CN103977751A - Reactor overtemperature control method of methanol-to-olefins device - Google Patents
Reactor overtemperature control method of methanol-to-olefins device Download PDFInfo
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- CN103977751A CN103977751A CN201410146592.8A CN201410146592A CN103977751A CN 103977751 A CN103977751 A CN 103977751A CN 201410146592 A CN201410146592 A CN 201410146592A CN 103977751 A CN103977751 A CN 103977751A
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Abstract
The invention relates to a reactor overtemperature control method of a methanol-to-olefins device, and mainly solves the reactor overtemperature problem in the prior art. According to the reactor overtemperature control method of the methanol-to-olefins device, at least one temperature detectors are arranged respectively in a dense phase section and a dilute phase section of a fluidized bed reactor, when the detected temperature of the temperature detectors exceeds 500 DEG C, the temperature detectors alarm, operators need to perform operations of reducing raw material load or improving heat load, when the detected temperature exceeds 535 DEG C, spray water cooling interlocking is stared, if the detected temperature is still rising, cutting material interlocking is stared, and if the detected temperature decreases after water spraying, and when the detected temperature is reduced to 500 DEG C or less, the water spraying is stopped; the technical scheme well solves the reactor overtemperature problem, and the reactor overtemperature control method can be used for reactor temperature control of the MTO (methanol-to-olefins) device.
Description
Technical field
The present invention relates to a kind of control method of methanol-to-olefins device reaction device overtemperature.
Background technology
Ethene, propylene are the core of petrochemical industry and the most basic basic material.Along with expanding economy, the market demand of ethene, propylene is more and more vigorous, and consumption figure is sharp increase also.But due to the minimizing gradually of petroleum resources, climbing up and up of crude oil price, adopts the production line of traditional petroleum to face the challenge of raw material supply anxiety.The relative petroleum resources of coal resources are compared with horn of plenty, and cheap, adopt coal can greatly reduce the consumption of petroleum resources through Methanol ethene, propylene, have saved cost.Methanol-to-olefins (MTO) technique is to arise at the historic moment under this environment, shows huge potential advantages.
Because methanol-to-olefins is strong exothermal reaction, so the temperature control of its reactor seems particularly important.
CN96105942.7 has related to and a kind of the reaction vessel for exothermic reaction has been carried out to temperature controlled method, comprise and use two or more individual flow passages, the heat being pulled away as required injects two or more and has the cooling agent of different temperatures to said individual flow passage.But the method is not suitable for the methanol to olefins reaction temperature control that adopts fluidized-bed reactor.
Prior art remains the risk problem at MTO reactor reaction temperature overtemperature, and the present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the problem that prior art exists reactor overtemperature, and a kind of control method of new methanol-to-olefins device reaction device overtemperature is provided.The method, for the control of MTO device reaction actuator temperature, has advantages of not overtemperature, safe and reliable of reactor.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of control method of methanol-to-olefins device reaction device overtemperature, close phase section and dilute phase section at fluidized-bed reactor respectively at least arrange a Temperature Detector, when the detected temperatures of described Temperature Detector exceedes 500 DEG C of alarms, the operation that operating personnel need to reduce raw material load or improve heat-obtaining load, in the time that detected temperatures exceedes 535 DEG C, start shower water cooling interlocking, if detected temperatures still rises, start and cut off raw material interlocking, if detected temperatures declines after shower water, in the time that detected temperatures is reduced to below 500 DEG C, stop-spraying trickle.
In technique scheme, preferably, described cool water shower line is ring-type.
This patent adopts, at reactor, cool water shower line is set, and exceedes after uniform temperature at reactor, carries out spraying cooling, cuts off raw material simultaneously, has effectively controlled reactor temperature rise, safe and reliable, has obtained good technique effect.
Brief description of the drawings
Fig. 1 is the structural representation of device of the present invention.
1,2,3 is Temperature Detector; 4 is temperature alarming; 5 is temperature interlocking; 6 is cool water shower line; 7 is MTO reactor dilute phase section; 8 is product gas outlet; 9 is heat collector; 10 is heat collector fluidizing agent pipeline; 11 is methanol feedstock; 12 is the close phase section of MTO reactor; 13 is heat collector gaseous phase outlet pipeline.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Detailed description of the invention
[embodiment 1]
In the reactor part of MTO process units as shown in Figure 1, methyl alcohol enters from reactor bottom, and after having reacted, gas product, in top discharge, carries out subsequent treatment, and temperature of reactor is by adjusting the steam flow control of reactor external warmer.Three groups of online temperature detection (one group of dilute phase section is set on reactor axial direction, two groups of close phase sections), detection reaction temperature conditions in real time, when detected temperatures exceedes 500 DEG C of alarms, the operation that operating personnel need to reduce raw material load or improve heat-obtaining load, in the time that detected temperatures exceedes 535 DEG C, start shower water cooling interlocking, if detected temperatures still rises, start and cut off raw material interlocking, if detected temperatures declines after shower water, in the time that detected temperatures is reduced to below 500 DEG C, stop-spraying trickle.The temperature rise of reactor can be effectively controlled in this measure, does not cut off raw material in the process of carrying out shower water cooling as far as possible, ensures the safety of MTO device reaction system.
[comparative example]
According to the condition described in embodiment and step, cool water shower line is not set in reactor, MTO reaction temperature setting value is 480 DEG C, in the time that reaction temperature exceedes 535 DEG C, have to start and cut off raw material interlocking, system shutdown, causes enterprise's heavy losses.
Claims (2)
1. the control method of a methanol-to-olefins device reaction device overtemperature, close phase section and dilute phase section at fluidized-bed reactor respectively at least arrange a Temperature Detector, when the detected temperatures of described Temperature Detector exceedes 500 DEG C of alarms, the operation that operating personnel need to reduce raw material load or improve heat-obtaining load, in the time that detected temperatures exceedes 535 DEG C, start shower water cooling interlocking, if detected temperatures still rises, start and cut off raw material interlocking, if detected temperatures declines after shower water, in the time that detected temperatures is reduced to below 500 DEG C, stop-spraying trickle.
2. the control method of methanol-to-olefins device reaction device overtemperature according to claim 1, is characterized in that described cool water shower line is ring-type.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410146592.8A CN103977751A (en) | 2014-04-11 | 2014-04-11 | Reactor overtemperature control method of methanol-to-olefins device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410146592.8A CN103977751A (en) | 2014-04-11 | 2014-04-11 | Reactor overtemperature control method of methanol-to-olefins device |
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| CN103977751A true CN103977751A (en) | 2014-08-13 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1158857A (en) * | 1995-01-24 | 1997-09-10 | 三菱化学株式会社 | Method for controlling reaction temperature |
| CN1617842A (en) * | 2002-01-07 | 2005-05-18 | 埃克森美孚化学专利公司 | Reducing temperature differences within the regenerator of an oxygenate to olefin process |
| US7619011B1 (en) * | 2006-03-03 | 2009-11-17 | The United States Of America As Represented By The United States Department Of Energy | Design of slurry bubble column reactors: novel technique for optimum catalyst size selection contractual origin of the invention |
| CN102600771A (en) * | 2011-01-21 | 2012-07-25 | 中国科学院过程工程研究所 | Fluidized bed reactor and method for methanation of gas mixture containing H2 and CO |
-
2014
- 2014-04-11 CN CN201410146592.8A patent/CN103977751A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1158857A (en) * | 1995-01-24 | 1997-09-10 | 三菱化学株式会社 | Method for controlling reaction temperature |
| CN1617842A (en) * | 2002-01-07 | 2005-05-18 | 埃克森美孚化学专利公司 | Reducing temperature differences within the regenerator of an oxygenate to olefin process |
| US7619011B1 (en) * | 2006-03-03 | 2009-11-17 | The United States Of America As Represented By The United States Department Of Energy | Design of slurry bubble column reactors: novel technique for optimum catalyst size selection contractual origin of the invention |
| CN102600771A (en) * | 2011-01-21 | 2012-07-25 | 中国科学院过程工程研究所 | Fluidized bed reactor and method for methanation of gas mixture containing H2 and CO |
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Application publication date: 20140813 |