CN103508832B - Method for utilizing byproduct ethylene in preparation process of propylene from methanol or dimethyl ether - Google Patents
Method for utilizing byproduct ethylene in preparation process of propylene from methanol or dimethyl ether Download PDFInfo
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- CN103508832B CN103508832B CN201210202454.8A CN201210202454A CN103508832B CN 103508832 B CN103508832 B CN 103508832B CN 201210202454 A CN201210202454 A CN 201210202454A CN 103508832 B CN103508832 B CN 103508832B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention relates to a method for utilizing a byproduct ethylene in a preparation process of propylene from methanol or dimethyl ether. The method comprises the following steps: 1, mixing a C1-C2 component at the tower top of a deethanizer of a methanol or dimethyl ether-to-propylene separating system with a dilution gas to obtain a mixture, heating the mixture to 200-500DEG C, introducing the heated mixture to a C1-C2 component conversion reactor, and converting an effective component ethylene to generate an above C3-baed hydrocarbon component in the C1-C2 component conversion reactor; and 2, cooling a reaction product at an outlet of the C1-C2 component conversion reactor, introducing the cooled reaction product to a gas-liquid separator, evacuating the above obtained gas phase or partially returning the gas phase to the C1-C2 component conversion reactor, and returning the above obtained liquid phase to the separating system of the preparation process of propylene from methanol or dimethyl ether. Compared with the prior art, the method has the advantages of omission of an ethylene deep cooling separating system in present methanol-to-propylene technologies, substantial simplification of the separating system, substantial reduction of the apparatus investment in the preparation process of propylene from methanol or dimethyl ether, improvement of the propylene yield through the C1-C2 component conversion, and increase of the benefit of a methanol or dimethyl ether-to-propylene apparatus.
Description
Technical field
The present invention relates to a kind of recoverying and utilizing method of byproduct ethylene, especially relate to the Application way of a kind of methyl alcohol or dimethyl ether propylene byproduct in process thing ethene.
Background technology
Propylene is a kind of important Organic Chemicals, mainly for the production of polypropylene, vinyl cyanide and vinylformic acid.Current propylene obtains through steam cracking or catalytic cracking primarily of petroleum, and its price affects by oil price.Because petroleum resources are nervous, oil price run at high level, the raw materials cost of production of propylene remains high; In addition, because newly-built steam cracking device many employings light hydrocarbons is if ethane is as raw material, cause ethylene, propylene output ratio unbalance, this more makes propylene shortage, and propylene price is surging.Thus, to develop with main product propylene be target, and propylene production technology has good market outlook, as preparing propylene by dehydrogenating propane and preparing propylene from methanol.Due to domestic propane shortage of resources, methyl alcohol production capacity is seriously superfluous, and methanol prices is cheap.Exploitation preparing propylene from methanol (MTP) technology has more advantage, has wide market outlook and realistic meaning.
At present, industrialized preparing propylene from methanol (MTP) technology adopts multistage insulation formula fixed-bed reactor (WO2006/136433A1, WO2007/140844A1), and catalyzer is the ZSM-5 molecular sieve of modification.Main reactor divides six layers, intersegmental cold shock feed control temperature, and the ethylene component in separation system except propylene product, carbon four loop back reactor to improve the yield (WO2007/04212A1) of propylene to carbon six component.There is a large amount of ethene (being greater than 40% of propone output) steps of Returning reactor after separation system deep cooling in this technological process, due to the boiling point of ethene very low (being-102 DEG C under normal pressure), in system, the partitioning cycle of a large amount of ethene causes separation system compressors energy consumption high, and low temperature separation process cost is high.Therefore, need the technique developing new methyl alcohol or dimethyl ether propylene, avoid a large amount of ethylene synthesis or avoided the circulation of a large amount of ethene by the conversion reaction of ethene.
Chinese patent CN 101177374A discloses a kind of ethene and methyl alcohol coreaction improves the methyl alcohol of Propylene Selectivity or the method for dme generation propylene.The ethylene product that methyl alcohol direct reaction generation olefin hydrocarbon produces by the method and methyl alcohol react, and carry out propylene enhancing.But there is the not high shortcoming of the transformation efficiency of ethene in ethene and methyl alcohol reaction.
Chinese patent CN 101747133A discloses and a kind of ethene in methanol-to-olefins product and butylene methanol to olefins reaction catalyzer is carried out anti-disproportionation reaction generate propylene being different from, and increases propene yield with this.But the anti-disproportionation reaction of ethene and butylene needs high-purity n-butene to do raw material, its application has limitation.
Chinese patent CN 102351629A discloses the patent of preparing propylene from methanol by-product gasoline, is characterised in that and passes through C
4material and methyl alcohol generation etherification reaction or and C
2material generation building-up reactions generates blend gasoline.C in the process
4material and C
2material generation building-up reactions for the production of gasoline, instead of for propylene enhancing.
Summary of the invention
Object of the present invention be exactly in order to overcome above-mentioned prior art exist defect and provide a kind of save a large amount of ethene compression partitioning cycle step and the methyl alcohol of Propylene Selectivity or the Application way of dimethyl ether propylene byproduct in process thing ethene can be improved.
Object of the present invention can be achieved through the following technical solutions: the Application way of a kind of methyl alcohol or dimethyl ether propylene byproduct in process thing ethene, and it is characterized in that, the method comprises the following steps:
(1) by methyl alcohol or dimethyl ether propylene separation system deethanizer overhead C
1-C
2component and diluent gas mix and are heated to 200 ~ 500 DEG C, pass into C
1-C
2component conversion reactor, at C
1-C
2in component conversion reactor, active principle ethylene conversion generates and is mainly C
3above hydrocarbon component;
(2) by C
1-C
2component conversion reactor outlet reaction product passes into gas-liquid separator after cooling, and the emptying or component loops of gas phase returns C
1-C
2component conversion reactor, liquid phase returns the separation system of methyl alcohol or dimethyl ether propylene process.
Described diluent gas is the mixture of one or more compositions in methane, ethane, water vapour, hydrogen or alkane light oil; Diluent gas and C
1-C
2the mass ratio of component is 0 ~ 10.
Described diluent gas and C
1-C
2the mass ratio of component is 0.3 ~ 3.
Described C
1-C
2the temperature of reaction of component conversion reactor is 200 ~ 500 DEG C, and reaction pressure is 0.1 ~ 4MPa; C
1-C
2the mixed gas of component and diluent gas enters C
1-C
2the charging mark state volume space velocity of component conversion reactor counts 500 ~ 10000h with ethene
-1; Described C
1-C
2in component conversion reactor, the transformation efficiency of active principle ethene is 50% ~ 100%, and reaction product is mainly C
3-C
10hydro carbons.
Described C
1-C
2the temperature of reaction of component conversion reactor is 250 ~ 400 DEG C, and reaction pressure is 0.1 ~ 2MPa; Described C
1-C
2the mixed gas of component and diluent gas enters C
1-C
2the charging mark state volume space velocity of component conversion reactor counts 1000 ~ 5000h with ethene
-1.
Described C
1-C
2be filled with catalyzer in component conversion reactor, described catalyzer is ZSM-5 molecular sieve or through the ZSM-5 molecular sieve of modification, amorphous silicic Al catalysts, fixing phosphoric acid catalyst or other types acid molecular sieve catalyst; The silica alumina ratio of described ZSM-5 molecular sieve is 10 ~ 500.
The silica alumina ratio of described ZSM-5 molecular sieve is 50 ~ 200, and grain size is 0.1 ~ 100 micron; The ZSM-5 molecular sieve of described modification modifying element used is one or more in W, Ca, Mg, Fe, P, Ce, and modifying element is 0.01wt% ~ 20wt% relative to the addition of molecular sieve.
Described C
1-C
2component conversion reactor is calandria type fixed bed reactor, and adopt thermal barrier to move heat, thermal barrier is high pressure water, middle setting-out, thermal oil, fused salt or stack gas, and the temperature of thermal barrier is 200 ~ 400 DEG C, thermal barrier temperature and C
1-C
2the temperature difference between component conversion reactor import temperature of reaction is-50 ~ 50 DEG C; Described calandria type fixed bed reactor number is 1 ~ 5.
Described calandria type fixed bed reactor number is 2 ~ 3, loading catalyst between loading catalyst or reaction tubes in the reaction tubes of each calandria type fixed bed reactor, reaction tubes caliber 20 ~ 50mm, reaction tubes pipe range 1 ~ 10m; During described thermal barrier adopts during setting-out, can direct by-product middle pressure steam; When adopting thermal oil or fused salt, by heat exchange byproduct steam.
Described C
1-C
2component conversion reactor outlets products enters gas-liquid separator after interchanger heat exchange cooling, and the product stream temperature entering gas-liquid separator is-10 ~ 90 DEG C, and more excellent temperature is 20 ~ 40 DEG C; Gas-phase product partially draining in gas-liquid separator, component loops returns C
1-C
2component conversion reactor, the gas-phase product of circulation and the molar flow ratio of emptying gas-phase product are 0 ~ 100, and the liquid phase component in gas-liquid separator returns the separation system of methyl alcohol or dimethyl ether propylene.
The ethylene separation circulation that the present invention is directed to the existence of existing MTP industrialized unit causes the problem that sepn process cost is high, energy consumption is high, provides a kind of step saving a large amount of ethene compression partitioning cycle also can improve the technological process of Propylene Selectivity.The scheme that the present invention deals with problems is the C will produced in methyl alcohol or dimethyl ether propylene process
1-C
2component (active principle is ethene) passes through C
1-C
2component conversion reactor changes into C
3above higher hydrocarbons, then return separation system, to increase the yield of propylene.
Compared with prior art, the invention has the beneficial effects as follows:
(1) C
1-C
2hydrocarbon conversion reaction application of installation, in methyl alcohol or dimethyl ether propylene process, can avoid a large amount of ethene to reheat the step looping back methyl alcohol or dimethyl ether propylene reactor through low temperature separation process.Simplify technical process, reduce separating energy consumption.
(2) C
1-C
2hydrocarbon adopts shell and tube reactor, effectively can shift out reaction heat, keeps the stability of catalyzer, and can a small amount of middle pressure steam of by-product.
(3) C is adopted
1-C
2hydrocarbon conversion process, makes part ethylene synthesis high-carbon hydrocarbon, after returning separation system, has reclaimed ethene and has improve the yield of propylene.
Accompanying drawing explanation
Fig. 1 is present invention process schema.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
Accompanying drawing is process flow sheet of the present invention, and in figure, A is heating heat exchanger, and interchanger C, D are water cooler, and B is C
1-C
2hydrocarbon conversion reactor, E is gas-liquid separator, and F is circulating air compressor.
As shown in Figure 1, logistics 1 is the C of methyl alcohol or dimethyl ether propylene process by-product
1-C
2hydrocarbon component raw material, this material and the recycle gas from interchanger C mix, and enter heating heat exchanger A.In heating heat exchanger A, raw material is heated to temperature of reaction and is connected to C by pipeline
1-C
2hydrocarbon conversion reactor B, at C
1-C
2in hydrocarbon conversion reactor B, ethylene component reacts generation higher hydrocarbons.Reactor inlet temperature of reaction is 200 ~ 500 DEG C, and better temperature of reaction is 250 ~ 400 DEG C.Reaction pressure is 0.1 ~ 4MPa, and better pressure is 0.1 ~ 2MPa.Raw material C
1-C
2charging mark state volume space velocity (in ethene) of component is 500 ~ 10000h
-1.Logistics 3 is C
1-C
2the outlets products of hydrocarbon conversion reactor B, mainly containing higher hydrocarbons, this logistics connects interchanger C by pipeline, and in interchanger C and recycle gas heat exchange be cooled, then enter water cooler D be further cooled to gas-liquid separator E be separated required for temperature.In gas-liquid separator E, product is separated into gas-liquid two-phase, and liquid phase stream 4 returns the separation system of methyl alcohol or dimethyl ether propylene, and gaseous stream is divided into 2 strands, is respectively logistics 5 and logistics 6.Logistics 5 is emptying or as fuel gas product, logistics 6 enters compressor F supercharging as reaction cycle gas and enters product gas interchanger C again, through interchanger C heat exchange Posterior circle gas and logistics 2 as periodic off-gases.Logistics 7 and logistics 8 are respectively reactor thermal barrier inlet stream and outlet streams.
Case study on implementation 1 ~ 6 is C
1~ C
2hydro carbons is at C
1~ C
2the embodiment of reacting in hydrocarbon conversion reactor.The present invention includes but be not limited to the range of application that example lifts.
Embodiment 1
Take ZSM-5 as catalyzer, catalyst S i/Al ratio is 10, specific surface area 320m
2/ g, pore volume 0.102ml/g.Using methane as diluent gas, by the by product C in methyl alcohol or dimethyl ether propylene process
1~ C
2component (20wt% and methane 80wt%) inputs calandria type fixed bed reactor, and system response pressure is 4MPa, and ethene mark state air speed is 1000h
-1, in calandria type fixed bed reactor, by the by product C in methyl alcohol or dimethyl ether propylene process
1~ C
2the hydrocarbon conversion is the reactant gases being rich in higher hydrocarbons.Reaction tubes pipe range 10m, internal diameter 20mm.Reaction-ure inlet temperature 200 DEG C, setting-out heat exchange in employing, thermal barrier temperature 220 DEG C, can direct by-product middle pressure steam.
Described calandria type fixed bed reactor number is 1, and calandria type fixed bed reactor is exported reaction product and pass into gas-liquid separator after cooling, gas phase is emptying, and liquid phase returns the separation system of methyl alcohol or dimethyl ether propylene process.
Embodiment 2
Take high silica ZSM-5 as catalyzer, catalyst S i/Al ratio is 500, specific surface area 370m
2/ g, pore volume 0.092ml/g.Take ethane as diluent gas, by the by product C in methyl alcohol or dimethyl ether propylene process
1~ C
2component (90wt% and ethane 10wt%) inputs calandria type fixed bed reactor, system response pressure 0.8MPa, and ethene mark state air speed is 7000h
-1, in calandria type fixed bed reactor, by C
1~ C
2the hydrocarbon conversion is the reactant gases being rich in higher hydrocarbons.Reaction tubes pipe range 6m, internal diameter 50mm.Reaction-ure inlet temperature 350 DEG C, adopts 320 DEG C of thermal oil heat exchange and utilizes high temperature heat conductive oil byproduct steam.
Described calandria type fixed bed reactor number is 5, and calandria type fixed bed reactor outlets products enters gas-liquid separator after interchanger heat exchange cooling, and the product stream temperature entering gas-liquid separator is-10 DEG C; In gas-liquid separator, gas-phase product all circulates and returns C
1-C
2component conversion reactor, the liquid phase component in gas-liquid separator returns the separation system of methyl alcohol or dimethyl ether propylene.
Embodiment 3
Adopt amorphous silicic Al catalysts, catalyst S i/Al ratio is 20, specific surface area 300m
2/ g, pore volume 0.085ml/g.Using methane as diluent gas, by the by product C in methyl alcohol or dimethyl ether propylene process
1~ C
2component (10wt% and methane 90wt%) inputs calandria type fixed bed reactor, reaction pressure 0.1MPa, and ethene mark state air speed is 5000h
-1, close in the calandria type fixed bed reactor of isothermal, by C
1~ C
2the hydrocarbon conversion is the reactant gases being rich in higher hydrocarbons.Reaction tubes pipe range 1m, internal diameter 25mm.Reaction-ure inlet temperature 400 DEG C, adopts fused salt heat exchanging, temperature of molten salt 400 DEG C.
Described calandria type fixed bed reactor number is 2, and calandria type fixed bed reactor outlets products enters gas-liquid separator after interchanger heat exchange cooling, and the product stream temperature entering gas-liquid separator is 90 DEG C; Gas-phase product partially draining in gas-liquid separator, component loops returns C
1-C
2component conversion reactor, the gas-phase product of circulation and the molar flow ratio of emptying gas-phase product are 10, and the liquid phase component in gas-liquid separator returns the separation system of methyl alcohol or dimethyl ether propylene.
Embodiment 4
With the silica gel of load phosphoric acid for solid phosphoric acid catalyst, the charge capacity of phosphoric acid is 5wt%.In calandria type fixed bed reactor, using the gas mixture of methane, ethane and hydrogen as diluent gas, by C
1~ C
2the hydrocarbon conversion is the reactant gases being rich in higher hydrocarbons.Reaction tubes pipe range 6m, internal diameter 35mm.Reaction-ure inlet temperature 300 DEG C, adopts 300 DEG C of thermal oil heat exchange and utilizes high temperature heat conductive oil byproduct steam, reaction pressure 3MPa, and reactor inlet charging is ethene 40%+ methane 20%+ ethane 20%+ hydrogen 20%, and ethene mark state air speed is 500h
-1.
Described calandria type fixed bed reactor number is 3, and calandria type fixed bed reactor outlets products enters gas-liquid separator after interchanger heat exchange cooling, and the product stream temperature entering gas-liquid separator is 20 DEG C; Gas-phase product partially draining in gas-liquid separator, component loops returns C
1-C
2component conversion reactor, the gas-phase product of circulation and the molar flow ratio of emptying gas-phase product are 50, and the liquid phase component in gas-liquid separator returns the separation system of methyl alcohol or dimethyl ether propylene.
Embodiment 5
With the ZSM-5 of P Modification for catalyzer, modifying element phosphorus is 0.01wt%, catalyst S i/Al ratio relative to the addition of molecular sieve is 200, specific surface area 300m
2/ g, pore volume 0.121ml/g.In calandria type fixed bed reactor, by C
1~ C
2the hydrocarbon conversion is the reactant gases being rich in higher hydrocarbons.Reaction tubes pipe range 3m, internal diameter 25mm.Reaction-ure inlet temperature 320 DEG C, adopt 320 DEG C of thermal oil heat exchange and byproduct steam, reaction pressure 0.8MPa, reactor inlet charging is ethene 100%, and ethene mark state air speed is 10000h
-1.
Described calandria type fixed bed reactor number is 4, and calandria type fixed bed reactor outlets products enters gas-liquid separator after interchanger heat exchange cooling, and the product stream temperature entering gas-liquid separator is 40 DEG C; Gas-phase product partially draining in gas-liquid separator, component loops returns C
1-C
2component conversion reactor, the gas-phase product of circulation and the molar flow ratio of emptying gas-phase product are 80, and the liquid phase component in gas-liquid separator returns the separation system of methyl alcohol or dimethyl ether propylene.
Embodiment 6
With the ZSM-5 of Ce modification for catalyzer, modifying element Ce is 20wt%, catalyst S i/Al ratio relative to the addition of molecular sieve is 25, specific surface area 320m
2/ g, pore volume 0.102ml/g.In calandria type fixed bed reactor, by C
1~ C
2the hydrocarbon conversion is the reactant gases being rich in higher hydrocarbons.Reaction tubes pipe range 2m, internal diameter 25mm.Reaction-ure inlet temperature 500 DEG C, adopts 450 DEG C of stack gas heat exchange, reaction pressure 0.1MPa, and reactor inlet charging is ethene 40%+ methane 20%+ water vapor 30%+ hydrogen 10%, and ethene mark state air speed is 5000h
-1.
Calandria type fixed bed reactor outlets products enters gas-liquid separator after interchanger heat exchange cooling, and the product stream temperature entering gas-liquid separator is 30 DEG C; Gas-phase product partially draining in gas-liquid separator, component loops returns C
1-C
2component conversion reactor, the gas-phase product of circulation and the molar weight ratio of emptying gas-phase product are 30, and the liquid phase component in gas-liquid separator returns the separation system of methyl alcohol or dimethyl ether propylene.
The reaction result of embodiment 1 ~ 6 sees the following form:
Table 1
Claims (8)
1. an Application way for methyl alcohol or dimethyl ether propylene byproduct in process thing ethene, it is characterized in that, the method comprises the following steps:
(1) by methyl alcohol or dimethyl ether propylene separation system deethanizer overhead C
1-C
2component and diluent gas mix and are heated to 200 ~ 500 DEG C, pass into C
1-C
2component conversion reactor, at C
1-C
2in component conversion reactor, active principle ethylene conversion generates and is mainly C
3above hydrocarbon component;
(2) by C
1-C
2component conversion reactor outlet reaction product passes into gas-liquid separator after cooling, and the emptying or component loops of gas phase returns C
1-C
2component conversion reactor, liquid phase returns the separation system of methyl alcohol or dimethyl ether propylene process;
Described C
1-C
2the temperature of reaction of component conversion reactor is 200 ~ 500 DEG C, and reaction pressure is 0.1 ~ 4MPa; C
1-C
2the mixed gas of component and diluent gas enters C
1-C
2the charging mark state volume space velocity of component conversion reactor counts 500 ~ 10000h with ethene
-1; Described C
1-C
2in component conversion reactor, the transformation efficiency of active principle ethene is 50% ~ 100%, and reaction product is mainly C
3-C
10hydro carbons;
Described C
1-C
2component conversion reactor is calandria type fixed bed reactor, and adopt thermal barrier to move heat, thermal barrier is high pressure water, middle setting-out, thermal oil, fused salt or stack gas, and the temperature of thermal barrier is 200 ~ 400 DEG C, thermal barrier temperature and C
1-C
2the temperature difference between component conversion reactor import temperature of reaction is-50 ~ 50 DEG C; Described calandria type fixed bed reactor number is 1 ~ 5;
Described C
1-C
2component conversion reactor outlets products enters gas-liquid separator after interchanger heat exchange cooling, and the product stream temperature entering gas-liquid separator is-10 ~ 90 DEG C, and gas-phase product partially draining in gas-liquid separator, component loops returns C
1-C
2component conversion reactor, the gas-phase product of circulation and the molar flow ratio of emptying gas-phase product are 0 ~ 100:1, and the liquid phase component in gas-liquid separator returns the separation system of methyl alcohol or dimethyl ether propylene.
2. the Application way of a kind of methyl alcohol according to claim 1 or dimethyl ether propylene byproduct in process thing ethene, it is characterized in that, described diluent gas is the mixture of one or more compositions in methane, ethane, water vapour, hydrogen or alkane light oil; Diluent gas and C
1-C
2the mass ratio of component is 0 ~ 10.
3. the Application way of a kind of methyl alcohol according to claim 2 or dimethyl ether propylene byproduct in process thing ethene, is characterized in that, described diluent gas and C
1-C
2the mass ratio of component is 0.3 ~ 3.
4. the Application way of a kind of methyl alcohol according to claim 1 or dimethyl ether propylene byproduct in process thing ethene, is characterized in that, described C
1-C
2the temperature of reaction of component conversion reactor is 250 ~ 400 DEG C, and reaction pressure is 0.1 ~ 2MPa; Described C
1-C
2the mixed gas of component and diluent gas enters C
1-C
2the charging mark state volume space velocity of component conversion reactor counts 1000 ~ 5000h with ethene
-1.
5. the Application way of a kind of methyl alcohol according to claim 1 or dimethyl ether propylene byproduct in process thing ethene, is characterized in that, described C
1-C
2be filled with catalyzer in component conversion reactor, described catalyzer is ZSM-5 molecular sieve or through the ZSM-5 molecular sieve of modification, amorphous silicic Al catalysts, fixing phosphoric acid catalyst or other types acid molecular sieve catalyst; The silica alumina ratio of described ZSM-5 molecular sieve is 10 ~ 500.
6. the Application way of a kind of methyl alcohol according to claim 5 or dimethyl ether propylene byproduct in process thing ethene, is characterized in that, the silica alumina ratio of described ZSM-5 molecular sieve is 50 ~ 200, and grain size is 0.1 ~ 100 micron; The ZSM-5 molecular sieve of described modification modifying element used is one or more in W, Ca, Mg, Fe, P, Ce, and modifying element is 0.01wt% ~ 20wt% relative to the addition of molecular sieve.
7. the Application way of a kind of methyl alcohol according to claim 1 or dimethyl ether propylene byproduct in process thing ethene, it is characterized in that, described calandria type fixed bed reactor number is 2 ~ 3, loading catalyst between loading catalyst or reaction tubes in the reaction tubes of each calandria type fixed bed reactor, reaction tubes caliber 20 ~ 50mm, reaction tubes pipe range 1 ~ 10m; During described thermal barrier adopts during setting-out, can direct by-product middle pressure steam; When adopting thermal oil or fused salt, by heat exchange byproduct steam.
8. the Application way of a kind of methyl alcohol according to claim 1 or dimethyl ether propylene byproduct in process thing ethene, is characterized in that, the product stream temperature entering gas-liquid separator is 20 ~ 40 DEG C.
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|---|---|---|---|
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1962573A (en) * | 2006-12-01 | 2007-05-16 | 中国化学工程集团公司 | Method and reactor for catalytic cracking for producing propylene using fluid bed |
| CN101309886A (en) * | 2005-11-14 | 2008-11-19 | 日挥株式会社 | Method for production of lower olefin |
| CN101585747A (en) * | 2009-06-25 | 2009-11-25 | 浙江大学 | Method for transforming oxygenates into propylene |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101309886A (en) * | 2005-11-14 | 2008-11-19 | 日挥株式会社 | Method for production of lower olefin |
| CN1962573A (en) * | 2006-12-01 | 2007-05-16 | 中国化学工程集团公司 | Method and reactor for catalytic cracking for producing propylene using fluid bed |
| CN101585747A (en) * | 2009-06-25 | 2009-11-25 | 浙江大学 | Method for transforming oxygenates into propylene |
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