CN103865564A - Integrated method for synthetising gasoline from methyl alcohol or dimethyl ether - Google Patents
Integrated method for synthetising gasoline from methyl alcohol or dimethyl ether Download PDFInfo
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Abstract
The invention discloses an integrated method for synthetising gasoline from methyl alcohol or dimethyl ether. The integrated method is characterized by comprising the following steps: generating hydrocarbons rich in gasoline components from methyl alcohol or dimethyl ether in a synthesis reactor; separating through a flash tank, a gas-liquid separation tank and a fractionating tower to obtain C1-2 hydrocarbons, C3-4 hydrocarbons, light gasoline components, heavy gasoline components and water, wherein the light gasoline components are discharged as products; entering water into a sewage treatment unit; returning C1-2 hydrocarbons to the synthesis reactor after being supersized by a compressor; aromatizing the C3-4 hydrocarbons again, and then directly mixing the product with the heavy gasoline components to enter an alkyl transfer reactor as the raw material; returning the reaction product to the flash tower; discharging a little of C1-2 and heavy gasoline components as byproducts. The integrated method is simple in technological process, and the system is low in energy consumption; on the basis of fed refined methanol, the yield of the gasoline achieves 36-40%; on the basis of the fed dimethyl ether, the yield of the gasoline achieves 50-54%.
Description
Technical field
The invention belongs to methyl alcohol or dme deep process technology field, what be specifically related to is the integrated approach of a kind of methyl alcohol or dme synthetic gasoline.
Background technology
Methyl alcohol or dme synthetic gasoline technology are 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.
In recent years, 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%; On the other hand, due to the restriction of national policy, dme market is since two thousand eight always at a low ebb.Therefore, the deep process technology of exploitation methyl alcohol or dme is extremely urgent.
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, but, by this technology synthetic gasoline time, understand a certain amount of liquefied gas of by-product and the heavy aromatics that is rich in durol, have a strong impact on the economic benefit of enterprise.
US3931349 has disclosed a kind of two-stage method technique of methanol synthesized gasoline, wherein first paragraph is dimethyl ether by methanol dehydration, the mixture of first paragraph methyl alcohol, dme and water out enters second segment reactor, generates liquefied gas and gasoline under ZSM-5 molecular sieve catalyst action.This technological line is the classical preparing gasoline by methanol technique of being developed by Mobil company, Mobil company is in order to promote the economic benefit of yield of gasoline and technique subsequently, a series of improvement technique is proposed again, such as proposing the parallel connection of synthetic oil reactor in US4404414, and the circulation gas for controlling temperature of reaction is passed through to each reactor successively, to reduce the energy consumption of circulation gas; In US4035430, propose the durol cyclically utilizing of by-product, to reduce the growing amount of durol in the reaction process of synthetic gasoline, promote the selectivity of gasoline; In US4423274, propose to adopt fluidized-bed reactor, to promote the selectivity of object product; In US4665249, propose first by the dme separating-purifying in first paragraph dehydration reactor product, and then enter synthetic oil reactor, to promote stability and the yield of gasoline of catalyzer.
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 in patent, does not mention the recycling to the by product such as liquefied gas, heavy aromatics.
CN101787306A has disclosed a kind of refining methanol synthetic oil method and apparatus, by the means such as fractionation, crystallization, methyl alcohol synthetic oil is separated into fuel gas, liquefied gas, treated gasoline and durol.Although can promote the quality of the each product of preparing gasoline by methanol by this technique, flow process complexity, system energy consumption is high.
Summary of the invention
The object of this invention is to provide a kind of less energy-consumption, flow process is simple, and has the methyl alcohol of high yield of gasoline or the integrated approach of dme synthetic gasoline.
The present invention is the integrated approach of a kind of methyl alcohol or dme synthetic gasoline, it is characterized in that:
Methyl alcohol or dme generate the hydro carbons that is rich in gasoline component after synthesis reactor, obtain C through flash tank, knockout drum, separation column after separating
1～2hydro carbons, C
3～4hydro carbons, petroleum naphtha component, heavy petrol component and water, wherein petroleum naphtha component is arranged outward as product, and water enters sewage treatment unit, C
1～2hydro carbons returns to synthesis reactor after compressor supercharging, C
3～4hydro carbons is after aromizing again, and product directly mixes as raw material and enters transalkylation reactor with heavy petrol component, and reaction product is returned to flashing tower, a small amount of C
1～2discharge as by product with heavy petrol component; This Technology has been omitted deethanizing column and debutanizing tower, and C out at the bottom of flashing tower
5 +hydro carbons temperature is 50～300 ℃, can enter separation column without heat exchange or through simple heat exchange; C
3～4after aromatization of hydrocarbons product mixes with heavy petrol component, temperature is 250～400 ℃, can enter transalkylation reactor without heat exchange; The temperature out of transalkylation reactor is 200～450 ℃, after simple heat exchange, can return to flashing tower.Technical process of the present invention is simple, and system energy consumption is low, and take charging refined methanol as benchmark, yield of gasoline reaches 36～40%, and take charging dme as benchmark, yield of gasoline reaches 50～54%.
Processing step comprises:
(1) take HZSM-5 molecular sieve as catalyzer, be 350～450 ℃ in temperature, pressure is 0.5～2.0MPa, raw material WHSV is 0.5～2.5h
-1condition under, methyl alcohol or dme are transformed and generate the hydrocarbon mixture that is rich in gasoline component through synthesis reactor;
(2) reaction product of step (1) enters flashing tower after heat exchange is cooled to 50～300 ℃, is separated into gas-liquid two-phase, and gas phase is C
1～C
4hydro carbons, liquid phase is C
5 +hydro carbons and water;
(3) gas-phase product that step (2) obtains again cooling through heat exchange, separate after obtain C
1～2hydro carbons and C
3～4hydro carbons, the former returns to synthesis reactor through compressor, and the latter enters liquid gas aromatization reaction device, and reaction conditions is 400～600 ℃ of temperature, and pressure is 0.1～2.0MPa, raw material WHSV is 0.1～2.0h
-1, catalyzer adopts the ZSM-5 molecular sieve of one or more modifications in Ga, Zn, Ce, Fe, Ni, Cr, and on catalyzer, total metal content is 0.5～7.0%;
(4) step (2) obtains C
5 +hydro carbons is sent into separation column through heat pump, fractionation obtains petroleum naphtha component and heavy petrol component, heavy petrol component directly enters lighting reactor after mixing with the product of liquid gas aromatization reaction device, reaction product is returned to flashing tower, reaction conditions is 200～450 ℃ of temperature, pressure 1.0～3.0MPa, raw material WHSV is 0.1～2.0h
-1, catalyzer adopts metal-modified Y molecular sieve, and modified metal is one or more in Mo, Co, Ni, La, Ce, and on catalyzer, total metal content is 0.5～7.0%;
According to integrated approach of the present invention, it is characterized in that:
Methyl alcohol or dme generate the hydro carbons that is rich in gasoline component after synthesis reactor, obtain C through flash tank, knockout drum, separation column after separating
1～2hydro carbons, C
3～4hydro carbons, petroleum naphtha component, heavy petrol component and water, wherein petroleum naphtha component is arranged outward as product, and water enters sewage treatment unit, C
1～2hydro carbons returns to synthesis reactor after compressor supercharging, C
3～4hydro carbons is after aromizing again, and product directly mixes as raw material and enters transalkylation reactor with heavy petrol component, and reaction product is returned to flashing tower, a small amount of C
1～2discharge as by product with heavy petrol component.This Technology has been omitted deethanizing column and debutanizing tower, and C out at the bottom of flashing tower
5 +hydro carbons temperature is 80～280 ℃, can enter separation column without heat exchange or through simple heat exchange; C
3～4after aromatization of hydrocarbons product mixes with heavy petrol component, temperature is 300～350 ℃, can enter transalkylation reactor without heat exchange; The temperature out of transalkylation reactor is 250～400 ℃, after simple heat exchange, can return to flashing tower.Technical process of the present invention is simple, and system energy consumption is low, and take charging refined methanol as benchmark, yield of gasoline reaches 37～39%, and take charging dme as benchmark, yield of gasoline reaches 51～53%.
Processing step comprises:
(1) take HZSM-5 molecular sieve as catalyzer, be 380～420 ℃ in temperature, pressure is 1.0～1.8MPa, raw material WHSV is 1.0～2.0h
-1condition under, methyl alcohol or dme are transformed and generate the hydrocarbon mixture that is rich in gasoline component through synthesis reactor;
(2) reaction product of step (1) enters flashing tower after heat exchange is cooled to 80～280 ℃, is separated into gas-liquid two-phase, and gas phase is C
1～C
4hydro carbons, liquid phase is C
5 +hydro carbons and water;
(3) gas-phase product that step (2) obtains again cooling through heat exchange, separate after obtain C
1～2hydro carbons and C
3～4hydro carbons, the former returns to synthesis reactor through compressor, and the latter enters liquid gas aromatization reaction device, and reaction conditions is 450～550 ℃ of temperature, and pressure is 0.1～1.0MPa, raw material WHSV is 0.5～1.5h
-1, catalyzer adopts the ZSM-5 molecular sieve of one or more modifications in Ga, Zn, Ce, Fe, Ni, Cr, and on catalyzer, total metal content is 1.0～6.0%;
(4) step (2) obtains C
5 +hydro carbons is sent into separation column through heat pump, fractionation obtains petroleum naphtha component and heavy petrol component, heavy petrol component directly enters lighting reactor after mixing with the product of liquid gas aromatization reaction device, reaction product is returned to flashing tower, reaction conditions is 250～400 ℃ of temperature, pressure 1.2～2.0MPa, raw material WHSV is 0.5～1.5h
-1, catalyzer adopts metal-modified Y molecular sieve, and modified metal is one or more in Mo, Co, Ni, La, Ce, and on catalyzer, total metal content is 1.0～5.0%;
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the integrated approach of a kind of methyl alcohol of the present invention or dme synthetic gasoline:
Wherein: E-1, E-2, E-4, E-6, E-14 interchanger, E-3 synthetic oil reactor, E-5 flash tank, E-7, E-9 knockout drum, E-10 recycle gas compressor, E-11 liquid gas aromatization reaction device, E-12 gun barrel, E-13 high-temperature pump, E-15 separation column, E-16 lighting reactor.
Technical process is described as follows:
Methyl alcohol or dme, after P-1 enters the gasification of E-1, E-2 interchanger, and are mixed into synthetic oil reactor from the circulation gas of E-4 interchanger, and reaction product enters E-5 flash tank after E-4, the cooling of E-1 interchanger.E-5 gaseous phase materials enters E-7 knockout drum through E-6 interchanger, and E-7 gaseous phase materials enters knockout drum E-9 after E-8 water cooler, and E-7 liquid phase material is discharged through P-4.E-9 gaseous phase materials enters E-6, E-4 interchanger after compressor E-10 supercharging, and E-9 liquid phase material enters liquid gas aromatization reaction device E-11.E-5 flash tank liquid phase material enters gun barrel E-12, and water is arranged and entered Sewage treatment systems outside P-3, and oil phase enters separation column E-15 through E-13 heat pump, E-14 interchanger, and tower top discharging is petroleum naphtha component, the discharging gasoline component of attaching most importance at the bottom of tower.Heavy petrol component enters E-16 lighting reactor after mixing with E-11 reaction product, reaction product is returned to E-1 interchanger, a small amount of C
1～2discharge by P-5, P-6 with heavy petrol component.
Embodiment
Embodiment 1
Raw material adopts refined methanol, and synthetic oil reactor adopts fixed-bed reactor, and reaction conditions is 380 ℃ of temperature, pressure 1.0MPa, methyl alcohol WHSV=1.0h
-1.Liquid gas aromatization reaction device adopts fixed-bed reactor, and reaction conditions is 450 ℃ of temperature, and pressure is 0.5MPa, and raw material WHSV is 1.0h
-1, catalyzer adopts Ga/Ce-ZSM-5 molecular sieve catalyst, and wherein Ga content is that 1.5%, Ce content is 0.5%.Transalkylation reactor adopts fixed-bed reactor, and reaction conditions is 300 ℃ of temperature, pressure 1.2MPa, and raw material WHSV is 1.0h
-1, catalyzer adopts Mo/Ni-Y molecular sieve catalyst, and wherein Mo content is that 1.5%, Ni content is 1.0%.Under above processing condition, at the bottom of E-5 flashing tower, drop temperature is 130 ℃, after simple heat exchange, can enter E-15 separation column, after E-11 aromatization reactor product mixes with the discharging of E-15 Fractionator Bottom, temperature is 300 ℃, can enter E-16 transalkylation reactor without heat exchange, E-16 product can return to E-5 through simple heat exchange cooling.The yield (take methyl alcohol as base, lower same) of each product is as shown in table 1.
Embodiment 2
Raw material adopts refined methanol, and synthetic oil reactor adopts moving-burden bed reactor, and reaction conditions is 400 ℃ of temperature, pressure 1.5MPa, methyl alcohol WHSV=1.5h
-1.Liquid gas aromatization reaction device adopts moving-burden bed reactor, and reaction conditions is 500 ℃ of temperature, and pressure is 0.2MPa, and raw material WHSV is 0.8h
-1, catalyzer adopts Ga/Fe-ZSM-5 molecular sieve catalyst, and wherein Ga content is that 3.0%, Fe content is 2.0%.Transalkylation reactor adopts fixed-bed reactor, and reaction conditions is 320 ℃ of temperature, pressure 1.8MPa, and raw material WHSV is 0.7h
-1, catalyzer adopts Mo/La-Y molecular sieve catalyst, and wherein Mo content is that 3.0%, La content is 0.3%.Under above processing condition, at the bottom of E-5 flashing tower, drop temperature is 150 ℃, after simple heat exchange, can enter E-15 separation column, after E-11 aromatization reactor product mixes with the discharging of E-15 Fractionator Bottom, temperature is 320 ℃, can enter E-16 transalkylation reactor without heat exchange, E-16 product can return to E-5 after simple heat exchange cooling.The yield of each product is as shown in table 1.
Embodiment 3
Raw material adopts dme, and synthetic oil reactor adopts fluidized-bed reactor, and reaction conditions is 420 ℃ of temperature, pressure 1.8MPa, methyl alcohol WHSV=2.0h
-1.Liquid gas aromatization reaction device adopts fluidized-bed reactor, and reaction conditions is 550 ℃ of temperature, and pressure is 0.2MPa, and raw material WHSV is 1.5h
-1, catalyzer adopts Ga/Zn-ZSM-5 molecular sieve catalyst, and wherein Ga content is that 3.0%, Zn content is 1.0%.Transalkylation reactor adopts fixed-bed reactor, and reaction conditions is 340 ℃ of temperature, pressure 2.0MPa, and raw material WHSV is 1.2h
-1, catalyzer adopts Mo/Co-Y molecular sieve catalyst, and wherein Mo content is that 3.0%, Co content is 2.0%.Under above processing condition, at the bottom of E-5 flashing tower, drop temperature is 170 ℃, after simple heat exchange, can enter E-15 separation column, after E-11 aromatization reactor product mixes with the discharging of E-15 Fractionator Bottom, temperature is 340 ℃, can enter E-16 transalkylation reactor without heat exchange, E-16 product can return to E-5 after simple heat exchange cooling.The yield of each product is as shown in table 1.
Table 1 methanol/dimethyl ether is produced the product composition of gasoline integrated approach
Claims (2)
1. an integrated approach for methyl alcohol or dme synthetic gasoline, is characterized in that:
Methyl alcohol or dme generate the hydro carbons that is rich in gasoline component after synthesis reactor, obtain C through flash tank, knockout drum, separation column after separating
1～2hydro carbons, C
3～4hydro carbons, petroleum naphtha component, heavy petrol component and water, wherein petroleum naphtha component is arranged outward as product, and water enters sewage treatment unit, C
1～2hydro carbons returns to synthesis reactor after compressor supercharging, C
3～4hydro carbons is after aromizing again, and product directly mixes as raw material and enters transalkylation reactor with heavy petrol component, and reaction product is returned to flashing tower, a small amount of C
1～2discharge as by product with heavy petrol component;
Processing step comprises:
1) take HZSM-5 molecular sieve as catalyzer, be 350～450 ℃ in temperature, pressure is 0.5～2.0MPa, raw material WHSV is 0.5～2.5h
-1condition under, methyl alcohol or dme are transformed and generate the hydrocarbon mixture that is rich in gasoline component through synthesis reactor;
2) reaction product of step 1) enters flashing tower after heat exchange is cooled to 50～300 ℃, is separated into gas-liquid two-phase, and gas phase is C
1～C
4hydro carbons, liquid phase is C
5 +hydro carbons and water;
3) step 2) gas-phase product that obtains again cooling through heat exchange, obtain C after separating
1～2hydro carbons and C
3～4hydro carbons, the former returns to synthesis reactor through compressor, and the latter enters liquid gas aromatization reaction device, and reaction conditions is 400～600 ℃ of temperature, and pressure is 0.1～2.0MPa, raw material WHSV is 0.1～2.0h
-1, catalyzer adopts the ZSM-5 molecular sieve of one or more modifications in Ga, Zn, Ce, Fe, Ni, Ce, and on catalyzer, total metal content is 0.5～7.0%;
4) step 2) obtain C
5 +hydro carbons is sent into separation column through heat pump, fractionation obtains petroleum naphtha component and heavy petrol component, heavy petrol component directly enters lighting reactor after mixing with the product of liquid gas aromatization reaction device, reaction product is returned to flashing tower, reaction conditions is 200～450 ℃ of temperature, pressure 1.0～3.0MPa, raw material WHSV is 0.1～2.0h
-1, catalyzer adopts metal-modified Y molecular sieve, and modified metal is one or more in Mo, Co, Ni, La, Ce, and on catalyzer, total metal content is 0.5～7.0%.
2. it is characterized in that in accordance with the method for claim 1:
Methyl alcohol or dme generate the hydro carbons that is rich in gasoline component after synthesis reactor, obtain C through flash tank, knockout drum, separation column after separating
1～2hydro carbons, C
3～4hydro carbons, petroleum naphtha component, heavy petrol component and water, wherein petroleum naphtha component is arranged outward as product, and water enters sewage treatment unit, C
1～2hydro carbons returns to synthesis reactor after compressor supercharging, C
3～4hydro carbons is after aromizing again, and product directly mixes as raw material and enters transalkylation reactor with heavy petrol component, and reaction product is returned to flashing tower, a small amount of C
1～2discharge as by product with heavy petrol component;
Processing step comprises:
1) take HZSM-5 molecular sieve as catalyzer, be 380～420 ℃ in temperature, pressure is 1.0～1.8MPa, raw material WHSV is 1.0～2.0h
-1condition under, methyl alcohol or dme are transformed and generate the hydrocarbon mixture that is rich in gasoline component through synthesis reactor;
2) reaction product of step 1) enters flashing tower after heat exchange is cooled to 80～280 ℃, is separated into gas-liquid two-phase, and gas phase is C
1～C
4hydro carbons, liquid phase is C
5 +hydro carbons and water;
3) step 2) gas-phase product that obtains again cooling through heat exchange, obtain C after separating
1～2hydro carbons and C
3～4hydro carbons, the former returns to synthesis reactor through compressor, and the latter enters liquid gas aromatization reaction device, and reaction conditions is 450～550 ℃ of temperature, and pressure is 0.1～1.0MPa, raw material WHSV is 0.5～1.5h
-1, catalyzer adopts the ZSM-5 molecular sieve of one or more modifications in Ga, Zn, Ce, Fe, Ni, Ce, and on catalyzer, total metal content is 1.0～6.0%;
4) step 2) obtain C
5 +hydro carbons is sent into separation column through heat pump, fractionation obtains petroleum naphtha component and heavy petrol component, heavy petrol component directly enters lighting reactor after mixing with the product of liquid gas aromatization reaction device, reaction product is returned to flashing tower, reaction conditions is 250～400 ℃ of temperature, pressure 1.2～2.0MPa, raw material WHSV is 0.5～1.5h
-1, catalyzer adopts metal-modified Y molecular sieve, and modified metal is one or more in Mo, Co, Ni, La, Ce, and on catalyzer, total metal content is 1.0～5.0%.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105013528A (en) * | 2015-07-24 | 2015-11-04 | 麦森能源科技有限公司 | Composite molecular sieve catalyst for preparation of gasoline from methanol and preparation method thereof |
| CN107206365A (en) * | 2015-01-22 | 2017-09-26 | 托普索公司 | For converting methanol into the method for being suitable as gasoline or mixed material |
| CN112375583A (en) * | 2020-10-27 | 2021-02-19 | 湖南红宝科技开发有限公司 | Method and device for preparing gasoline by taking methanol as raw material |
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| 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 |
| US20110152594A1 (en) * | 2009-12-11 | 2011-06-23 | Exxonmobil Research And Engineering Company | Process and system to convert methanol to light olefin, gasoline and distillate |
| CN102146010A (en) * | 2010-02-10 | 2011-08-10 | 江苏煤化工程研究设计院有限公司 | Process for producing low carbon olefin and arene parallel cogeneration gasoline by using methanol as raw material |
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2014
- 2014-02-24 CN CN201410062786.XA patent/CN103865564B/en active Active
Patent Citations (3)
| 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 |
| US20110152594A1 (en) * | 2009-12-11 | 2011-06-23 | Exxonmobil Research And Engineering Company | Process and system to convert methanol to light olefin, gasoline and distillate |
| CN102146010A (en) * | 2010-02-10 | 2011-08-10 | 江苏煤化工程研究设计院有限公司 | Process for producing low carbon olefin and arene parallel cogeneration gasoline by using methanol as raw material |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107206365A (en) * | 2015-01-22 | 2017-09-26 | 托普索公司 | For converting methanol into the method for being suitable as gasoline or mixed material |
| CN105013528A (en) * | 2015-07-24 | 2015-11-04 | 麦森能源科技有限公司 | Composite molecular sieve catalyst for preparation of gasoline from methanol and preparation method thereof |
| CN112375583A (en) * | 2020-10-27 | 2021-02-19 | 湖南红宝科技开发有限公司 | Method and device for preparing gasoline by taking methanol as raw material |
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