation column, 7-lightness-removing column, 8-first connects pipeline, and 9-second connects pipeline, and 10-the 3rd connects pipeline, 11-the 4th connects pipeline, 12-crude carbinol discharge tube, and 13-the 5th connects pipeline, 14-the 6th connects pipeline, 15-fresh water (FW) circulating line, 16-Methanol Recovery pipeline, 17-light component discharge line, 18-isobutene. discharge line, 19-raw material enters pipeline.
Embodiment:
nullThe present embodiment includes input and output material heat exchanger 1，Input and output material heat exchanger 1 connects has raw material to enter pipeline 19、First connects pipeline 8、Second connects pipeline 9、3rd connects pipeline 10，First connects pipeline 8 connection Cutting Tap 4，And it is connected to the side of Cutting Tap 4，Second connects pipeline 9 connection hotline heater 2，3rd connects pipeline 10 connection responds device 3，And it is connected to the bottom of reactor 3，Second other end connecting pipeline 9 is also connected with reactor 3，And it is connected to the top of reactor 3，Cutting Tap 4 top connects the 4th connection pipeline 11，Connect bottom Cutting Tap 4 and have crude carbinol discharge tube 12，4th connects pipeline 11 connection extraction tower 5，Extraction tower 5 top connects the 5th connection pipeline 13，Extraction tower 5 side connects fresh water (FW) circulating line 15，Connect bottom extraction tower 5 and have the 6th connection pipeline 14，5th connects pipeline 13 connection lightness-removing column 7，And it is connected to the side of lightness-removing column 7，Fresh water (FW) circulating line 15 connects methanol distillation column 6，And it is connected to the bottom of methanol distillation column 6，6th connects pipeline 14 is connected with methanol distillation column 6，And it is connected to the side of methanol distillation column 6，The top of methanol distillation column 6 connects Methanol Recovery pipeline 16，The top of lightness-removing column 7 connects light component discharge line 17，The bottom of lightness-removing column 7 connects isobutene. discharge line 18.
The reaction pressure of described reactor is 0.55 ~ 0.65MPa.
Work process:
Raw material initially enters input and output material heat exchanger 1, enter back into after hotline heater 2 is raised to reaction temperature and enter reactor 3, product enters Cutting Tap 4 after input and output material heat exchanger 1, extraction product coarse methanol at the bottom of Cutting Tap 4 tower, the thick isobutene. of Cutting Tap 4 tower top enters extraction tower 5, product after extraction methanol removal enters lightness-removing column 7, the light component of lightness-removing column 7 removed overhead, obtains the high-purity isobutene. of product at the bottom of tower.
Extraction water (containing methanol) at the bottom of extraction tower 5 tower enters methanol distillation column 6, and methanol distillation column 6 tower top obtains methanol, and tower bottom technique water enters extraction tower 5, recycles.
Operation principle:
1 refines MTBE first passes around input and output material heat exchanger, makes raw material and the abundant heat exchange of product, improves heat utilization ratio.
2 through the raw material of input and output material heat exchange, uses hotline heater 2, after being heated to reaction temperature, enters reactor, and reaction pressure is 0.55 ~ 0.65MPa, is cracked to form methanol and isobutene., and cracking conversion ratio is more than 92%.
3 pyrolysis products are after input and output material heat exchanger is lowered the temperature (95 DEG C), and gas phase state enters Cutting Tap, separated by methanol (containing the most anti-MTBE) at the bottom of Cutting Tap tower, and as raw material of etherification, tower top obtains thick isobutene. (containing methanol 3.6%).
4 thick isobutene .s enter extraction tower 5, and water elution removes methanol therein.
Methanol aqueous solution at the bottom of 5 extraction tower towers delivers to methanol distillation column, obtains refined methanol as raw material of etherification by rectifying tower top, and tower bottom technique water is delivered to extraction tower 5 and recycled.
Thick isobutene. after 6 washings enters lightness-removing column, removes light component therein (by-product dimethyl ether), obtains the high-purity isobutene. of product at the bottom of tower.
Implementing above-mentioned flow process, the composition obtaining isobutene. and methanol is shown in Fig. 3 and Fig. 4, can meet polymer grade index.
Utilize technical solutions according to the invention, or those skilled in the art is under the inspiration of technical solution of the present invention, design similar technical scheme, and reach above-mentioned technique effect, all fall into protection scope of the present invention.
Claims (2)
- null1. methyl tertiary butyl ether(MTBE) cracking high-purity isobutene. system，It is characterized in that: include input and output material heat exchanger，Described input and output material heat exchanger connects has raw material to enter pipeline、First connects pipeline、Second connects pipeline、3rd connects pipeline，Described first connects pipeline connection Cutting Tap，And it is connected to the side of Cutting Tap，Described second connects pipeline connection hotline heater，Described 3rd connects pipeline connection responds device，And it is connected to the bottom of reactor，Described second other end connecting pipeline is also connected with reactor，And it is connected to the top of reactor，Described Cutting Tap top connects the 4th connection pipeline，Connect bottom described Cutting Tap and have crude carbinol discharge tube，Described 4th connects pipeline connection extraction tower，Described extraction tower top connects the 5th connection pipeline，Described extraction tower side connects fresh water (FW) circulating line，Connect bottom described extraction tower and have the 6th connection pipeline，Described 5th connects pipeline connection lightness-removing column，And it is connected to the side of lightness-removing column，Described fresh water (FW) circulating line connects methanol distillation column，And it is connected to the bottom of methanol distillation column，Described 6th connects pipeline is connected with methanol distillation column，And it is connected to the side of methanol distillation column，The top of described methanol distillation column connects Methanol Recovery pipeline，The top of described lightness-removing column connects light component discharge line，The bottom of described lightness-removing column connects isobutene. discharge line.
- A kind of methyl tertiary butyl ether(MTBE) cracking high-purity isobutene. system the most according to claim 1, it is characterised in that: the reaction pressure of described reactor is 0.55 ~ 0.65MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510076113.4A CN105985211A (en) | 2015-02-12 | 2015-02-12 | System for preparing high-purity isobutene through cracking of methyl tert-butyl ether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510076113.4A CN105985211A (en) | 2015-02-12 | 2015-02-12 | System for preparing high-purity isobutene through cracking of methyl tert-butyl ether |
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| CN105985211A true CN105985211A (en) | 2016-10-05 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101024595A (en) * | 2006-02-24 | 2007-08-29 | 兰州红叶精细化工公司 | Process for cracking isobutene by methyl-tert-butyl ether |
| CN103772113A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for preparing polymer-grade isobutene by cracking methyl tertbutyl ether |
| CN103992202A (en) * | 2013-03-11 | 2014-08-20 | 上海蓝科石化工程技术有限公司 | System and method for cracking of methyl tertiary butyl ether to prepare high purity isobutylene |
| CN204589028U (en) * | 2015-02-12 | 2015-08-26 | 天津海成能源工程技术有限公司 | The high-purity iso-butylene system of a kind of methyl tertiary butyl ether cracking |
-
2015
- 2015-02-12 CN CN201510076113.4A patent/CN105985211A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101024595A (en) * | 2006-02-24 | 2007-08-29 | 兰州红叶精细化工公司 | Process for cracking isobutene by methyl-tert-butyl ether |
| CN103772113A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for preparing polymer-grade isobutene by cracking methyl tertbutyl ether |
| CN103992202A (en) * | 2013-03-11 | 2014-08-20 | 上海蓝科石化工程技术有限公司 | System and method for cracking of methyl tertiary butyl ether to prepare high purity isobutylene |
| CN204589028U (en) * | 2015-02-12 | 2015-08-26 | 天津海成能源工程技术有限公司 | The high-purity iso-butylene system of a kind of methyl tertiary butyl ether cracking |
Non-Patent Citations (2)
| Title |
|---|
| 杨志毅等: "甲基叔丁基醚裂解制异丁烯技术进展", 《广东化工》 * |
| 程引贵等: "MTBE 裂解制异丁烯生产工艺及催化剂研究概述", 《甘肃科技》 * |
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