CN101239871B

CN101239871B - Method for increasing selectivity of low-carbon olefins in methanol or dimethyl ether converting process

Info

Publication number: CN101239871B
Application number: CN2007100372343A
Authority: CN
Inventors: 谢在库; 齐国祯; 杨为民; 钟思青
Original assignee: China Petroleum and Chemical Corp; Sinopec Shanghai Research Institute of Petrochemical Technology
Current assignee: China Petroleum and Chemical Corp; Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date: 2007-02-07
Filing date: 2007-02-07
Publication date: 2011-05-18
Anticipated expiration: 2027-02-07
Also published as: CN101239871A

Abstract

The invention relates to a method for improving the selectivity of ethylene and propylene during methanol or dimethyl ether conversion process, which mainly solves the problem of the prior art, such as low selectivity of lower olefins. The invention uses methanol or dimethyl ether as the material, comprises steps that: a) the material enters into a reaction region from the bottom of a first fluidization bed reactor to be contacted with the catalyst, thereby generating an effluent 1 containing ethylene and propylene, the effluent 1 is separated to obtain ethylene and propylene; b) the catalyst after reaction in the first fluidization bed enters into the bottom of a second fluidization bed reactor, and contact and react with the methanol material to generate an effluent 2 containing dimethyl ether, the effluent 2 is back the first fluidization bed reactor to feed, and the reacted catalyst to be regenerated is regenerated after entering into a lower generation region of a reactor; c) the generated catalyst is back to the lower reaction region of the first fluidization bed reactor. Accordingly, the invention solves the problem well and is useful in industrial production of lower olefins.

Description

Improve the method for selectivity of light olefin in methyl alcohol or the dimethyl ether conversion process

Technical field

The present invention relates to improve in a kind of methyl alcohol or the dimethyl ether conversion process method of selectivity of light olefin.

Technical background

Low-carbon alkene is defined as ethene and propylene here, is two kinds of important basic chemical industry raw materials, and its demand is in continuous increase.Ethene, propylene mainly are to make by petroleum path traditionally, but because limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people begin to greatly develop the substitute energy transformation technology, and as the technology of oxygen-containing compound conversion to produce olefine (OTO), oxygenatedchemicals comprises methyl alcohol, ethanol, dme, methyl ethyl ether, methylcarbonate etc.Have many technology to can be used to produce oxygenatedchemicals, raw material comprises coal, Sweet natural gas, biomass etc.Wherein, methyl alcohol is one of large Essential Chemistry product, is the preferred oxides of producing low-carbon alkene, generally by hydrogen, CO and/or CO ₂In the presence of heterogeneous catalyst, in methanol sythesis reactor, carry out catalyzed reaction production, for example use copper/zinc oxide catalyzer in tubular reactor, to become to produce methyl alcohol.

Announced among the US6166282 that a kind of oxygenate conversion is the technology and the reactor of low-carbon alkene, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu reaction of gas speed is finished, after rising to the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Because reaction after product gas and catalyzer sharp separation have effectively prevented the generation of secondary reaction.Through analog calculation, to compare with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all significantly reduce.

Announced among the CN1723262 that it is low-carbon alkene technology that the multiple riser reaction unit that has central catalyst return is used for oxygenate conversion, this covering device comprises a plurality of riser reactors, gas solid separation district, a plurality of offset components etc., each riser reactor has the port of injecting catalyst separately, be pooled to the disengaging zone of setting, catalyzer and product gas are separated.

In the conversion process of low-carbon alkene, can not expect the by product that obtains at methyl alcohol, particularly not expect to obtain number of C because side reaction generates ₁Material.C described in the present invention ₁Material mainly is meant CH ₄, CO, CO ₂Wherein, CO is mainly derived from the decomposition of methyl alcohol, the generation of hydrogen is arranged simultaneously, CO ₂Mainly be to be come by water gas shift reaction by CO, and methane is except subsidiary generate that part of in the methoxyl group generative process, other also comes from the decomposition of methyl alcohol.These C ₁The generation of by product, except needs increase by product from desired alkene the isolating investment, also greatly reduce the effective rate of utilization of carbon back in the methanol molecules, and then reduced the selectivity of low-carbon alkene, therefore, wish to reduce the generation of these by products as far as possible, improve the selectivity of low-carbon alkene.

JP01090136 relates to a kind of by the sulfuration of reactor metal surface being avoided the method for the decomposition of methyl alcohol, this method is included under the catalyzer existence condition in more than 450 ℃ methyl alcohol being reacted in the tubular reactor of being made by iron and/or nickel or stainless steel, reactor wall uses the compound such as dithiocarbonic anhydride, disulfides other than hydrogen or dimethyl thioether to vulcanize, and also sulfide can be joined in the charging.This method inevitably can be brought some impurity into, need separate from product.

CN1662477 is by a kind of nozzle material-feeding of design system, and the temperature of the method control feed system of employing isulating jacket or cooling system, thereby reaches the degree of decomposing in the control methanol feeding.But this method does not relate to the problem that methyl alcohol decomposes in reactor.

Though method described in the above-mentioned document can reduce the probability of methanolysis to a certain extent, all do not relate to the thermolysis problem of methyl alcohol, therefore all there is the lower problem of selectivity of light olefin.Need a kind of method can further reduce C ₁The generation of by product, the selectivity of raising low-carbon alkene.

Summary of the invention

Technical problem to be solved by this invention is the lower problem of selectivity of light olefin that exists in the prior art, and a kind of method of new raising selectivity of light olefin is provided.This method is used for the industrial production of methyl alcohol or dimethyl ether conversion production low-carbon alkene, has C ₁The by product selectivity is low, the selectivity of light olefin advantage of higher.

For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method that improves selectivity of light olefin in methyl alcohol or dimethyl ether conversion process, may further comprise the steps: a) mixture with methyl alcohol or methyl alcohol and dme is a raw material, raw material enters reaction zone from first fluidized bed reactor bottom, generate the effluent 1 that contains ethene, propylene with the catalyzer contact reacts, obtain ethene, propylene through separation; B) treat that the regenerated catalyzer enters the second fluidized-bed reactor bottom, generate the logistics 2 that contains dme with the methanol feedstock contact reacts, logistics 2 turns back to first fluidized bed reactor feed, and reacted reclaimable catalyst enters breeding blanket, revivifier bottom and regenerates; C) catalyzer after the regeneration returns first fluidized bed reactor lower part reaction zone.

In the technique scheme, reacted the treat regenerated catalyst of the catalyzer preferred version in second fluidized-bed reactor for from the first class bed bioreactor, transporting; The catalyzer preferred version with low green coke amount that comes out from the first class bed bioreactor is without stripping, directly enters second fluidized-bed reactor; Logistics 2 preferred versions are for entering from the bottom sparger or entering first fluidized bed reactor reaction zone from least one inlet that reaction zone is in axial direction gone up; First class bed bioreactor preferred version is a fast fluidized bed, and the second fluidized-bed reactor preferred version is a fast fluidized bed, and the revivifier preferred version is a dense phase fluidized bed; The temperature of reaction of first class bed bioreactor is 350～600 ℃, and preferred version is 425～500 ℃, and the raw material weight air speed is 0.1～100 hour ^-1, preferred version is 1.0～20 hours ^-1, in the reaction pressure 0～1MPa of gauge pressure, preferred version is 0.1～0.3MPa; Temperature of reaction in second fluidized-bed reactor is 200～400 ℃, and preferred version is 260～320 ℃, and the raw material weight air speed is 0.1～100 hour ^-1, preferred version is 1～20 hour ^-1Catalyzer all is selected from SAPO type molecular sieve catalyst in first class bed bioreactor, second fluidized-bed reactor, and preferred version all is selected from the molecular sieve catalyst into SAPO-34.

General main methyl alcohol, dme, the water of comprising before entering first reactor, can be selected non-imposed a part of water is removed in the second reactor outlet logistics, improves the dividing potential drop of second reactor feed.The feed state of first reactor can be liquid, can be gaseous state also, is preferably gaseous state.The all right non-imposed common charging of a certain proportion of thinner of interpolation in first reactor feed, thinner can be low-carbon alkanes (methane, ethane, propane etc.), low-carbon alcohol (methyl alcohol, ethanol, n-propyl alcohol, Virahol, propyl carbinol, isopropylcarbinol etc.), CO, nitrogen, water vapour, C4 hydrocarbon, mononuclear aromatics etc., wherein, preferred low-carbon alkanes, low-carbon alcohol, water vapour, more preferably low-carbon alcohol, water vapour, most preferably scheme is a water vapour, and the amount of thinner and the volume ratio of raw material are 0.1～10: regulate in 1 scope.

The bottom feed mouth position of first class bed bioreactor, second fluidized-bed reactor, revivifier generally is positioned at bed reaction zone bottom, and raw material enters reaction zone by gas distribution grid, nozzle or sparger.Can change in the larger context along the inlet position on the reaction zone axial direction due, generally the position in close bottom feed district below the reaction zone mid-way.Reaction product and catalyzer are deposited to reactor settling section bottom after gas-solid quickly separating, cyclonic separation, density of catalyst herein is higher, have two discharge ports in the position of settling section bottom 1/8～1/4 settling section height, part catalyzer turns back to the reaction zone bottom by a discharge port, to guarantee required raw material weight air speed or bed catalyst activity levels; Some catalyzer enters 1/10～1/5 reaction zone height place, reaction zone bottom of second fluidized-bed reactor by another discharge port through pipeline, contacts with methyl alcohol and reacts.Settling section at second fluidized-bed reactor, feed water vapour catalyzer is carried out stripping, the regenerated catalyst for the treatment of behind the stripping is regenerated through the height place, 1/10～1/5 breeding blanket, bottom, breeding blanket that pipeline enters revivifier by opening at the discharge port of settling section bottom 1/8～1/4 settling section height location, and the catalyzer after the regeneration turns back to the reaction zone bottom by the discharge port of opening at revivifier settling section bottom 1/8～1/4 settling section height location through pipeline.

Known in the field, be the reaction of low-carbon alkene for adopting the SAPO-34 molecular sieve catalyst with methyl alcohol or dimethyl ether conversion, contain the raising that certain carbon deposit will help selectivity of light olefin on the catalyzer.In first reactor, the average coke content of catalyzer should under this catalyst activity levels, can reach higher selectivity of light olefin between 3%～6% (weight).The average coke content of catalyzer that enters second reactor generally between 4～8% (weight), under this catalyst activity levels, under lower temperature of reaction, can be realized the conversion of methyl alcohol to dme.In revivifier, can adopt method known in the field to control the degree of making charcoal, as the oxygen concn in the control regenerating medium, recovery time, regeneration temperature etc.

The feed entrance point of first reactor enters the reaction zone except the sparger through reactor bottom, also can enter reaction zone from the one or more inlets on the reaction zone axial location, this feed process can play effect same when adding thinner, thereby can improve selectivity of light olefin.The number of inlet can change in a big way on the reaction zone axial direction due, but too much inlet not only can increase the complicacy of equipment, and be inconvenient to keep in repair, more even can have influence on the flow behavior of gas-solid in the reaction zone, in addition, inlet increases to a certain degree, and conversion of raw material may be reduced to the level that difficulty or ease are accepted, and the increment that selectivity of light olefin improves descends.Therefore, should be under the acceptable level, the quantity and the position of inlet rationally is set at feed stock conversion.The injection rate of reactant can be identical in each inlet, also can be different, and this does not limit in the present invention.Those of ordinary skill in the art should be able to adjust various operating parameterss and condition, so that use conventional experience to make low-carbon alcohol transformation efficiency, olefine selective optimization.

The carbonaceous material that reaction generates in this method is as CO _x, methane, ethene, ethane, propylene, propane, DME, C ₄, C ₅ ⁺Deng, can adopt separation method known in the field to separate.

For methanol-to-olefins (MTO) reaction of adopting the SAPO-34 molecular sieve catalyst, increase along with the reaction times, coke content on the catalyzer increases, when yield of light olefins is quite low, conversion of methanol can not drop to zero in long period of time, its reason is to exist because methanol conversion generates the reaction of dme, the increase that is catalyzer coke content has covered more acid sites, stopped up more duct, but methyl alcohol still can be in more weak acidity of catalyst in the heart and the outside surface of catalyzer change into dme.Known in the field, the coking yield of SAPO-34 catalyzer is lower in the MTO technology, and coking yield is less than 3% (weight).Therefore, the catalyzer that utilization of the present invention is reacted in first reactor, the green coke amount is lower is the mixture that contains dme with methanol conversion in second reactor.In addition, the decaying catalyst in first reactor directly enters second reactor without stripping, and the heat of taking out of can be used for the conversion of methyl alcohol to dme.

Calculation of thermodynamics shows that with respect to methyl alcohol, the dme thermolysis needs higher energy, in other words, is exactly under the certain reaction condition, compares the difficult generation thermolysis of dme with methyl alcohol.In addition, because methanol conversion is that temperature of reaction is lower in the reactor of dme, the decomposition probability of methyl alcohol is very low.And all or part of being converted into of methyl alcohol entered the reactor of producing alkene behind the dme, because methanol concentration is lower, it is bigger that dme decomposes difficulty, so just fundamentally further reduced C in the reaction system ₁The generation probability of by product has improved the selectivity of low-carbon alkene.

In addition, the method for the invention is except reducing C ₁The generation of by product reaches outside the purpose that improves selectivity of light olefin, also has following advantage: (1) is that the exothermic heat of reaction amount of alkene is scattered in two reactors with methanol conversion, has significantly reduced the thermal load of first reactor; (2) be that the water-dispersion that generates in the olefin hydrocarbon is in two reactors with methanol conversion, can select the portion water in the second reactor outlet logistics is removed, effectively reduce the water yield in first reactor, both reduced the load of first reactor and later separation workshop section, weakened of the influence of big water gaging again SAPO molecular sieve catalyst stability; (3) improved the molecular weight of first reactor feed,, reduced the volume required of first reactor with respect to methanol feeding.(4) regenerated catalyst for the treatment of that comes out from second reactor contains more carbon deposit before entering revivifier, makes the carbon difference of regenerator and spent agent increase, and so more helps the control that the revivifier inner catalyst is made charcoal.

Therefore, adopt method of the present invention, when improving selectivity of light olefin, also effectively disperseed the water yield in reaction heat and the system, both weakened the influence of water to catalyst stability, have to have reduced second reactor volume, but also make the revivifier easier control of making charcoal, technical have a bigger advantage.

Adopt the preferred technical solution of the present invention: reacted the treat regenerated catalyst of the catalyzer in second fluidized-bed reactor for from the first class bed bioreactor, transporting; The catalyzer with low green coke amount that comes out from the first class bed bioreactor directly enters second fluidized-bed reactor without stripping; Logistics 2 enters or enters first fluidized bed reactor reaction zone from one or more inlets that reaction zone is in axial direction gone up from the bottom sparger; The first class bed bioreactor is a fast fluidized bed, and second fluidized-bed reactor is a fast fluidized bed, and revivifier is a dense phase fluidized bed; First fluidized bed reactor reaction temperature is 350～600 ℃, and the raw material weight air speed is 0.1～100 hour ^-1, be 0～1MPa in the reaction pressure of gauge pressure; The temperature of reaction of second fluidized-bed reactor is 200～400 ℃, and the reaction weight space velocity is 0.1～100 hour ^-1Catalyzer all is selected from SAPO type molecular sieve catalyst in first class bed bioreactor, second fluidized-bed reactor, and low-carbon alkene (ethene+propylene) selectivity can reach 84.5% (weight), has obtained better technical effect.

Description of drawings

Fig. 1 is the schematic flow sheet of the method for the invention.

Among Fig. 1,1 is the first class bed bioreactor; 2 is second fluidized-bed reactor; 3 is the second reactor product outlet line; 4 is the material benzenemethanol feeding line; 5 first fluidized bed reactor reaction zones; 6 are the one or more inlets on the first class bed bioreactor axial location; 7 is gas-solid sharp separation district in first reactor; 8 is cyclonic separator; 9 is the first reactor product outlet line; 10 is that catalyzer is from the line of pipes of first reactor to second reactor; 11 is the line of pipes of reclaimable catalyst to revivifier; 12 is revivifier; 13 is the regenerating medium inlet line; 14 is the line of pipes of regenerated catalyst to first reactor; 15 is the interchanger of the reclaimable catalyst and the second reactor methanol charging; 16 is the catalyst return of first reactor; 17 is the catalyst return of revivifier.

All or part of material benzenemethanol is in second reactor, the lower catalyst of green coke amount of coming is carried in utilization from first reactor, the all or part of mixture that is converted into dimethyl ether and water, gas product converges with methyl alcohol feeding line 4 by pipeline 3 behind cyclone separator and enters first reactor, and perhaps the one or more inlets 6 (shown in the figure being 1) from the first reactor reaction district, 5 axial directions enter reaction zone 5. At reaction zone 5, the mixture of methyl alcohol, dimethyl ether is converted into the product that contains ethene, propylene at catalyst, behind fast branch 7, cyclone separator 8, enters follow-up centrifugal station by pipeline 9. The catalyst of sedimentation or isolated part inactivation enters second reactor by pipeline 10, in second reactor methyl alcohol is converted into dimethyl ether. Catalyst in second reactor behind the inactivation enters fluid bed regenerator 12 by pipeline 11 behind stripping, contact with the regenerating medium that enters regenerator through pipeline 13, and the oxidation reaction of carbon deposit takes place. Enter reactor 2 by pipeline 14 through the catalyst behind the coke-burning regeneration behind stripping, the heat that regenerated catalyst carries partly can be used for heating the material benzenemethanol that enters second reactor, finishes in heat exchanger 15. Flow by catalyst in control

catalyst transport line

10,14 and 16 can guarantee catalyst inventory and the catalyst activity level in first reactor. Catalyst transport line 17 can be used for the degree of control Burning Coke on Catalyst regeneration to a certain extent, guarantees that catalyst reaches required activity level in the feed-line 14.

The invention will be further elaborated below by embodiment, but be not limited only to present embodiment.

Embodiment

[embodiment 1]

In the 316 stainless steel fast fluidized bed reactors of 30 millimeters of φ, with the SAPO-34 molecular sieve catalyst of 50 grams after the spray-dried moulding reactor of packing into, be raw material with pure methyl alcohol, (the raw material weight air speed is 1.0 hours with the feeding rate of 50 Grams Per Hours ^-1) after being preheating to 180 ℃, entering reactor, the temperature of reaction of reactor is 425 ℃.In the gauge pressure reaction pressure is OMPa.Reaction product is analyzed by the gas-chromatography that has thermal conductivity detector.Product analysis when the reaction times is 0.5 hour the results are shown in Table 1.

Table 1

[embodiment 2～4]

According to each step and the condition of embodiment 1, be that product analysis the results are shown in Table 2 according to the temperature of reaction that changes reactor shown in the table 2 like that.

[embodiment 5～7]

According to each step and the condition of embodiment 1, just according to the weight space velocity that changes raw material shown in the table 3 like that, product analysis the results are shown in Table 3.

Table 2

Table 3

[embodiment 8～10]

According to the condition of embodiment 1, just according to changing reaction pressure shown in the table 4 like that, product analysis the results are shown in Table 4.

Table 4

[embodiment 11～13]

According to embodiment 1 described condition, change catalyst type, product analysis the results are shown in Table 5.

Table 5

[embodiment 14～17]

According to embodiment 1 described condition, change feed type, product analysis the results are shown in Table 6.

Table 6

[embodiment 18]

According to embodiment 1 described condition, under the differential responses time methanol conversion and reaction product optionally result of variations see Table 7.

Table 7

[embodiment 19]

According to embodiment 1 described condition, the reaction times is the decaying catalyst after 9 hours among the catalyzer employing embodiment 18, changes temperature of reaction into 260 ℃, and methanol conversion and dme selectivity see Table 8 with the variation in reaction times.

Table 8

Reaction times, hour	0.5	1	3	5	6	7	8
								Methanol conversion, % (weight)	74.8	73.5	70.5	66.1	61.3	56.8	37.5
The dme selectivity, % (weight)	95.7	94.9	93.9	94.1	93.7	92.6	91.4

[embodiment 20～23]

According to embodiment 19 described conditions, change temperature of reaction, the reaction result the when reaction times is 0.5 hour sees Table 9.

Table 9

Temperature of reaction, ℃	200	320	400
				Methanol conversion, % (weight)	68.9	77.4	89.5
The dme selectivity, % (weight)	93.2	96.8	83.2

[embodiment 24～26]

According to embodiment 19 described conditions, change the weight space velocity of methyl alcohol, the reaction result the when reaction times is 0.5 hour sees Table 10.

Table 10

The methyl alcohol weight space velocity, hour ^-1	0.1	20	100
				Methanol conversion, % (weight)	78.5	71.4	65.6
The dme selectivity, % (weight)	90.1	94.8	87.2

[embodiment 27]

Condition according to embodiment 17, the mixture of methyl alcohol, dme and water is divided into two portions, enter reaction zone by the bottom grid distributor with along an inlet on the reaction zone axial direction due respectively, the distance of inlet position and bottom grid distributor is 1/2 reaction zone height, and the weight ratio of two portions compound is 1: 1.Reaction result when the reaction times is 0.5 hour sees Table 11.

Table 11

[embodiment 28]

Condition according to embodiment 17, the mixture of methyl alcohol, dme and water is divided into three parts, enter reaction zone by the bottom grid distributor with along two inlets on the reaction zone axial direction due respectively, the distance of two inlet positions and bottom grid distributor is respectively 1/4 reaction zone height, 1/2 reaction zone height, and the weight ratio of three partially mixed material is 1: 1: 1.Reaction result when the reaction times is 0.5 hour sees Table 12.

Table 12

[embodiment 29]

Condition according to embodiment 17, the mixture of methyl alcohol, dme and water is divided into five parts, enter reaction zone by the bottom grid distributor with along four inlets on the reaction zone axial direction due respectively, the distance of four inlet positions and bottom grid distributor is respectively 1/8 reaction zone height, 1/6 reaction zone height, 1/4 reaction zone height, 1/2 reaction zone height, and the weight ratio of five partially mixed material is 1: 1: 1: 1: 1.Reaction result when the reaction times is 0.5 hour sees Table 13.

Table 13

Obviously, on the SAPO-34 of inactivation catalyzer, under lower temperature of reaction, methyl alcohol can partly be converted into dme and water, and the methanol feedstock that contains certain proportion dme and water makes C in reaction process ₁By product reduces, and has improved the selectivity of low-carbon alkene.It is the reaction zone of dme that this method equals to have added methanol conversion in the steam stripped equipment outside to catalyzer employing reactor, catalyzer directly utilizes is part decaying catalyst in the main reactor, exceeding under the prerequisite that increases facility investment, effectively optimized the utilization of energy, improved the ratio of low-carbon alkene in the product, have remarkable advantages, can be applicable to industrial production.

Claims

1. one kind is improved optionally method of ethene and propylene in methyl alcohol or dimethyl ether conversion process, may further comprise the steps:

A) be raw material with methyl alcohol or dme, raw material enters reaction zone from first fluidized bed reactor bottom, generates the effluent 1 that contains ethene, propylene with the catalyzer contact reacts, obtains ethene, propylene through separation;

B) the reacted regenerated catalyst for the treatment of of the first fluidized bed enters the second fluidized-bed reactor bottom, generate the logistics 2 that contains dme with the methanol feedstock contact reacts, logistics 2 turns back to first fluidized bed reactor feed, and reacted reclaimable catalyst enters breeding blanket, revivifier bottom and regenerates;

C) catalyzer after the regeneration returns first fluidized bed reactor lower part reaction zone;

Wherein, the catalyzer in the first fluidized bed or second fluidized-bed reactor all is selected from the SAPO-34 molecular sieve catalyst.

2. according to the described optionally method of ethene and propylene that in methyl alcohol or dimethyl ether conversion process, improves of claim 1, it is characterized in that logistics 2 enters or enters first fluidized bed reactor reaction zone from least one inlet that reaction zone is in axial direction gone up from the bottom sparger.

3. according to the described optionally method of ethene and propylene that improves of claim 1, it is characterized in that the first class bed bioreactor is a fast fluidized bed in methyl alcohol or dimethyl ether conversion process, second fluidized-bed reactor is a fast fluidized bed, and revivifier is a dense phase fluidized bed.

4. according to the described optionally method of ethene and propylene that improves of claim 1, it is characterized in that the temperature of reaction in the first class bed bioreactor is 350～600 ℃ in methyl alcohol or dimethyl ether conversion process, the raw material weight air speed is 0.1～100 hour ^-1, be 0～1MPa in the gauge pressure reaction pressure; Temperature of reaction in second fluidized-bed reactor is 200～400 ℃, and the raw material weight air speed is 0.1～100 hour ^-1

5. according to the described optionally method of ethene and propylene that in methyl alcohol or dimethyl ether conversion process, improves of claim 4, it is characterized in that the temperature of reaction in the first class bed bioreactor is 425～500 ℃, the raw material weight air speed is 1.0～20 hours-1, is 0.1～0.3MPa in the gauge pressure reaction pressure; Temperature of reaction in second fluidized-bed reactor is 260～320 ℃, and the raw material weight air speed is 1～20 hour ^-1