CN102190546B - Method for preparing propylene and aromatic hydrocarbon by virtue of conversion of methanol - Google Patents
Method for preparing propylene and aromatic hydrocarbon by virtue of conversion of methanol Download PDFInfo
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Abstract
The invention relates to a method for preparing propylene and aromatic hydrocarbon by virtue of conversion of methanol, and the method is mainly used for solving the problem that the methanol is just converted into propylene and the aromatic hydrocarbon can not be co-produced in the prior art. The method comprises the following steps: 1) converting above 80% of methanol into dimethyl ether by virtue of pre-reaction; 2) feeding the generated diamethyl ether and residual methanol into a device for producing propylene from the methanol for reaction so as to obtain a material flow I which mainly comprises the propylene, ethylene and C4, C5, C6 and over-C6 hydrocarbons; 3) after the material flow I is separated, returning the ethylene back to the device for producing the propylene from the methanol for cycling reaction, and feeding C4 and C5 hydrocarbons into an aromatizing device for reaction so as to obtain a material flow II containing aromatic hydrocarbon; and 4) cooling the material flow II, separating a gas-phase product low-carbon hydrocarbons from a liquid-phase product, and separating the liquid product from the material flow I so as to obtain C6 and over-C6 hydrocarbons, mixing, extracting and separating so as to obtain the aromatic hydrocarbon and non-aromatic hydrocarbon. By using the technical scheme, the problem is well solved; and the method can be used in industrialproduction for preparing the ethylene and the aromatic hydrocarbon by virtue of conversion of methanol.
Description
Technical field
The present invention relates to the method for a kind of preparing propylene by methanol transformation and aromatic hydrocarbons.
Background technology
Methyl alcohol is a kind of important Organic Chemicals, is widely used, and the source is abundant, except from biomass, obtaining, coal or Sweet natural gas also are the important source material of producing methyl alcohol, and China has been constructed and put into operation, and how cover is the device of raw material production methyl alcohol with Sweet natural gas, coal, and methanol output strengthens year by year.Planning and construction situation for China's methyl alcohol project, although various statistical information there are differences, but consistent conclusion is in the following short period, the production capacity of methyl alcohol will be considerably beyond actual demand, by 2010, after first large-scale methanol device production capacity discharges, the appearance of methyl alcohol production capacity surplus situation will be inevitable.Carry out methanol conversion technology research, for China's methyl alcohol finds an outlet that reality is feasible, have very important meaning for the development of methanol industry.
In fact, methyl alcohol can transform the most of basic material that obtains petrochemical process, as triolefin (ethene, propylene, divinyl), triphen (benzene,toluene,xylene), also can obtain automotive fuels such as gasoline, diesel oil.American UOP company and Norway Norsk Hydro company have developed methanol conversion alkene processed (MTO) technology cooperatively, in more than 90 day process of operation, methanol conversion is all the time near 100%, the selectivity of ethene and propylene is respectively 55 (mol) % and 27 (mol) %, and can flexible ethene and propylene between ratio (Industrial Catalysis, 2001,9 (4): 3～8).Germany LURGI has developed preparing propylene from methanol (MTP) technology (patent WO2004/018089), its technological principle is ZSM-5 catalyst series and the fixed-bed reactor that utilize modification, propylene one way selectivity is about 35～40%, and the heavy constituent Returning reactor can make propene yield reach 70%.Exxon-Mobil company has developed MTG (methanol conversion gasoline processed) technology and MOGD (methanol conversion petrol and diesel oil processed), wherein the MTG technology of Mobil company exploitation had once been built the commercial apparatus of producing 570000 tons of gasoline per year in New Zealand, and successfully turned round for 10 years.Domestic Dalian Chemistry and Physics Institute has developed DMTO (methanol conversion alkene processed comprises ethene and propylene) technology, has formed independent intellectual property right (ZL99127143).The technology of methanol conversion for preparing arene (MTA) has been developed in the Shanxi coalification, under proper technical conditions, adopts modified molecular sieve catalyst, and the aromatic hydrocarbons total content can reach (CN 1880288A) more than 70% in the liquid hydrocarbon product.
In the existing methanol conversion technology, product structure is single, such as the preparing propylene from methanol technology, can only obtain propylene, and can not coproduction aromatic hydrocarbons; Methyl alcohol aromatic hydrocarbons technology processed can only obtain aromatic hydrocarbons, again can not propylene enhancing, and raw material availability is not high.
The method of preparing propylene by methanol transformation and aromatic hydrocarbons can be in propylene enhancing coproduction aromatic hydrocarbons, improved the utilising efficiency of material benzenemethanol, have tangible economic worth.
Summary of the invention
Technical problem to be solved by this invention be existing preparing propylene by methanol transformation technology can only obtain propylene, can not coproduction aromatic hydrocarbons problem, a kind of new preparing propylene by methanol transformation and the method for aromatic hydrocarbons are provided.This method has when making methyl alcohol can be converted into the propylene of high added value, can also obtain the advantage of aromatic hydrocarbons.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: the method for a kind of preparing propylene by methanol transformation and aromatic hydrocarbons is characterized in that comprising the steps:
(1) with methyl alcohol be raw material, at first carry out pre-reaction, 80% above methanol conversion is dme;
(2) dme of Sheng Chenging and remaining methyl alcohol enter the preparing propylene from methanol device and react, and obtain comprising based on propylene, simultaneously the stream I of ethene, carbon four, carbon five, carbon six and above hydro carbons;
(3) stream I ethene after separating returns the reaction of preparing propylene from methanol reactor cycles; Carbon four, carbon five hydrocarbon enter the aromizing device and continue reaction, obtain containing the stream I I of aromatic hydrocarbons;
(4) stream I I separates the gas-phase product lower carbon number hydrocarbons through overcooling with liquid product, and the carbon six that liquid product and stream I are obtained after separating and above hydrocarbon mix again, through extracting and separating, obtain aromatic hydrocarbons and non-aromatics.
In the technique scheme, used catalyzer is aluminum oxide in the pre-reaction, and temperature of reaction is 200～280 ℃, methyl alcohol weight space velocity 1～4h
-1, reaction pressure 0.05～0.1MPa.The catalyzer that the preparing propylene from methanol reaction is used, comprise following component by weight percentage: (a) HZSM-5 65.0～88.0%; (b) P 0～1.0%; (c) the binding agent silicon oxide 11.0～35.0%.The service temperature of preparing propylene from methanol reaction unit is 420～500 ℃, and working pressure is 0.02～0.08MPa, and the material benzenemethanol weight space velocity is 1～4h
-1The used catalyzer of carbon four carbon five hydrocarbon aromatizings reaction comprises following component by weight percentage: (a) HZSM-5 66.0～86.0%; (b) Ga 0.2～2.0%; (c) the binding agent aluminum oxide 12.0～33.8%.The temperature of reaction of the aromatization of carbon four carbon five hydrocarbon is 500～600 ℃, and reaction pressure is 0.3～0.8MPa, and weight space velocity is 2～5h
-1
Methanol conversion provided by the present invention is the pre-reaction of dme, and its methanol conversion is greater than 80%, and the dme selectivity is near 100%, and methanol conversion can reach 85% under the top condition.
Dme and unconverted methanol mixed that pre-reaction produces enter the preparing propylene from methanol reactor, and methyl alcohol and dimethyl ether conversion rate are greater than 99.5%, and selectivity of product is respectively (methanol quality base): propylene is greater than 32%, and ethene is greater than 13.2%.
After above-mentioned product separated, carbon four carbon five hydrocarbon entered aromizing device, C
6 +The liquid product total recovery is greater than 25% (methanol quality base), and this liquid product mixes with the liquid product that comes out from the preparing propylene from methanol reactor, obtains the aromatic hydrocarbons total recovery greater than 40% (in methanol quality) through separation.
The present invention utilizes the characteristics of preparing propylene from methanol reaction product kind complexity, developed the method for a kind of preparing propylene by methanol transformation and aromatic hydrocarbons, this method adds the reaction unit of carbon four carbon five hydrocarbon aromatizings behind the preparing propylene from methanol reaction unit, after being separated, carbon four carbon five hydro carbons that produce in the preparing propylene from methanol reaction process directly enter aromatization reactor, the liquid product that the liquid product that aromizing is produced and preparing propylene from methanol reaction at last produces merges, adopt the method for extracting and separating, liquid product is separated to obtain aromatic hydrocarbons.Returning reactor again after this method is separated the ethene that produces in the preparing propylene from methanol reaction process has further improved the yield of propylene in the preparing propylene from methanol process, and coproduction aromatic hydrocarbon product.Use method of the present invention, at 230 ℃ of pre-reaction temperature, reaction pressure 0.08MPa, methyl alcohol weight space velocity 2h
-1470 ℃ of preparing propylene from methanol temperature of reaction, reaction pressure 0.05MPa, methyl alcohol weight space velocity 1h
-1Carbon four carbon five hydrocarbon aromatizing temperature of reaction are 560 ℃, and reaction pressure is 0.5MPa, and weight space velocity is 3h
-1Condition under, the transformation efficiency of its material benzenemethanol is 100%, the propylene selectivity can reach 38%, simultaneously the yield of benzene,toluene,xylene BTX aromatics can reach 44% (in methanol quality), has obtained better technical effect.
Description of drawings
Fig. 1 is the process route view of preparing propylene by methanol transformation provided by the invention and aromatic hydrocarbons, wherein 1 is the methanol feedstock pipeline, 2 for methanol conversion be the pre-reactor of dme, 3 is methyl alcohol and dme mixture conduit, and 4 is the water vapour pipeline, and 5 is methyl alcohol, dme, the water vapor mixture pipeline, 6 is the preparing propylene from methanol reactor, 7 is preparing propylene from methanol reaction product pipeline, and 8 is condenser, and 9 is condensed gas-phase product pipeline, 10 is the liquid product pipeline, 11 is knockout tower, and 12 is C1～C2 lighter hydrocarbons pipeline, and 13 is C3～C5 hydrocarbon pipeline, 14 is knockout tower, 15 is product propylene pipeline, and 16 is carbon four carbon five component pipelines, and 17 is the aromatization device, 18 is the aromatization reaction products pipeline, 19 is condenser, and 20 is the gaseous component pipeline, and 21 is the liquid product pipeline, 22 liquid product and aromizing liquid product mixing ducts for the preparing propylene from methanol reaction, 23 is the extracting and separating tower, and 24 is the aromatic hydrocarbons pipeline, and 25 is the non-aromatics pipeline.
Material benzenemethanol enters pre-reactor 2 through piping 1 among Fig. 1, reaction product dme and unreacted methanol are mixed pipeline 5 with the water vapor of coming from pipeline 4 through pipeline 3, enter preparing propylene from methanol reactor 6, the product that comes out from reactor 6 enters condenser 8 through pipeline 7, and condensed product liquid is discharged through pipeline 10.The gas-phase product that flows out from condenser 8 enters knockout tower 11 through pipeline 9, and isolated C1～C2 hydrocarbon is through pipeline 12 and pipeline 5 Returning reactors 6 circulating reactions, and all the other products enter knockout tower 14 through pipeline 13 to be continued to separate.One of target product propylene separates by pipeline 15 from knockout tower to be collected, and residue carbon four carbon five components enter aromatization device 17 through pipeline 16.Reaction product at first enters condenser 19 through pipeline 18, and wherein gaseous component is discharged through pipeline 20, and liquid product flows out from pipeline 21.The liquid phase component that flows out from pipeline 21 with mix from pipeline 10 effluent liquid phase components, enter extracting and separating tower 23 through pipeline 22, isolate aromatic hydrocarbons and non-aromatics, respectively from pipeline 24 and pipeline 25 discharges.
The present invention is further elaborated below by embodiment.
Embodiment
[embodiment 1]
According to technical process shown in Figure 1, material benzenemethanol enters pre-reactor 2 through pipeline 1, and the control reaction conditions: 200 ℃ of temperature of reaction, reaction pressure 0.1MPa, methyl alcohol weight space velocity are 1.0h
-1, this moment, methanol conversion was 80%, dme selectivity 100%.Reaction product dme and unreacted methanol are mixed pipeline 5 with the water vapor of coming from pipeline 4 through pipeline 3, enter preparing propylene from methanol reactor 6, wherein catalyzer consists of 88%HZSM-5,0.02%P, all the other are binding agent, the control reaction conditions is: 420 ℃ of temperature of reaction, reaction pressure 0.02MPa, H
2O/CH
3OH=1.50/1 (quality), methyl alcohol weight space velocity 2.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 33%, ethylene selectivity 13.2%, carbon four carbon five selectivity 38.2%, all the other are mainly liquid product except a small amount of methane ethane.The product that comes out from reactor 6 enters condenser 8 through pipeline 5, and condensed product liquid is discharged through pipeline 10.The gas-phase product that flows out from condenser 8 enters knockout tower 11 through pipeline 9, and isolated C1～C2 hydrocarbon is through pipeline 12 and pipeline 5 Returning reactors 6 circulating reactions, and all the other products enter knockout tower 14 through pipeline 13 to be continued to separate.One of target product propylene separates by pipeline 15 from knockout tower to be collected, residue carbon four carbon five components enter aromatization device 17 through pipeline 16, wherein catalyzer consists of 66%HZSM-5,0.5%Ga, all the other are binding agent, control reaction conditions: 500 ℃ of temperature of reaction, reaction pressure 0.3MPa, weight space velocity 2.0h
-1, reaction product at first enters condenser 19 through pipeline 18, and wherein gaseous component is discharged through pipeline 20, and liquid product flows out from pipeline 21.The liquid phase component that flows out from pipeline 21 with mix from pipeline 10 effluent liquid phase components, enter extracting and separating tower 23 through pipeline 22, isolate aromatic hydrocarbons and non-aromatics, from pipeline 24 and pipeline 25 discharges, wherein aromatic hydrocarbons (BTX) total recovery is 43% (methanol quality base) respectively.
[embodiment 2]
Technical process is with embodiment 1.The pre-reaction condition is: 220 ℃ of temperature of reaction, reaction pressure 0.05MPa, methyl alcohol weight space velocity are 2.0h
-1, this moment, methanol conversion was 82%, dme selectivity 100%.The preparing propylene from methanol catalysts consists of 80%HZSM-5,1.0%P, and all the other are binding agent, 450 ℃ of temperature of reaction, reaction pressure 0.05MPa, H
2O/CH
3OH=1 (quality), methyl alcohol weight space velocity 3.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 34.5%, ethylene selectivity 12%, carbon four carbon five selectivity 36.5%, all the other are mainly liquid product except a small amount of methane ethane.The aromatization catalyzer consists of 70%HZSM-5,0.2%Ga, and all the other are binding agent, 530 ℃ of temperature of reaction, reaction pressure 0.5MPa, weight space velocity 3.0h
-1, obtaining aromatic hydrocarbons (BTX) total recovery is 45% (methanol quality base).
[embodiment 3]
Technical process is with embodiment 1.The pre-reaction condition is: 250 ℃ of temperature of reaction, reaction pressure 0.08MPa, methyl alcohol weight space velocity are 3.0h
-1, this moment, methanol conversion was 84%, dme selectivity 100%.The preparing propylene from methanol catalysts consists of 75%HZSM-5, does not add P, and all the other are binding agent, 480 ℃ of temperature of reaction, reaction pressure 0.08MPa, H
2O/CH
3OH=1.5/1 (quality), methyl alcohol weight space velocity 4.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 36.8%, ethylene selectivity 11.2%, carbon four carbon five selectivity 36%, all the other are mainly liquid product except a small amount of methane ethane.The aromatization catalyzer consists of 75%HZSM-5,1.0%Ga, and all the other are binding agent, 550 ℃ of temperature of reaction, reaction pressure 0.8MPa, weight space velocity 4.0h
-1, obtaining aromatic hydrocarbons (BTX) total recovery is 42% (methanol quality base).
[embodiment 4]
Technical process is with embodiment 1.The pre-reaction condition is: 280 ℃ of temperature of reaction, reaction pressure 0.08MPa, methyl alcohol weight space velocity are 4.0h
-1, this moment, methanol conversion was 83%, dme selectivity 100%.The preparing propylene from methanol catalysts consists of 70%HZSM-5,0.08%P, and all the other are binding agent, 500 ℃ of temperature of reaction, reaction pressure 0.05MPa, H
2O/CH
3OH=1 (quality), methyl alcohol weight space velocity 2.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 32.6%, ethylene selectivity 14.2%, carbon four carbon five selectivity 38%, all the other are mainly liquid product except a small amount of methane ethane.The aromatization catalyzer consists of 80%HZSM-5,2.0%Ga, and all the other are binding agent, 580 ℃ of temperature of reaction, reaction pressure 0.4MPa, weight space velocity 5.0h
-1, obtaining aromatic hydrocarbons (BTX) total recovery is 49%.
[embodiment 5]
Technical process is with embodiment 1.The pre-reaction condition is: 230 ℃ of temperature of reaction, reaction pressure 0.1MPa, methyl alcohol weight space velocity are 2.0h
-1, this moment, methanol conversion was 82%, dme selectivity 100%.The preparing propylene from methanol catalysts consists of 65%HZSM-5,0.5%P, and all the other are binding agent, 500 ℃ of temperature of reaction, reaction pressure 0.05MPa, H
2O/CH
3OH=1 (quality), methyl alcohol weight space velocity 1.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 35.3%, ethylene selectivity 13.6%, carbon four carbon five selectivity 40%, all the other are mainly liquid product except a small amount of methane ethane.The aromatization catalyzer consists of 86%HZSM-5,1.0%Ga, and all the other are binding agent, 600 ℃ of temperature of reaction, reaction pressure 0.5MPa, weight space velocity 4.0h
-1, obtaining aromatic hydrocarbons (BTX) total recovery is 45%.
[embodiment 6]
Technical process is with embodiment 1.The pre-reaction condition is: 250 ℃ of temperature of reaction, reaction pressure 0.1MPa, methyl alcohol weight space velocity are 2.0h
-1, this moment, methanol conversion was 85%, dme selectivity 100%.The preparing propylene from methanol catalysts consists of 60%HZSM-5,0.2%P, and all the other are binding agent, 500 ℃ of temperature of reaction, reaction pressure 0.05MPa, H
2O/CH
3OH=1 (quality), methyl alcohol weight space velocity 1.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 34.3%, ethylene selectivity 13.8%, carbon four carbon five selectivity 43%, all the other are mainly liquid product except a small amount of methane ethane.The aromatization catalyzer consists of 80%HZSM-5,1.0%Ga, and all the other are binding agent, 600 ℃ of temperature of reaction, reaction pressure 0.5MPa, weight space velocity 4.0h
-1, obtaining aromatic hydrocarbons (BTX) total recovery is 46%.
[embodiment 7]
Technical process is with embodiment 1.The pre-reaction condition is: 230 ℃ of temperature of reaction, reaction pressure 0.1MPa, methyl alcohol weight space velocity are 1.0h
-1, this moment, methanol conversion was 84%, dme selectivity 100%.The preparing propylene from methanol catalysts consists of 72%HZSM-5,0.5%P, and all the other are binding agent, 500 ℃ of temperature of reaction, reaction pressure 0.05MPa, H
2O/CH
3OH=1 (quality), methyl alcohol weight space velocity 1.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 36.3%, ethylene selectivity 15.3%, carbon four carbon five selectivity 40%, all the other are mainly liquid product except a small amount of methane ethane.The aromatization catalyzer consists of 80%HZSM-5,1.0%Ga, and all the other are binding agent, 580 ℃ of temperature of reaction, reaction pressure 0.5MPa, weight space velocity 3.0h
-1, obtaining aromatic hydrocarbons (BTX) total recovery is 43%.
[embodiment 8]
Technical process is with embodiment 1.The pre-reaction condition is: 230 ℃ of temperature of reaction, reaction pressure 0.1MPa, methyl alcohol weight space velocity are 1.0h
-1, this moment, methanol conversion was 84%, dme selectivity 100%.The preparing propylene from methanol catalysts consists of 78%HZSM-5,0.5%P, and all the other are binding agent, 480 ℃ of temperature of reaction, reaction pressure 0.05MPa, H
2O/CH
3OH=1 (quality), methyl alcohol weight space velocity 1.0h
-1, this moment methyl alcohol and dimethyl ether conversion rate 100%, propylene selectivity 38.2%, ethylene selectivity 16.3%, carbon four carbon five selectivity 38%, all the other are mainly liquid product except a small amount of methane ethane.The aromatization catalyzer consists of 80%HZSM-5,1.0%Ga, and all the other are binding agent, 550 ℃ of temperature of reaction, reaction pressure 0.3MPa, weight space velocity 3.0h
-1, obtaining aromatic hydrocarbons (BTX) total recovery is 41.5%.
Claims (1)
1. the method for a preparing propylene by methanol transformation and aromatic hydrocarbons comprises the steps:
(1) with methyl alcohol be raw material, at first carry out pre-reaction, 80% above methanol conversion is dme;
(2) dme of Sheng Chenging and remaining methyl alcohol enter the preparing propylene from methanol device and react, and obtain comprising based on propylene, simultaneously the stream I of ethene, carbon four, carbon five, carbon six and above hydro carbons;
(3) stream I ethene after separating returns the reaction of preparing propylene from methanol reactor cycles; Carbon four, carbon five hydrocarbon enter the aromizing device and continue reaction, obtain containing the stream I I of aromatic hydrocarbons;
(4) stream I I separates the gas-phase product lower carbon number hydrocarbons through overcooling with liquid product, and the carbon six that liquid product and stream I are obtained after separating and above hydrocarbon mix again, through extracting and separating, obtain aromatic hydrocarbons and non-aromatics;
Wherein, used catalyzer is aluminum oxide in the pre-reaction, and temperature of reaction is 200～280 ℃, methyl alcohol weight space velocity 1～4h
-1, reaction pressure 0.05～0.1MPa;
Used catalyzer in the preparing propylene from methanol reaction, composed of the following components by weight percentage:
a)HZSM-5 65.0～88.0％；
b)P 0～1.0％；
C) the binding agent silicon oxide 11.0～35.0%;
The service temperature of preparing propylene from methanol reaction unit is 420～500 ℃, and working pressure is 0.02～0.08MPa, and the material benzenemethanol weight space velocity is 1～4h
-1
The catalyzer that carbon four carbon five hydrocarbon aromatizings react used is composed of the following components by weight percentage:
a)HZSM-5 66.0～86.0％；
b)Ga 0.2～2.0％；
C) the binding agent aluminum oxide 12.0～33.8%;
The temperature of reaction of the aromatization of carbon four carbon five hydrocarbon is 500～600 ℃, and reaction pressure is 0.3～0.8MPa, and weight space velocity is 2～5h
-1
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| CN104098418B (en) * | 2013-04-08 | 2016-06-08 | 中石化洛阳工程有限公司 | A kind of aromatization of methanol technique |
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| CN103864561B (en) * | 2014-02-24 | 2015-04-22 | 中国海洋石油总公司 | Technical method for preparing aromatic hydrocarbon through methanol aromatization |
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| CN1151110C (en) * | 2001-02-07 | 2004-05-26 | 北京燕山石油化工公司研究院 | Process for preparing bimethyl ether by catalytic dewatering of methanol |
| DE10233975A1 (en) * | 2002-07-25 | 2004-02-12 | Lurgi Ag | Device for the production of propylene from methanol comprises preferably two or three vertically arranged reaction stages having a form-selective pentasil-type zeolite catalyst with heat exchangers arranged between the stages |
| CN100548945C (en) * | 2006-05-12 | 2009-10-14 | 中国科学院山西煤炭化学研究所 | Process of methanol conversion for preparing arene and catalyzer and method for preparing catalyst |
| CN101607858B (en) * | 2009-07-24 | 2013-07-24 | 中国海洋石油总公司 | Method for preparing aromatic hydrocarbons and propylene simultaneously employing methanol/dimethyl ether |
| CN101602643B (en) * | 2009-07-24 | 2013-07-24 | 中国海洋石油总公司 | Method for preparing ethylene and propylene and co-producing p-xylene through methanol/dimethyl ether conversion |
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| CN102190546A (en) | 2011-09-21 |
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