CN103288603A - Optimized dimethyl ether device driving method - Google Patents
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- CN103288603A CN103288603A CN2013102245827A CN201310224582A CN103288603A CN 103288603 A CN103288603 A CN 103288603A CN 2013102245827 A CN2013102245827 A CN 2013102245827A CN 201310224582 A CN201310224582 A CN 201310224582A CN 103288603 A CN103288603 A CN 103288603A
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Abstract
The invention discloses an optimized dimethyl ether device driving method. The optimized dimethyl ether device driving method comprises the following steps of: (1) firstly putting medium-pressure nitrogen before a dimethyl ether device drives; (2) in an initial stage, strictly controlling an inlet temperature of a reactor; (3) rapidly increasing a dimethyl ether load to 1.5%, stabilizing for a period of time, and observing bed temperature change; (4) after bed temperature is penetrated, continuously increasing the dimethyl ether load to more than 10%; (5) when the dimethyl ether load reaches the using standard, starting to eliminate a medium-pressure nitrogen system for increasing pressure; (6) increasing a system pressure to an operating pressure; and (7) producing a qualified dimethyl ether product. The optimized dimethyl ether device driving method has the beneficial effects that high pressure batch charging is adopted, a system pressure increasing process is reduced, driving time is reduced to less than 2 hours at present from the originally about 5 hours, the driving time is reduced by 3 hours, consumption of methanol during batch charging is reduced, driving cost is saved, and overtemperature of a catalyst bed layer in a driving process is prevented and charging time of the dimethyl ether device is reduced.
Description
Technical field
The present invention relates to a kind of dme device starting method of optimization, belong to dme device technical field of producing.
Background technology
Dme is a kind of important chemical material, can be used for the synthetic of chemical, is a kind of emerging energy substitute, because its good physical property and chemical property, make dme that unique purposes be arranged in chemical industry such as pharmacy, fuel, agricultural chemicals, as easy compression, condensation, vaporization etc.Dme has very important effect in national economy, be one of new forms of energy product of greatly developing of country.At present both at home and abroad dimethyl ether production method is mainly the methanol vapor phase method, and this technical characterstic is that technology maturation is reliable, investment is low, the product adjustment is flexible, technology is simple, production cost is low etc.
The development in nearly ten years of China's dme production technology process, reach its maturity, but still there are some difficult problems in the dme production process, as the dme that adopts the heat-insulating fixed bed device feeds intake in the process, pressure and air speed are well below the design load (approximately having only 15%) of ordinary production owing to feed intake, cause methanol steam long in the reaction times that catalyst surface is detained, a large amount of gatherings of reaction heat cause the bed overtemperature, control temperature and have only by regulating the methanol steam input, means are single, are difficult to control the normal rising of bed temperature; Simultaneously because the pressure of foundation when reaching dme pressure-raising load is low excessively, it is long that pressure of foundation during with pressure-raising is brought up to the charging time of system's routine operating pressure, and in the startup procedure of whole dme all constantly with system gas emptying, cause consumption quantity of methyl alcohol increase in the startup procedure, these problems have caused big potential safety hazard and financial loss to enterprise.
Summary of the invention
The object of the present invention is to provide a kind of dme device starting method of optimization, can prevent beds overtemperature and shortening dme device charging time in the startup procedure.
The objective of the invention is to be achieved through the following technical solutions: a kind of dme device starting method of optimization, in increasing by one, the Reactor inlet of dme device presses nitrogen pipeline, and in the dme device fed intake process, it carried out according to following steps:
(1), device at first drops into before driving and presses nitrogen among the 3.5MPa, prevent because the bed overtemperature that the catalyst activity height causes under the underload and improve initial driving pressure;
(2), the initial stage, strict control dme load is corresponding reactor inlet temperatures down, and the dme load is increased to 1.5%, the inlet temperature that slowly increases reactor reaches more than 245 ℃ until the inlet temperature of reactor;
(3), fast dme is loaded and increase to 1.5%--10%, keep bed temperature in 380 ℃ of design temperatures, and stable temperature in, observe bed temperature and change;
(4), treat that bed temperature penetrates after, continue to increase the dme load to more than 10%, wherein dme every increase by 1.5% of loading, the inlet temperature of reactor increases 1-5 ℃, prevents beds overtemperature in the startup procedure;
(5), reach the use standard until the dme load, pressure nitrogen system pressure-raising in beginning to move back;
(6), system pressure is increased to working pressure;
(7), the dme product that output is qualified.
Press on the nitrogen pipeline in described and the twice gate valve is set with vacuum breaker, control the middle pressure nitrogen flow that enters in the reactor by gate valve.
Beneficial effect of the present invention is: press nitrogen pipeline in the Reactor inlet preparation, feed intake reactor air speed in the process of solution is low and cause the difficult problem of overtemperature, the employing high pressure feeds intake, minimizing system pressure-raising process, the driving time foreshortened in present 2 hours by original about 5 hours, and the driving time shortens 3 hours, reduced the consumption of methyl alcohol when feeding intake, saved the driving cost, prevented in the startup procedure beds overtemperature simultaneously and shortened dme device charging time.
Description of drawings
Fig. 1 is production scheme of the present invention;
Fig. 2 is the structural representation of dme device of the present invention.
Wherein, the 1-reactor, the 2-methanol evaporator, 3-input and output material interchanger is pressed nitrogen pipeline among the 4-, the 5-well heater.
Embodiment
Further describe technical scheme of the present invention below in conjunction with accompanying drawing, but that claimed scope is not limited to is described.
As Fig. 1, the dme device that the present invention adopts is the two-step approach synthetic technology, be raw material with methyl alcohol, dehydration reaction takes place and produces dme in methyl alcohol vaporization back in dimethyl ether reactor, in the dme rectifying tower, obtain purity then greater than the dme product of 99%wt, methanol content is less than 200ppmwt in the waste water, discharge amount of exhaust gas is few, dme is produced controlled methanol consumption and is mainly determined by the dme startup procedure, beds overtemperature in the dme device startup procedure, charging time are long, directly influence the production cost of dme.Reaction bed temperature and shortening feed intake the driving time to reducing the dme production cost in the control dme device startup procedure, and improving the dme competitiveness of product in market has vital role.
A kind of dme device starting method of optimization, in increasing by one, the Reactor inlet of dme device presses nitrogen pipeline, particularly be to increase to press nitrogen pipeline 4 in one between methanol evaporator 2 and input and output material interchanger 3, in the dme device fed intake process, it carried out according to following steps:
(1), device at first drops into before driving and presses nitrogen among the 3.5MPa, the temperature of nitrogen is normal temperature, at this moment system pressure is at 0.1-0.3MPa, can prevent because the bed overtemperature that the catalyst activity height causes under the underload and improve initial driving pressure;
(2), the initial stage, strict control dme load is the reactor inlet temperatures of correspondence down, shown in Figure 2, flow to the methanol steam flow that the variable valve increase enters system by b, flow to the flow of variable valve control phlegma by d, make its outlet process gas satisfy corresponding load required temperature down, the dme load is increased to 1.5%, the inlet temperature that slowly increases reactor reaches more than 245 ℃ until the inlet temperature of reactor;
(3), fast dme is loaded and increase to 1.5%--10%, keep bed temperature in 380 ℃ of design temperatures, and stable temperature in, observe bed temperature and change;
(4), treat that bed temperature penetrates after, continue to increase the dme load to more than 10%, wherein dme every increase by 1.5% of loading, the inlet temperature of reactor increases 1-5 ℃, prevent beds overtemperature in the startup procedure, wherein, corresponding relation such as the table one of the inlet temperature of dme load and reactor.
The corresponding relation of table one load and inlet temperature
| ? | Dimethyl ether reactor load % | |
| 1 | 0～1.5 | 245 |
| 2 | 8.5 | 250 |
| 3 | 16.5 | 255 |
| 4 | 23.5 | 260 |
(5), reach the use standard until the dme load, pressure nitrogen system pressure-raising in beginning to move back;
(6), system pressure is increased to working pressure;
(7), the dme product that output is qualified.
Press on the nitrogen pipeline in described and the twice gate valve is set with vacuum breaker, control the middle pressure nitrogen flow that enters in the reactor by gate valve.
Claims (2)
1. the dme device starting method of an optimization is pressed nitrogen pipeline in the Reactor inlet of dme device increases by one, and it is characterized in that: in the dme device fed intake process, it carried out according to following steps:
(1), device at first drops into before driving and presses nitrogen among the 3.5MPa, prevent because the bed overtemperature that the catalyst activity height causes under the underload and improve initial driving pressure;
(2), the initial stage, strict control dme load is corresponding reactor inlet temperatures down, and the dme load is increased to 1.5%, the inlet temperature that slowly increases reactor reaches more than 245 ℃ until the inlet temperature of reactor;
(3), fast dme is loaded and increase to 1.5%--10%, keep bed temperature in 380 ℃ of design temperatures, and stable temperature in, observe bed temperature and change;
(4), treat that bed temperature penetrates after, continue to increase the dme load to more than 10%, wherein dme every increase by 1.5% of loading, the inlet temperature of reactor increases 1-5 ℃, prevents beds overtemperature in the startup procedure;
(5), reach the use standard until the dme load, pressure nitrogen system pressure-raising in beginning to move back;
(6), system pressure is increased to working pressure;
(7), the dme product that output is qualified.
2. the dme device starting method of optimization according to claim 1 is characterized in that: press on the nitrogen pipeline in described the twice gate valve to be set with vacuum breaker, control the middle pressure nitrogen flow that enters in the reactor by gate valve.
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| CN201310224582.7A CN103288603B (en) | 2013-06-06 | 2013-06-06 | Optimized dimethyl ether device driving method |
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| CN201310224582.7A CN103288603B (en) | 2013-06-06 | 2013-06-06 | Optimized dimethyl ether device driving method |
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101130488A (en) * | 2007-08-08 | 2008-02-27 | 四川泸天化绿源醇业有限责任公司 | Catalyst temperature raising method for producing dimethyl ether by gas phase method |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101130488A (en) * | 2007-08-08 | 2008-02-27 | 四川泸天化绿源醇业有限责任公司 | Catalyst temperature raising method for producing dimethyl ether by gas phase method |
Non-Patent Citations (3)
| Title |
|---|
| 葛志跃等: "甲醇气相法制备二甲醚常见问题及解决措施", 《大氮肥》, vol. 35, no. 1, 29 February 2012 (2012-02-29), pages 35 - 37 * |
| 陈天富等: "10万t /a 二甲醚装置无氮工况下合成催化剂升温开车探讨", 《泸天化科技》, no. 3, 31 December 2011 (2011-12-31) * |
| 陈天富等: "二甲醚合成塔催化剂床层超温原因分析与对策", 《泸天化科技》, no. 3, 31 December 2011 (2011-12-31) * |
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