CN102010301A - Low-energy-consumption process for producing dimethyl ether and production equipment thereof - Google Patents
Low-energy-consumption process for producing dimethyl ether and production equipment thereof Download PDFInfo
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- CN102010301A CN102010301A CN2010105327736A CN201010532773A CN102010301A CN 102010301 A CN102010301 A CN 102010301A CN 2010105327736 A CN2010105327736 A CN 2010105327736A CN 201010532773 A CN201010532773 A CN 201010532773A CN 102010301 A CN102010301 A CN 102010301A
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Abstract
The invention discloses a low-energy-consumption process for producing dimethyl ether and production equipment thereof. The production equipment comprises a methanol preheater, a methanol heater, a methanol evaporator, a flash drum, a vaporization tower, a reactor and a rectifying tower, which are connected with one another through a pipeline. The producing process comprises the following steps of: preheating methanol serving as a raw material with steam condensate and waste water by using the methanol preheater; exhausting the preheated methanol into the methanol heater; heating with reaction gas and exhausting the heated methanol into the methanol evaporator; heating with steam condensate and waste water; exhausting a steam-liquid mixture into the flash drum; cooling the mixed gas coming out of the reactor by using a gas heat exchanger; recycling heat energy by using a first vaporization tower reboiler and the methanol heater; condensing the mixed gas in a crude methanol preheater and a crude methanol condenser respectively; separating out non-condensable gas in a crude methyl ether storage groove; and exhausting crude methyl ether into the crude methanol preheater, partially vaporizing and exhausting the partially vaporized crude methanol into the rectifying tower. The process and the equipment are suitable for producing 99.0 to 99.9 percent dimethyl ether from refined methanol, can make full use of heat energy, save heating steam and cooling water and lower production cost.
Description
Technical field
The present invention relates to the dme synthesis technical field, especially relate to a kind of less energy-consumption dme manufacturing process and production unit thereof.
Background technology
Rapid growth along with national economy, demand to petroleum resources also enlarges day by day, the insufficient problem of crude resources will seriously restrict the development of petrochemical industry, and will threaten energy security and economic security, so the exploitation of substitute energy all has and important meaning for energy security.Dme is a kind of nontoxic oxygenated fuel, and it can be formed by multiple resource conversion such as coal, Sweet natural gas and biomass.Dme is as domestic fuel gas, and it all is better than oil liquefied gas in performance index such as accumulating, combustion safety, premix gas calorific value and theoretical combustion temperatures, can be used as the peak regulation gas and the liquefied gas mixed gas of urban duct coal gas.Dme is fit to self-igniton engine, is automobile fuel ideal substitute.
At present, the production unit and the manufacturing process of dme are more, wherein common production unit comprises vaporizing puies forward tower, dme rectifying tower and the Dehydration of methanol system of heating up in a steamer, described Dehydration of methanol system and described vaporization are carried and are heated up in a steamer tower and described dme rectifying tower links to each other by pipeline, and the dme rectifying tower has the dme condenser by pipe connection.Described process for preparing dimethyl ether comprise the steps: a, with impurity based on the material benzenemethanol of water be that the mixed solution of main component is carried in vaporization and being heated up in a steamer that vaporization separates the tower from the extraction of dme rectifying tower with the diformazan alcohol and water, send into the Dehydration of methanol system from the methanol steam that cat head comes out, carry from vaporization and heat up in a steamer Tata still still liquid and discharge system continuously.B, described Dehydration of methanol system based on the reactant of dme, first alcohol and water therefrom, the bottom enters the dme rectifying tower, from the required dme product of dme rectifying tower cat head extraction, wherein, the dme steam of dme rectifying tower cat head passes back into described dme rectifying tower after by described dme condenser condenses.Yet above-mentioned existing dme production unit and manufacturing process energy consumption when making dme is higher, and the heat energy of steam condensate, wastewater containing methanol, reaction gas is underutilized.
Summary of the invention
The defective that The present invention be directed to the existence of above-mentioned background technology provides a kind of less energy-consumption dme manufacturing process and production unit thereof, it can make full use of the heat energy of steam condensate, wastewater containing methanol and reaction gas, save heating steam and water coolant, reduced production cost.
For achieving the above object, the invention discloses a kind of less energy-consumption dme production unit, it comprises the methanol preheater that links to each other along order by pipeline, the methyl alcohol well heater, methanol evaporator and flash tank, the top of described flash tank links to each other by the top of pipeline with gas heat exchanger and vaporization tower, the bottom of described flash tank links to each other with first topping-up pump by pipeline, described first topping-up pump links to each other with the vaporization top of tower by pipeline, described gas heat exchanger links to each other with the described reactor and the first vaporization tower reboiler by pipeline, described vaporization tower bottom links to each other with the described first vaporization tower reboiler and the second vaporization tower reboiler by pipeline, described vaporization tower bottom links to each other with the described first vaporization tower reboiler by pipeline, the described vaporization tower bottom and the second vaporization tower reboiler all link to each other with methanol preheater with described methanol evaporator earlier by pipeline again, the described first vaporization tower reboiler links to each other with described methyl alcohol well heater and thick methyl ether preheater earlier by pipeline, described thick methyl ether preheater is by pipeline and thick methyl ether condenser, second topping-up pump and described rectifying tower link to each other, the described thick methyl ether condenser and second topping-up pump all link to each other with described thick methyl ether storage tank by pipeline, wherein, described vaporization tower and rectifying tower are packing tower.
Further, the technology by described dme production unit manufacturing dme comprises the steps:
1., material benzenemethanol at first passes through methanol preheater, the steam condensate of discharging with the waste water and the second vaporization tower reboiler of the discharge of vaporization tower is preheated to 100～140 ℃ to described material benzenemethanol, then the described material benzenemethanol after the preheating is entered the methyl alcohol well heater, with the reaction gas of discharging the material benzenemethanol in the methyl alcohol well heater is heated from reactor, again described material benzenemethanol is entered methanol evaporator, make the liquid-vapor mixture in the methanol evaporator enter flash tank with steam condensate and waste water heating, gas phase in the flash tank enters gas heat exchanger from top exit with the methanol steam of vaporization tower, and the liquid phase in the flash tank enters the vaporization top of tower through first topping-up pump.
2., the gas mixture that comes out of autoreactor is lowered the temperature through gas heat exchanger earlier, reclaim heat energy with the first vaporization tower reboiler and methyl alcohol well heater successively, partial condensation in thick methyl ether preheater then, total condensation in thick methyl ether condenser again, arrive thick methyl ether storage tank at last and separate non-condensable gas, thick methyl ether in the described thick methyl ether storage tank enters thick methyl ether preheater again through second topping-up pump, in the described thick methyl ether preheater thick methyl ether enter the rectifying tower middle and lower part after partly vaporizing, after rectifying, form product.
Further, described steam condensate of discharging from the waste water and the second vaporization tower reboiler of the discharge of vaporization tower is used for the heating of the material benzenemethanol in the described methanol evaporator is made it the part vaporization.
Further, described steam condensate of discharging from the waste water and the second vaporization tower reboiler of the discharge of vaporization tower is earlier to the heating of the material benzenemethanol in the described methanol evaporator, again to the material benzenemethanol preheating in the described methanol preheater.
Further, described reaction gas of discharging from reactor is preheating material methyl alcohol to 220～300 ℃ gas heat exchanger earlier, provide heat for described first vaporization tower reboiler and the methyl alcohol well heater again, arrive described thick methyl ether preheater then and reclaim low grade heat energy, total condensation in thick methyl ether condenser arrives thick methyl ether storage tank at last and separates non-condensable gas.
In sum, dme production unit of the present invention and manufacturing process thereof have following advantage:
1., the present invention increased methanol preheater, methanol evaporator and flash tank, first topping-up pump, and the heat energy of steam condensate, waste water is made full use of.
2., the present invention strengthened thick methyl ether preheater, and thick methyl ether is partly vaporized, and enters rectifying tower with the liquid-vapor mixture state, saves reboiler steam; Reaction gas is partial condensation in thick methyl ether preheater, has reduced thick methyl ether condenser duty, saves recirculated cooling water.
3., vaporize tower and rectifying tower of the present invention be packing tower, can reduce cat head and the tower base pressure is poor, reduces the saturated vapor pressure of material, saves steam.
Description of drawings
Fig. 1 is the schematic diagram of a kind of embodiment of dme production unit of the present invention.
Embodiment
For further understanding feature of the present invention, technique means and the specific purposes that reached, function, the present invention is described in further detail below in conjunction with accompanying drawing and embodiment.
See also Fig. 1, less energy-consumption dme production unit of the present invention comprises methanol preheater 1, methyl alcohol well heater 2, methanol evaporator 3 and the flash tank 4 that links to each other along order by pipeline.The bottom of described flash tank 4 links to each other with first topping-up pump 5 by pipeline, described first topping-up pump 5 links to each other with vaporization tower 6 tops by pipeline, the top of described flash tank 4 links to each other by the top of pipeline with gas heat exchanger 7 and vaporization tower 6, and described vaporization tower 6 is interconnected with described gas heat exchanger 7.
Described gas heat exchanger 7 links to each other with the reactor 8 and the first vaporization tower reboiler 9 by pipeline, and wherein, the top of described reactor 8 all links to each other with gas heat exchanger 7 by pipeline with the bottom.Described vaporization tower 6 bottoms link to each other with the first vaporization tower reboiler 9 and the second vaporization tower reboiler 10 by pipeline, described vaporization tower 6 bottoms link to each other with the described first vaporization tower reboiler 9 by pipeline, connect the form that pipeline formation circulation is communicated with between described vaporization tower 6 and the described first vaporization tower reboiler 9 thereby make.The described vaporization tower 6 and the second vaporization tower reboiler 10 all link to each other with described methanol evaporator 3 earlier by pipeline and link to each other with methanol preheater 1.
In addition, the described first vaporization tower reboiler 9 also links to each other with described methyl alcohol well heater 2 and thick methyl ether preheater 11 earlier by pipeline.Described thick methyl ether preheater 11 links to each other with thick methyl ether condenser 12, second topping-up pump 14 and rectifying tower 15 by pipeline, and the described thick methyl ether condenser 12 and second topping-up pump 14 all link to each other with thick methyl ether storage tank 13 by pipeline.Wherein, described vaporization tower 6 and rectifying tower 15 are packing tower.
The technology of making dme by described dme production unit comprises the steps:
1., material benzenemethanol at first passes through described methanol preheater 1, the steam condensate that the waste water of discharging with vaporization tower 6 and the second vaporization tower reboiler 10 are discharged is preheated to 100～140 ℃ to described material benzenemethanol.Then the described material benzenemethanol after the preheating is entered methyl alcohol well heater 2, use the reaction gas of discharging that the material benzenemethanol in the methyl alcohol well heater 2 is heated, more described material benzenemethanol is entered methanol evaporator 3 from reactor 8.
The steam condensate of discharging from the waste water and the second vaporization tower reboiler 10 of 6 discharges of vaporization tower enters described methanol evaporator 3 by pipeline, and to the material benzenemethanol preheating in the described methanol evaporator 3, make the liquid-vapor mixture in the methanol evaporator 3 enter flash tank 4, gas phase in the flash tank 4 enters gas heat exchanger 7 from top exit with the methanol steam of vaporization tower 6, and the liquid phases in the flash tank 4 enter vaporization tower 6 tops through first topping-up pump 5.Wherein, described waste water of discharging from vaporization tower 6 bottoms enters in the described vaporization tower 6 behind the first vaporization tower reboiler 9 more again, thereby can absorb the heat energy of the material benzenemethanol in the first vaporization tower reboiler 9.
2., the gas mixture that comes out of autoreactor 8 is preheated to 220～300 ℃ at gas heat exchanger 7 earlier, described gas mixture contains dme, methyl alcohol, water and hydrogen etc., provide heat for described first vaporization tower reboiler 9 and the methyl alcohol well heater 2 again, promptly reclaim heat energy with the first vaporization tower reboiler 9 and methyl alcohol well heater 2 successively, partial condensation and reclaim low grade heat energy in thick methyl ether preheater 11 then, total condensation in thick methyl ether condenser 12 arrives thick methyl ether storage tank 13 at last and separates non-condensable gas again.Thick methyl ether in the described thick methyl ether storage tank 13 enters thick methyl ether preheater 11 again through second topping-up pump 14, in the described thick methyl ether preheater 11 thick methyl ether enter rectifying tower 15 middle and lower parts after partly vaporizing, after rectifying, form product.
In sum, dme production unit of the present invention and manufacturing process thereof have following advantage:
1., the present invention increased methanol preheater 1, methanol evaporator 3 and flash tank 4, first topping-up pump 5, and the heat energy of steam condensate, waste water is made full use of.
2., the present invention strengthened thick methyl ether preheater 11, and thick methyl ether is partly vaporized, and enters rectifying tower 15 with the liquid-vapor mixture state, saves reboiler steam; Reaction gas is partial condensation in thick methyl ether preheater 11, has reduced thick methyl ether condenser 12 loads, saves recirculated cooling water.
3., vaporize tower 6 and rectifying tower 15 of the present invention be packing tower, can reduce cat head and the tower base pressure is poor, reduces the saturated vapor pressure of material, saves steam.
The above embodiment has only expressed one embodiment of the present invention, and it describes comparatively concrete and detailed, but can not therefore be interpreted as limitation of the scope of the invention.Should be pointed out that for the person of ordinary skill of the art without departing from the inventive concept of the premise, can also make some distortion and improvement, these all belong to protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with claims.
Claims (5)
1. less energy-consumption dme production unit, it comprises reactor (8) and rectifying tower (15), it is characterized in that: also comprise the methanol preheater (1) that links to each other along order by pipeline, methyl alcohol well heater (2), methanol evaporator (3) and flash tank (4), the top of described flash tank (4) links to each other by the top of pipeline with gas heat exchanger (7) and vaporization tower (6), the bottom of described flash tank (4) links to each other with first topping-up pump (5) by pipeline, described first topping-up pump (5) links to each other with vaporization tower (6) top by pipeline, described gas heat exchanger (7) links to each other with the described reactor (8) and the first vaporization tower reboiler (9) by pipeline, described vaporization tower (6) bottom links to each other with the described first vaporization tower reboiler (9) and the second vaporization tower reboiler (10) by pipeline, described vaporization tower (6) bottom links to each other with the first vaporization tower reboiler (9) by pipeline again, described vaporization tower (6) bottom and the second vaporization tower reboiler (10) all link to each other with methanol preheater (1) with described methanol evaporator (3) earlier by pipeline again, the described first vaporization tower reboiler (9) links to each other with described methyl alcohol well heater (2) earlier by pipeline and links to each other with thick methyl ether preheater (11), described thick methyl ether preheater (11) is by pipeline and thick methyl ether condenser (12), second topping-up pump (14) and described rectifying tower (15) link to each other, described thick methyl ether condenser (12) and second topping-up pump (14) all link to each other with described thick methyl ether storage tank (13) by pipeline, wherein, described vaporization tower (6) and rectifying tower (15) are packing tower.
2. less energy-consumption dme manufacturing process, it comprises the steps:
1., material benzenemethanol at first passes through methanol preheater (1), the steam condensate of discharging with the waste water and the second vaporization tower reboiler (10) of vaporization tower (6) discharge is preheated to 100～140 ℃ to described material benzenemethanol, then the described material benzenemethanol after the preheating is entered methyl alcohol well heater (2), with the reaction gas of discharging the material benzenemethanol in the methyl alcohol well heater (2) is heated from reactor (8), again described material benzenemethanol is entered methanol evaporator (3), make the liquid-vapor mixture in the methanol evaporator (3) enter flash tank (4) with steam condensate and waste water heating, gas phase in the flash tank (4) enters gas heat exchanger (7) from top exit with the methanol steam that vaporization tower (6) comes, and the liquid phase in the flash tank (4) enters vaporization tower (6) top through first topping-up pump (5).
2., the gas mixture that autoreactor (8) comes out is lowered the temperature through gas heat exchanger (7) earlier, reclaim heat energy with the first vaporization tower reboiler (9) and methyl alcohol well heater (2) successively, partial condensation in thick methyl ether preheater (11) then, total condensation in thick methyl ether condenser (12) again, arrive thick methyl ether storage tank (13) at last and separate non-condensable gas, thick methyl ether in the described thick methyl ether storage tank (13) enters thick methyl ether preheater (11) again through second topping-up pump (14), enter rectifying tower (15) middle and lower part after thick methyl ether in the described thick methyl ether preheater (11) is partly vaporized, after rectifying, form product.
3. a kind of less energy-consumption dme manufacturing process according to claim 2, it is characterized in that: described steam condensate of discharging from the waste water and the second vaporization tower reboiler (10) of vaporization tower (6) discharge is used for the heating of the material benzenemethanol in the described methanol evaporator (3) is made it part and vaporizes.
4. a kind of less energy-consumption dme manufacturing process according to claim 2, it is characterized in that: described steam condensate of discharging from the waste water and the second vaporization tower reboiler (10) of vaporization tower (6) discharge heats the material benzenemethanol in the described methanol evaporator (3) earlier, again to the material benzenemethanol preheating in the described methanol preheater (1).
5. according to each described a kind of less energy-consumption dme manufacturing process of claim 2 to 4, it is characterized in that: described reaction gas of discharging from reactor (8) is preheating material methyl alcohol to 220～300 ℃ gas heat exchanger (7) earlier, be that described first vaporization tower reboiler (9) and methyl alcohol well heater (2) provide heat again, arrive described thick methyl ether preheater (11) then and reclaim low grade heat energy, total condensation in thick methyl ether condenser (12) arrives thick methyl ether storage tank (13) at last and separates non-condensable gas.
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| CN2010105327736A CN102010301A (en) | 2010-11-02 | 2010-11-02 | Low-energy-consumption process for producing dimethyl ether and production equipment thereof |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659531A (en) * | 2012-04-19 | 2012-09-12 | 东莞市九丰化工有限公司 | Preparation process system and preparation method for low-energy-consumption dimethyl ether |
| CN103508852A (en) * | 2013-03-26 | 2014-01-15 | 新能(张家港)能源有限公司 | Dimethyl ether energy-saving heating device and method |
| CN103877920A (en) * | 2014-04-11 | 2014-06-25 | 东莞市九丰化工有限公司 | Reaction device for preparing mixed aromatics from methanol |
| CN104058941A (en) * | 2013-03-22 | 2014-09-24 | 泉州恒河化工有限公司 | Method for preparing dimethyl ether by dehydration of methanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US4802956A (en) * | 1986-11-20 | 1989-02-07 | Horst Dornhagen | Process for the purification of dimethylether by distillation |
| CN1125216A (en) * | 1995-10-13 | 1996-06-26 | 化学工业部西南化工研究院 | Method for producing dimethyl ether from methyl alcohol |
| CN101125803A (en) * | 2007-08-17 | 2008-02-20 | 沈建冲 | Preparation method for dimethyl ether |
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2010
- 2010-11-02 CN CN2010105327736A patent/CN102010301A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4802956A (en) * | 1986-11-20 | 1989-02-07 | Horst Dornhagen | Process for the purification of dimethylether by distillation |
| CN1125216A (en) * | 1995-10-13 | 1996-06-26 | 化学工业部西南化工研究院 | Method for producing dimethyl ether from methyl alcohol |
| CN101125803A (en) * | 2007-08-17 | 2008-02-20 | 沈建冲 | Preparation method for dimethyl ether |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659531A (en) * | 2012-04-19 | 2012-09-12 | 东莞市九丰化工有限公司 | Preparation process system and preparation method for low-energy-consumption dimethyl ether |
| CN104058941A (en) * | 2013-03-22 | 2014-09-24 | 泉州恒河化工有限公司 | Method for preparing dimethyl ether by dehydration of methanol |
| CN104058941B (en) * | 2013-03-22 | 2015-11-25 | 黄志忠 | The method of dimethyl ether by methanol dehydration |
| CN103508852A (en) * | 2013-03-26 | 2014-01-15 | 新能(张家港)能源有限公司 | Dimethyl ether energy-saving heating device and method |
| CN103508852B (en) * | 2013-03-26 | 2015-06-03 | 新能(张家港)能源有限公司 | Dimethyl ether energy-saving heating device and method |
| CN103877920A (en) * | 2014-04-11 | 2014-06-25 | 东莞市九丰化工有限公司 | Reaction device for preparing mixed aromatics from methanol |
| CN103877920B (en) * | 2014-04-11 | 2016-03-23 | 东莞市九丰化工有限公司 | Methanol is for the reaction unit of BTX aromatics |
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Application publication date: 20110413 |