CN103865563A - Low-energy-consumption method for synthetising gasoline from methanol - Google Patents
Low-energy-consumption method for synthetising gasoline from methanol Download PDFInfo
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- CN103865563A CN103865563A CN201410062713.0A CN201410062713A CN103865563A CN 103865563 A CN103865563 A CN 103865563A CN 201410062713 A CN201410062713 A CN 201410062713A CN 103865563 A CN103865563 A CN 103865563A
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Abstract
The invention discloses a low-energy-consumption method for synthetising gasoline from methanol. The method is characterized by comprising the following steps: entering a raw material methanol into a synthesis oil reactor filled with a catalyst after heat exchange, generating water and hydrocarbons of taking a gasoline component as a main component by transformation under the condition that the liquid hourly space velocity of the methanol at 350-450 DEG C and 0.5-2.0MPa is 0.1-2.0h<-1>; carrying out hydrocarbon-water separation after cooling the reaction product, entering the hydrocarbons into a subsequent cooling separation system; pumping the liquid water to the synthesis oil reactor through a high-temperature pump as medium for entrained reaction heat release. Compared with the existing method for synthetising gasoline from methanol, the low-energy method has the innovation points and advantages that (1) water is taken as the medium for entrained reaction heat release, and a circulating air compressor does not need to be arranged in the system, so that the energy consumption of the system can be greatly reduced; (2) primary purification of the product water can be achieved by circulating reuse, and the subsequent treatment difficulty of the product water is reduced; (3) the reaction product is cooled to 100-200 DEG C by heat exchange, so as to achieve hydrocarbon-water separation. Therefore, the load of the heat exchange unit can be greatly reduced.
Description
Technical field
The invention belongs to methanol derivatives technical field, be specifically related to be a kind of take methyl alcohol as raw material under less energy-consumption condition the method for synthetic gasoline.
Background technology
Methanol synthesized gasoline (MTG) technology is to develop on the methyl alcohol of Mobil company exploitation is converted into the basis of aromatic hydrocarbons on ZSM-5 molecular sieve, by the synthetic gasoline of this technology without sulphur, without nitrogen, olefin(e) centent is low, can be used as high-quality gasoline blend component and use, this technology is significant for China.Because under the drive of coal liquefaction correlative study, domestic coal-based methanol plant investment temperature rises steadily, so that methyl alcohol production capacity increases year by year, and by the end of the end of the year 2012, domestic methyl alcohol production capacity amounts to and reached 5,200 ten thousand tons.But methyl alcohol tradition downstream development of chemical industry is slow, cause the idle production capacity of methyl alcohol constantly to rise, ended for the end of the year 2012, nearly 2,100 ten thousand tons/year of the idle production capacity of methyl alcohol, industry working rate is only 60%.So the deep process technology of exploitation methyl alcohol is extremely urgent.
It is the process of strong heat release that methanol conversion generates hydro carbons, and at 400 ℃, every conversion 1kg methyl alcohol is by heat release 1510～1740kJ, and under adiabatic condition, temperature rise can reach 650 ℃.Therefore, to realize industrialized major project problem be transfer reaction heat how to MTG.Mobil company had developed MTG fixed bed, fluidized-bed and 3 kinds of techniques of shell and tube reactor for this reason once, but this in 3 technique respectively there are relative merits, what obtain so far industrial applications is only fixed-bed process.In fixed-bed process, in order to control the temperature rise of synthetic oil reactor, need to configure large-scale recycle gas compressor, with the C of inertia
1～2hydrocarbon component is medium, a large amount of reaction heat is taken out of, so that system energy consumption is higher.According to statistics, domestic operation, amount to and be about 2,000,000 tons/year at the methyl alcohol of building or dme synthetic gasoline device capbility, what adopt is all fixed-bed process.
In US4404414, Mobil company proposes the parallel connection of synthetic oil reactor, and the circulation gas for controlling temperature of reaction is passed through to each reactor successively, and to reduce the energy consumption of circulation gas, but system still needs configuration cycles air compressor.
CN1923366A has disclosed a kind of single stage method preparing gasoline by methanol novel process, and methyl alcohol directly generates gasoline and liquefied gas through first stage reactor.This technology is researched and developed by Shanxi coalification institute, and obtains Industrial demonstration application in Yunnan coalification group.Compared with two-stage method technique, the technical process of single stage method preparing gasoline by methanol is short, invests lowly, improves thereby the economy of MTG is obtained, but still has the deficiency that recycle gas compressor energy consumption is high.
Summary of the invention
A kind of method that the present invention relates to methanol synthesized gasoline of less energy-consumption, is characterized in that:
Material benzenemethanol enters the synthetic oil reactor of filling HZSM-5 molecular sieve catalyst after heat exchange, 350～450 ℃, volume space velocity is 0.1～2.0h when 0.5～2.0MPa, methanol solution
-1under condition, transform and generate water and the hydro carbons take gasoline component as master, reaction product is after being cooled to 100～200 ℃, carry out the separation of hydrocarbon water, hydro carbons enters follow-up cooling separation, liquid water is sent synthetic oil reactor back to through high-temperature pump, and as the medium that carries exothermic heat of reaction, when the liquid of water and methanol feeding, volume ratio is 1～10;
Processing step comprises:
1) methyl alcohol temperature after heat exchange rises to 330～400 ℃, the synthetic oil reactor that enters filling HZSM-5 molecular sieve catalyst reacts, reaction product temperature after heat exchange is cooling is down to 100～200 ℃, enter hydrocarbon water separator, when wherein the condition of synthetic oil reaction is 350～450 ℃ of temperature, pressure 0.5～2.0MPa, methanol solution, volume space velocity is 0.1～2.0h
-1, synthetic oil reactor adopts fixed bed, moving-bed or fluidized-bed;
2) the water small part obtaining through hydrocarbon water separator enters Sewage treatment systems, and rest part is delivered to interchanger through high-temperature pump, promote temperature to 330～400 ℃ after water enter synthetic oil reactor;
3) hydrocarbon phase obtaining through hydrocarbon water separator obtains fuel gas, liquefied gas, petroleum naphtha component and heavy petrol component through deethanizing column, debutanizing tower, gasoline separation tower after separating.
According to the method described in the present invention, it is characterized in that:
Material benzenemethanol enters the synthetic oil reactor of filling HZSM-5 molecular sieve catalyst after heat exchange, 360～420 ℃, volume space velocity is 0.5～1.8h when 0.8～1.8MPa, methanol solution
-1under condition, transform and generate water and the hydro carbons take gasoline component as master, reaction product is after being cooled to 120～180 ℃, carry out the separation of hydrocarbon water, hydro carbons enters follow-up cooling separation, liquid water is sent synthetic oil reactor back to through high-temperature pump, and as the medium that carries exothermic heat of reaction, when the liquid of water and methanol feeding, volume ratio is 2～6;
Processing step comprises:
1) methyl alcohol temperature after heat exchange rises to 360～380 ℃, the synthetic oil reactor that enters filling HZSM-5 molecular sieve catalyst reacts, reaction product temperature after heat exchange is cooling is down to 120～180 ℃, enter hydrocarbon water separator, when wherein the condition of synthetic oil reaction is 360～420 ℃ of temperature, pressure 0.8～1.8MPa, methanol solution, volume space velocity is 0.5～1.8h
-1, synthetic oil reactor can adopt fixed bed, moving-bed or fluidized-bed;
2) the water small part obtaining through hydrocarbon water separator enters Sewage treatment systems, and rest part is delivered to interchanger through high-temperature pump, promote temperature to 360～380 ℃ after water enter synthetic oil reactor;
3) hydrocarbon phase obtaining through hydrocarbon water separator obtains fuel gas, liquefied gas, petroleum naphtha component and heavy petrol component through deethanizing column, debutanizing tower, gasoline separation tower after separating.
Compared with the method for existing methanol synthesized gasoline, the present invention has following innovative point and advantage: (1), using water as the medium that carries methyl alcohol exothermic heat of reaction, without configuration cycles air compressor, therefore can significantly reduce system energy consumption in system; (2) cyclically utilizing can be realized the rough purification of product water, reduces the subsequent disposal difficulty of product water; (3) reaction product can realize the separation of hydrocarbon water after heat exchange is cooled to 100～200 ℃, therefore can significantly reduce the load of heat exchange unit.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the method for the methanol synthesized gasoline of a kind of less energy-consumption of the present invention: wherein: E-1, E-3 interchanger, E-2 synthesis reactor, E-4 hydrocarbon water separator, E-5 high-temperature pump, E-6 deethanizing column, E-7 debutanizing tower, E-8 gasoline separation tower.
Technological process comprises: methyl alcohol enters E-2 synthetic oil reactor after P-1 enters E-1 heat exchange, and reaction product enters E-4 hydrocarbon water separator after E-3 heat exchange cooling, is separated into water, liquid hydrocarbon and hydrocarbon gas three-phase.Aqueous portion enters Sewage treatment systems through P-2, and rest part returns to synthetic oil reactor after E-5 high-temperature pump, E-3 interchanger.Hydrocarbon gas enters E-6 deethanizing column through P-5, separates and obtains fuel gas and C
3 +hydro carbons, the latter is through P-6 and jointly enter E-7 debutanizing tower from the liquid hydrocarbon of hydrocarbon water separator, separates and obtains liquefied gas and gasoline component, and the latter enters E-8 gasoline separation tower, separates and obtains petroleum naphtha and heavy petrol.
Embodiment
The present invention is further illustrated by the following examples, but content not thereby limiting the invention.
Methyl alcohol is heated to 360 ℃, jointly enter with the recirculated water of 360 ℃ the synthetic oil reactor that loads HZSM-5 molecular sieve catalyst, under 360 ℃, 0.8MPa condition, methanol conversion generates water and the hydro carbons take gasoline component as master, reaction product, after being cooled to 120 ℃, is carried out the separation of hydrocarbon water, and hydro carbons enters follow-up cooling separation, liquid water is sent synthetic oil reactor back to through high-temperature pump, and when methanol solution, volume space velocity is 0.5h
-1, when the liquid of water and methanol feeding, volume ratio is 6, product yield situation is as shown in table 1.
Methyl alcohol is heated to 370 ℃, jointly enter with the recirculated water of 370 ℃ the synthetic oil reactor that loads HZSM-5 molecular sieve catalyst, under 400 ℃, 1.2MPa condition, methanol conversion generates water and the hydro carbons take gasoline component as master, reaction product, after being cooled to 150 ℃, is carried out the separation of hydrocarbon water, and hydro carbons enters follow-up cooling separation, liquid water is sent synthetic oil reactor back to through high-temperature pump, and when methanol solution, volume space velocity is 1.0h
-1, when the liquid of water and methanol feeding, volume ratio is 4, product yield situation is as shown in table 1.
Methyl alcohol is heated to 380 ℃, jointly enter with the recirculated water of 380 ℃ the synthetic oil reactor that loads HZSM-5 molecular sieve catalyst, under 420 ℃, 1.8MPa condition, methanol conversion generates water and the hydro carbons take gasoline component as master, reaction product, after being cooled to 180 ℃, is carried out the separation of hydrocarbon water, and hydro carbons enters follow-up cooling separation, liquid water is sent synthetic oil reactor back to through high-temperature pump, and when methanol solution, volume space velocity is 1.8h
-1, when the liquid of water and methanol feeding, volume ratio is 2, product yield situation is as shown in table 1.
Table 1 methanol synthesized gasoline product yield situation
| Embodiment | Fuel gas/% | Liquefied gas/% | Petroleum naphtha/% | Heavy petrol/% | Water/% | Total/% |
| 1 | 2.5 | 10.1 | 30.2 | 1.0 | 56.2 | 100.0 |
| 2 | 0.8 | 7.8 | 33.1 | 2.1 | 56.2 | 100.0 |
| 3 | 1.4 | 8.5 | 31.4 | 2.5 | 56.2 | 100.0 |
Claims (2)
1. a method for the methanol synthesized gasoline of less energy-consumption, is characterized in that:
Material benzenemethanol enters the synthetic oil reactor of filling HZSM-5 molecular sieve catalyst after heat exchange, 350～450 ℃, volume space velocity is 0.1～2.0h when 0.5～2.0MPa, methanol solution
-1under condition, transform and generate water and the hydro carbons take gasoline component as master, reaction product is after being cooled to 100～200 ℃, carry out the separation of hydrocarbon water, hydro carbons enters follow-up cooling separation, liquid water is sent synthetic oil reactor back to through high-temperature pump, and as the medium that carries exothermic heat of reaction, when the liquid of water and methanol feeding, volume ratio is 1～10;
Processing step comprises:
1) methyl alcohol temperature after heat exchange rises to 330～400 ℃, the synthetic oil reactor that enters filling HZSM-5 molecular sieve catalyst reacts, reaction product temperature after heat exchange is cooling is down to 100～200 ℃, enter hydrocarbon water separator, when wherein the condition of synthetic oil reaction is 350～450 ℃ of temperature, pressure 0.5～2.0MPa, methanol solution, volume space velocity is 0.1～2.0h
-1, synthetic oil reactor adopts fixed bed, moving-bed or fluidized-bed;
2) the water small part obtaining through hydrocarbon water separator enters Sewage treatment systems, and rest part is delivered to interchanger through high-temperature pump, promote temperature to 330～400 ℃ after water enter synthetic oil reactor;
3) hydrocarbon phase obtaining through hydrocarbon water separator obtains fuel gas, liquefied gas, petroleum naphtha component and heavy petrol component through deethanizing column, debutanizing tower, gasoline separation tower after separating.
2. it is characterized in that in accordance with the method for claim 1:
Material benzenemethanol enters the synthetic oil reactor of filling HZSM-5 molecular sieve catalyst after heat exchange, 360～420 ℃, volume space velocity is 0.5～1.8h when 0.8～1.8MPa, methanol solution
-1under condition, transform and generate water and the hydro carbons take gasoline component as master, reaction product is after being cooled to 120～180 ℃, carry out the separation of hydrocarbon water, hydro carbons enters follow-up cooling separation, liquid water is sent synthetic oil reactor back to through high-temperature pump, and as the medium that carries exothermic heat of reaction, when the liquid of water and methanol feeding, volume ratio is 2～6;
Processing step comprises:
1) methyl alcohol temperature after heat exchange rises to 360～380 ℃, the synthetic oil reactor that enters filling HZSM-5 molecular sieve catalyst reacts, reaction product temperature after heat exchange is cooling is down to 120～180 ℃, enter hydrocarbon water separator, when wherein the condition of synthetic oil reaction is 360～420 ℃ of temperature, pressure 0.8～1.8MPa, methanol solution, volume space velocity is 0.5～1.8h
-1, synthetic oil reactor can adopt fixed bed, moving-bed or fluidized-bed;
2) the water small part obtaining through hydrocarbon water separator enters Sewage treatment systems, and rest part is delivered to interchanger through high-temperature pump, promote temperature to 360～380 ℃ after water enter synthetic oil reactor;
3) hydrocarbon phase obtaining through hydrocarbon water separator obtains fuel gas, liquefied gas, petroleum naphtha component and heavy petrol component through deethanizing column, debutanizing tower, gasoline separation tower after separating.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104449797A (en) * | 2014-11-24 | 2015-03-25 | 湖南省馨盛能源开发有限责任公司 | Technological process of methanol-to-gasoline |
| CN105907417A (en) * | 2016-06-21 | 2016-08-31 | 北斗航天软件（北京）有限公司 | Method for preparing high-octane-value gasoline blending components from methyl alcohol |
| CN106795439A (en) * | 2014-10-10 | 2017-05-31 | 埃克森美孚研究工程公司 | From the apparatus and method of oxygenatedchemicals production gasoline, alkene and aromatic compounds |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1923770A (en) * | 2006-09-15 | 2007-03-07 | 中国科学院山西煤炭化学研究所 | Technology of preparing hydrocarbons produce from methanol by one-step method |
| CN101629091A (en) * | 2009-08-14 | 2010-01-20 | 山西恒扬科技有限公司 | Technique for preparing low carbon mixed hydrocarbon rich in propylene and gasoline fraction by methanol |
| US20100044273A1 (en) * | 2008-08-20 | 2010-02-25 | Catalytic Distillation Technologies | Reformate benzene reduction via transalkylation |
| CN102618316A (en) * | 2012-03-12 | 2012-08-01 | 江苏煤化工程研究设计院有限公司 | Technique method for producing oil product and co-producing propylene by utilizing methyl alcohol and mixing fixed bed |
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- 2014-02-24 CN CN201410062713.0A patent/CN103865563A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1923770A (en) * | 2006-09-15 | 2007-03-07 | 中国科学院山西煤炭化学研究所 | Technology of preparing hydrocarbons produce from methanol by one-step method |
| US20100044273A1 (en) * | 2008-08-20 | 2010-02-25 | Catalytic Distillation Technologies | Reformate benzene reduction via transalkylation |
| CN101629091A (en) * | 2009-08-14 | 2010-01-20 | 山西恒扬科技有限公司 | Technique for preparing low carbon mixed hydrocarbon rich in propylene and gasoline fraction by methanol |
| CN102618316A (en) * | 2012-03-12 | 2012-08-01 | 江苏煤化工程研究设计院有限公司 | Technique method for producing oil product and co-producing propylene by utilizing methyl alcohol and mixing fixed bed |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106795439A (en) * | 2014-10-10 | 2017-05-31 | 埃克森美孚研究工程公司 | From the apparatus and method of oxygenatedchemicals production gasoline, alkene and aromatic compounds |
| CN104449797A (en) * | 2014-11-24 | 2015-03-25 | 湖南省馨盛能源开发有限责任公司 | Technological process of methanol-to-gasoline |
| CN105907417A (en) * | 2016-06-21 | 2016-08-31 | 北斗航天软件（北京）有限公司 | Method for preparing high-octane-value gasoline blending components from methyl alcohol |
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Application publication date: 20140618 |