CN101279874B - Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether - Google Patents

Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether Download PDF

Info

Publication number
CN101279874B
CN101279874B CN2007100390854A CN200710039085A CN101279874B CN 101279874 B CN101279874 B CN 101279874B CN 2007100390854 A CN2007100390854 A CN 2007100390854A CN 200710039085 A CN200710039085 A CN 200710039085A CN 101279874 B CN101279874 B CN 101279874B
Authority
CN
China
Prior art keywords
bed reactor
fluidized
catalyzer
catalyst
propylene
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN2007100390854A
Other languages
Chinese (zh)
Other versions
CN101279874A (en
Inventor
谢在库
齐国祯
杨为民
钟思青
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Priority to CN2007100390854A priority Critical patent/CN101279874B/en
Publication of CN101279874A publication Critical patent/CN101279874A/en
Application granted granted Critical
Publication of CN101279874B publication Critical patent/CN101279874B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • 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
    • 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
    • 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 producing a low carbon olefin by methanol or dimethyl enther, which mainly solves the problems of low production capacity of device, low selectivity of the low carbon olefin, small catalyst circulating load and large temperature gradient of a reactor of the prior art. The invention properly solves the problems by adopting the technical proposals that: a methanol is taken as a raw material, and the method comprises the following steps that: a) from 10 to 90 percent of methanol by total weight enters a reaction zone from the bottom part of a first fluidized bed reactor and contacts with a catalyst to generate a stream 1; b) the residual methanol enters the reaction zone from the bottom part of a second fluidized bed reactor and contacts with the catalyst to generate a stream 2; c) catalyst dust respectively separated from the stream 1 and the stream 2 settles down or returns to a steam stripping section at the lower part of the settling section of the respective fluidized bed reactor from a catalyst dipleg at the lower part of the respective cyclone separator; d) the catalyst in the steam stripping section at the lower part of the settling section of the first fluidized bed reactor enters the bottom part of the second fluidized bed reactor after the steam stripping; and the catalyst in the steam stripping section at the lower part of the settling section of the second fluidized bed reactor enters the bottom part of a regenerator after the steam stripping; and e) the catalyst under regeneration entering the bottom part of the regenerator returns to the reaction zone at the lower part of the fluidized bed reactor after the regeneration by the regenerator and the steam stripping by a stripper, and the method of preparation can be used for the industrial production of low carbon olefin.

Description

Method by methyl alcohol or dme production low-carbon alkene
Technical field
The present invention relates to a kind of method of producing low-carbon alkene by methyl alcohol or dme.
Background technology
Low-carbon alkene mainly is ethene and propylene, is two kinds of important basic chemical industry raw materials, and its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, 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 technology that alternative materials transforms system ethene, propylene.Wherein, the alternative materials that is used for low-carbon alkene production that one class is important is an oxygenatedchemicals, for example alcohols (methyl alcohol, ethanol), ethers (dme, methyl ethyl ether), ester class (methylcarbonate, methyl-formiate) etc., these oxygenatedchemicalss can be transformed by coal, Sweet natural gas, biomass equal energy source.Some oxygenatedchemicals can reach fairly large production, as methyl alcohol, can be made by coal or Sweet natural gas, and technology is very ripe, can realize up to a million tonnes industrial scale.Because the popularity in oxygenatedchemicals source is added and is transformed the economy that generates low-carbon alkene technology, so by the technology of oxygen-containing compound conversion to produce olefine (OTO), particularly the technology by methanol conversion system alkene (MTO) is subjected to increasing attention.
In the US4499327 patent silicoaluminophosphamolecular molecular sieves catalyzer is applied to methanol conversion system olefin process and studies in great detail, think that SAPO-34 is the first-selected catalyzer of MTO technology.
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.But the single series processing power of the described fast fluidized bed reactor of this method is lower.
In addition, guarantee high selectivity of light olefin, need long-pending a certain amount of carbon of on the SAPO-34 catalyzer.The method that relates to catalyzer coke content in a kind of MTO of control reactor reaction zone in the US20060025646 patent is the catalyzer part of inactivation to be sent into the breeding blanket make charcoal, and another part decaying catalyst turns back to reaction zone and continues reaction.Because the agent of MTO technology alcohol is than very little, coking yield is lower, if, can make that the catalyst flow between reactor and the revivifier is less in the degree of making charcoal of revivifier inner control catalyzer, and very high to the requirement of catalyst flow control.
Art methods exists all that plant capacity is low, revivifier is made charcoal and is difficult to the problem of aspects such as controlling, the catalyst recirculation amount is less.
Summary of the invention
Technical problem to be solved by this invention is the problem that the plant capacity that exists in the prior art is low, yield of light olefins is low, the catalyst recirculation amount is little, the temperature of reactor gradient is big, and a kind of new method by methyl alcohol or dme production low-carbon alkene is provided.This method is used for the production of low-carbon alkene, has the advantage that the high and low carbon olefin yield of plant capacity height, catalyst recirculation amount are big, the temperature of reactor gradient is little.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of method of producing low-carbon alkene by methyl alcohol or dme, may further comprise the steps: a) 10～90% total methyl alcohol weight enter reaction zone from the bottom of first class bed bioreactor, contact with catalyzer to generate the logistics 1 that contains catalyst dust, ethene, propylene; B) methyl alcohol of surplus enters reaction zone from the bottom of second fluidized-bed reactor, contacts with catalyzer to generate the logistics 2 that contains catalyst dust, ethene, propylene; C) logistics 1 is after the cyclonic separator in each autoreactor settling section separates respectively with logistics 2, and the gas phase that contains ethene, propylene is discharged from reactor head separately and entered follow-up centrifugal station; Isolated respectively catalyst dust sedimentation or return the stripping stage of fluidized-bed reactor settling section bottom separately from logistics 1 and logistics 2 from the catalyzer dipleg of cyclonic separator bottom separately; D) catalyzer in the stripping stage of first class bed bioreactor settling section bottom enters the bottom of second fluidized-bed reactor behind stripping; Catalyzer in the stripping stage of the second fluidized-bed reactor settling section bottom enters regenerator bottoms behind stripping; What e) enter regenerator bottoms treats that regenerated catalyst is behind revivifier regeneration, stripper stripping, all return first fluidized bed reactor lower part reaction zone, all return the second fluidized-bed reactor lower reaction zone or a part and return first fluidized bed reactor lower part reaction zone, a part is returned the second fluidized-bed reactor lower reaction zone.
In the technique scheme, the described first class bed bioreactor and second fluidized-bed reactor and revivifier are fast fluidized bed; 40～60% total methyl alcohol weight enter reaction zone from the bottom of first class bed bioreactor; Described catalyzer is a SAPO type molecular sieve, and preferred version is the SAPO-34 molecular sieve; The average coke content of catalyzer behind the revivifier coke-burning regeneration is less than 1% (weight), and preferred version is less than 0.5% (weight); Temperature in the revivifier is between 550～700 ℃, and preferred version is 600～650 ℃; Pressure in the revivifier is counted 0～1MPa with gauge pressure, and preferred version is 0.1～0.3MPa; The temperature of the first class bed bioreactor and the second fluidized-bed reactor reaction zone is 350～600 ℃, and preferred version is 425～500 ℃; Pressure in the first class bed bioreactor and second fluidized-bed reactor is 0～1MPa in gauge pressure, and preferred version is 0.1～0.3MPa; The first class bed bioreactor and the second fluidized-bed reactor raw material weight air speed are 0.1～20 hour -1, preferred version is 3～8 hours -1Catalyzer in the stripping stage of first class bed bioreactor settling section bottom enters regenerator bottoms through the stripping rear section, and the catalyzer in the stripping stage of the second fluidized-bed reactor settling section bottom enters first fluidized bed reactor bottom through the stripping rear section; Catalyzer in the stripping stage of first class bed bioreactor settling section bottom returns first fluidized bed reactor bottom through the stripping rear section, and the catalyzer in the stripping stage of the second fluidized-bed reactor settling section bottom returns second fluidized-bed reactor bottom through the stripping rear section.
In reactor feed, can also add the common charging of a certain proportion of thinner non-imposedly, thinner can be low-carbon alkanes (methane, ethane, propane etc.), low-carbon 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.
Because the methanol molecules amount is little, it is quite big to reach the required reactor volume of up to a million tons methyl alcohol treatment scale, adding methanol conversion is may add a certain amount of thinner in the low-carbon alkene reaction process in order to improve the selectivity of low-carbon alkene, to reach certain treatment scale like this, required reactor diameter can be bigger, and the increase of reactor diameter is higher for the requirement meeting of aspects such as gas-solid flow distribution, inner member, back-mixing control.As calculated, realize 1,000,000 tons/year methyl alcohol treatment scale, the diameter of single series reactor will reach more than 10 meters.The reactor that diameter is so big can make gas-solid in the reactor skewness that flows, and the back-mixing degree strengthens, because the MTO reaction is strong exothermal reaction, can make also that therefore the thermograde in the reactor strengthens, and these factors all will have a strong impact on product selectivity.In addition, because the coking yield of methanol to olefins reaction is lower, but also the average coke content that needs to guarantee catalyst in reactor causes the catalyst recirculation amount in the reaction-regeneration system very little on required level, and is very high to the control requirement of catalyst flow.The present invention adopts a kind of fluidized bed reactor system, sets up two fluidized-bed reactors, can realize bigger methyl alcohol treatment scale under the less situation of single series reactor diameter.Exchange owing to catalyzer between two reactors, make that the intrasystem catalyzer coke content adjustment of entire reaction is more flexible, on this basis, can improve the intensity of making charcoal of revivifier, thereby increase " carbon is poor " of reclaimable catalyst and regenerated catalyst, make that the catalyst recirculation quantitative change in the reaction-regeneration system is big, flow control is more prone to.
Adopt technical scheme of the present invention: the first class bed bioreactor and second fluidized-bed reactor and revivifier are fast fluidized bed; Described catalyzer is a SAPO type molecular sieve; The average coke content of catalyzer behind the revivifier coke-burning regeneration is less than 1% (weight), and the temperature in the revivifier is between 550～700 ℃, and the pressure in the revivifier is counted 0～1MPa with gauge pressure; The temperature of the first class bed bioreactor and the second fluidized-bed reactor reaction zone is 350～600 ℃, pressure in the first class bed bioreactor and second fluidized-bed reactor is 0～1MPa in gauge pressure, and the first class bed bioreactor and the second fluidized-bed reactor raw material weight air speed are 0.1～20 hour -1, yield of light olefins can reach 77.13% (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 feeding line of first fluidized bed reactor bottom; 2 is the fluidized-bed reactor reaction zone; 3 is stripping stage; 4 is the settling section of fluidized-bed reactor; 5 is the reactor internal cyclone separators; 6 is collection chamber; 7 is product gas outlet; 8 is the first class bed bioreactor is carried catalyzer in second fluidized-bed reactor pipeline; 9 is second fluidized-bed reactor is carried catalyzer in the first class bed bioreactor pipeline; 10 is the line of pipes that first class bed bioreactor stripping stage catalyzer returns the reaction zone bottom; 11 is the line of pipes that the catalyzer of the second fluidized-bed reactor stripping stage returns reaction zone 2 bottoms; 12 be in second fluidized-bed reactor behind the stripping reclaimable catalyst enter the line of pipes of revivifier; 13 is the feeding line of second fluidized-bed reactor bottom; 14 is the opening for feed of revivifier; 15 is the revivifier breeding blanket; 16 is the gas-solid sharp separation section of fluidized-bed reactor; 17 is the gas-solid sharp separation section on top, revivifier breeding blanket; 18 is the revivifier settling section; 19 is the revivifier internal cyclone separators; 20 is flue gas discharge opening; 21 return the line of pipes of first fluidized bed reaction zone for regenerated catalyst; 22 return the line of pipes of second fluidized bed reaction zone for regenerated catalyst; 23 is reactive system; 24 is regenerated catalyst stripper.
Methyl alcohol enters respectively the reaction zone 2 of first class bed bioreactor and second fluidized bed reactor from feeding line 1 and 13, contact generation with catalyst and contain catalyst dust, ethene, the logistics of propylene, after cyclone separator in each autoreactor settling section 45 separates respectively, contain ethene, the gas phase of propylene enters collection chamber 6 from reactor head separately, enter follow-up centrifugal station from outlet 7 discharges at collection chamber 6 tops, isolated catalyst dust sedimentation or return the separately stripping section 3 of fluidized-bed reactor settling section 4 bottoms from the catalyst dipleg of cyclone separator 5 bottoms separately, enter 15 bottoms, regenerator renewing zone through stripping rear portion catalyst by pipeline 12, part catalyst is by pipeline 8,9 enter the bottom of another fluidized-bed reactor, and a part of catalyst is by pipeline 10,11 return the separately reaction zone 2 of fluidized-bed reactor bottom. Catalyst to be regenerated is behind regenerator regeneration, stripper 24 strippings, part catalyst returns first fluidized bed reactor lower part reaction zone by pipeline 21, part catalyst returns second fluidized bed reactor lower reaction zone by pipeline 22, and the flue gas of generation is discharged by exhanst gas outlet 20 after separating through the cyclone separator 19 in the regenerator.
The invention will be further elaborated below by embodiment, but be not limited only to present embodiment.
Embodiment
[embodiment 1～4]
In reaction-regenerative device as shown in Figure 1, revivifier adopts fast fluidized bed, and lift gas is an air, 600 ℃ of regeneration temperatures.Two reactors all adopt fast fluidized bed, and the gas superficial velocity in each reactor is 1.2 meter per seconds, and temperature of reaction is 425 ℃, pure methanol feeding, and wherein 40% (weight) enters the first class bed bioreactor, and the methyl alcohol weight space velocity is 3 hours -1, be 0MPa in gauge pressure reaction and regeneration pressure.First class bed bioreactor stripping stage links to each other with the second fluidized-bed reactor reaction zone by pipeline 8, and the weight ratio of the catalyst flow in catalyst flow and the pipeline 12,10 is 1: 2: 3.The second fluidized-bed reactor stripping stage links to each other with first fluidized bed reactor reaction zone by pipeline 9, and the weight ratio of the catalyst flow in catalyst flow and the pipeline 12,11 is 1: 2: 3.The thief hole of regenerator and spent agent lays respectively on pipeline 21 and the pipeline 12, and infrared carbon sulphur high speed analysis instrument is adopted in the analysis of carbon content on the catalyzer.The internal circulating load of catalyzer is remained on a rational value, make that system is stable, control is convenient, the catalyst recirculation amount is 2 with the ratio of methyl alcohol combined feed total feed mass rate.Catalyzer adopts the SAPO-34 modified catalyst of spray-dried moulding.The reactor outlet product adopts online gas chromatographic analysis, and experimental result sees Table 1.
Table 1
Embodiment Breeding blanket gas phase superfacial velocity, meter per second The average coke content of reaction zone inner catalyst, % (weight) The regenerator coke content, % (weight) Ethene carbon back yield, % (weight) Propylene carbon back yield, % (weight) Ethene+propylene carbon back yield, % (weight)
Embodiment 1 0.2 2.81 0.05 36.83 39.56 76.39
Embodiment 2 0.5 5.26 0.41 40.46 36.67 77.13
Embodiment 3 1.0 5.81 0.97 42.34 32.43 74.77
Embodiment 4 1.5 6.74 2.03 45.76 28.25 74.01
[embodiment 5～7]
According to embodiment 2 described conditions, just change regenerator temperature, experimental result sees Table 2.
Table 2
Parameter Regeneration temperature, ℃ The average coke content of reaction zone inner catalyst, % (weight) The regenerator coke content, % (weight) Ethene carbon back yield, % (weight) Propylene carbon back yield, % (weight) Ethene+propylene carbon back yield, % (weight)
Embodiment 5 550 5.64 0.78 41.43 34.92 76.35
Embodiment 6 650 5.12 0.13 40.65 35.29 75.94
Embodiment 7 700 4.69 0.02 38.67 35.98 74.65
[embodiment 8～10]
According to embodiment 3 described conditions, just change temperature of reactor, experimental result sees Table 3.
Table 3
Parameter Temperature of reaction, ℃ Ethene carbon back yield, % (weight) Propylene carbon back yield, % (weight) Ethene+propylene carbon back yield, % (weight)
Embodiment 8 350 34.25 36.86 71.11
Embodiment 9 500 45.87 30.93 76.8
Embodiment 10 600 51.34 21.41 72.75
[embodiment 11～13]
According to embodiment 3 described conditions, just change the methyl alcohol weight space velocity of each autoreactor, experimental result sees Table 4.
Table 4
Parameter The methyl alcohol weight space velocity, hour -1 Ethene carbon back yield, % (weight) Propylene carbon back yield, % (weight) Ethene+propylene carbon back yield, % (weight)
Embodiment 11 0.12 40.21 31.57 71.78
Embodiment 12 8.11 43.42 33.56 76.98
Embodiment 13 19.45 44.27 27.16 71.43
[embodiment 14～16]
According to embodiment 3 described conditions, reactor and revivifier adopt same press operation, change the pressure of reactor, revivifier, and experimental result sees Table 5.
Table 5
Parameter The pressure of reactor and revivifier, Mpa Ethene carbon back yield, % (weight) Propylene carbon back yield, % (weight) Ethene+propylene carbon back yield, % (weight)
Embodiment 14 0.1 40.64 33.66 74.3
Embodiment 15 0.3 38.88 32.87 71.75
Embodiment 16 1 35.87 31.65 67.52
[embodiment 17～19]
According to embodiment 3 described conditions, change the catalyst type in the reactor, experimental result sees Table 6.
Table 6
Parameter Catalyst type Ethene carbon back yield, % (weight) Propylene carbon back yield, % (weight) Ethene+propylene carbon back yield, % (weight)
Embodiment 17 SAPO-11 7.11 21.87 28.98
Embodiment 18 SAPO-18 41.18 30.88 72.06
Embodiment 19 SAPO-56 25.99 21.58 47.57
[embodiment 20]
According to embodiment 3 described conditions, 60% (weight) enters the first class bed bioreactor in the methanol feeding, and the methyl alcohol weight space velocity is 3 hours -1The weight ratio of the catalyst flow in catalyst flow in the pipeline 8 and the pipeline 12,10 is 2: 1: 1.The weight ratio of the catalyst flow in catalyst flow in the pipeline 9 and the pipeline 12,11 is 2: 3: 1, experimental result is: ethene carbon back yield is that 43.14% (weight) propylene carbon back yield is 32.15% (weight), ethene+propylene carbon back yield 75.29% (weight).

Claims (9)

1. method of producing ethene and propylene by methyl alcohol or dme may further comprise the steps:
A) 10～90% total methyl alcohol weight enter reaction zone from the bottom of first class bed bioreactor, contact with catalyzer to generate the logistics 1 that contains catalyst dust, ethene, propylene;
B) methyl alcohol of surplus enters reaction zone from the bottom of second fluidized-bed reactor, contacts with catalyzer to generate the logistics 2 that contains catalyst dust, ethene, propylene;
C) logistics 1 is after the cyclonic separator in each autoreactor settling section separates respectively with logistics 2, and the gas phase that contains ethene, propylene is discharged from reactor head separately and entered follow-up centrifugal station; Isolated respectively catalyst dust sedimentation or return the stripping stage of fluidized-bed reactor settling section bottom separately from logistics 1 and logistics 2 from the catalyzer dipleg of cyclonic separator bottom separately;
D) catalyzer in the stripping stage of first class bed bioreactor settling section bottom enters the bottom of second fluidized-bed reactor behind stripping; Catalyzer in the stripping stage of the second fluidized-bed reactor settling section bottom enters regenerator bottoms behind stripping;
What e) enter regenerator bottoms treats that regenerated catalyst is behind revivifier regeneration, stripper stripping, all return first fluidized bed reactor lower part reaction zone, all return the second fluidized-bed reactor lower reaction zone or a part and return first fluidized bed reactor lower part reaction zone, a part is returned the second fluidized-bed reactor lower reaction zone.
2. according to the described method of producing ethene and propylene of claim 1, it is characterized in that first class bed bioreactor, second fluidized-bed reactor and revivifier are fast fluidized bed by methyl alcohol or dme; 40～60% total methyl alcohol weight enter reaction zone from the bottom of first class bed bioreactor; Described catalyzer is a SAPO type molecular sieve.
3. according to the described method of producing ethene and propylene of claim 1 by methyl alcohol or dme, it is characterized in that the temperature in the revivifier is between 550～700 ℃, revivifier is interior to be 0～1MPa in gauge pressure pressure, and the average coke content of the catalyzer behind the revivifier coke-burning regeneration is less than 1% weight.
4. according to the described method of producing ethene and propylene of claim 3 by methyl alcohol or dme, it is characterized in that the temperature in the revivifier is 600～650 ℃, revivifier is interior to be 0.1～0.3MPa in gauge pressure pressure, and the average coke content of the catalyzer behind the revivifier coke-burning regeneration is less than 0.5% weight.
5. according to the described method of producing ethene and propylene of claim 2, it is characterized in that SAPO type molecular sieve is the SAPO-34 molecular sieve by methyl alcohol or dme.
6. according to the described method of producing ethene and propylene of claim 1 by methyl alcohol or dme, the temperature that it is characterized in that the first fluidized bed and the second fluidized-bed reactor reaction zone is 350～600 ℃, pressure in the reactor is 0～1MPa in gauge pressure, and the raw material weight air speed is 0.1～20 hour -1Between.
7. according to the described method of producing ethene and propylene of claim 6 by methyl alcohol or dme, the temperature that it is characterized in that the first fluidized bed and the second fluidized-bed reactor reaction zone is 425～500 ℃, pressure in the reactor is 0.1～0.3MPa in gauge pressure, and the raw material weight air speed is 3～8 hours -1
8. according to the described method of producing ethene and propylene of claim 1, it is characterized in that the catalyzer in the stripping stage of first class bed bioreactor settling section bottom enters regenerator bottoms through the stripping rear section by methyl alcohol or dme; Catalyzer in the stripping stage of the second fluidized-bed reactor settling section bottom enters first fluidized bed reactor bottom through the stripping rear section.
9. according to the described method of producing ethene and propylene of claim 1, it is characterized in that the catalyzer in the stripping stage of first class bed bioreactor settling section bottom returns first fluidized bed reactor bottom through the stripping rear section by methyl alcohol or dme; Catalyzer in the stripping stage of the second fluidized-bed reactor settling section bottom returns second fluidized-bed reactor bottom through the stripping rear section.
CN2007100390854A 2007-04-04 2007-04-04 Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether Active CN101279874B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2007100390854A CN101279874B (en) 2007-04-04 2007-04-04 Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2007100390854A CN101279874B (en) 2007-04-04 2007-04-04 Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether

Publications (2)

Publication Number Publication Date
CN101279874A CN101279874A (en) 2008-10-08
CN101279874B true CN101279874B (en) 2011-04-27

Family

ID=40012573

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2007100390854A Active CN101279874B (en) 2007-04-04 2007-04-04 Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether

Country Status (1)

Country Link
CN (1) CN101279874B (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101402538B (en) * 2008-11-21 2013-01-09 中国石油化工股份有限公司 Method for improving yield of light olefins
CN102295501B (en) * 2010-06-24 2014-09-10 中国石油化工股份有限公司 Method for producing low-carbon olefin

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4499327A (en) * 1982-10-04 1985-02-12 Union Carbide Corporation Production of light olefins
US6166282A (en) * 1999-08-20 2000-12-26 Uop Llc Fast-fluidized bed reactor for MTO process
US20060025646A1 (en) * 2004-07-30 2006-02-02 Fung Shun C Conversion of oxygenates to olefins

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4499327A (en) * 1982-10-04 1985-02-12 Union Carbide Corporation Production of light olefins
US6166282A (en) * 1999-08-20 2000-12-26 Uop Llc Fast-fluidized bed reactor for MTO process
US20060025646A1 (en) * 2004-07-30 2006-02-02 Fung Shun C Conversion of oxygenates to olefins

Also Published As

Publication number Publication date
CN101279874A (en) 2008-10-08

Similar Documents

Publication Publication Date Title
CN101348404B (en) Method for improving ethylene and propene yield in methyl alcohol or dimethyl ether conversion process
CN101279877B (en) Method for increasing yield of ethylene and propone in conversion process of oxocompound
CN101279873B (en) Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether
CN101239869B (en) Process for converting methanol or dimethyl ether to low-carbon olefins
CN101270023B (en) Method for improving yield of light olefin hydrocarbon
CN101333141B (en) Reaction device for conversing methanol or dimethyl ether to be low carbon olefin
CN101279875A (en) Method for increasing production of ethylene and propone
CN102276402B (en) Combined reaction apparatus for producing low-carbon olefin
CN101239874A (en) Reaction device for converting oxygen-containing compound to low-carbon olefins
CN101270019B (en) Method for preparing low carbon olefin hydrocarbon with methanol or dimethyl ether
CN101239873B (en) Method for converting oxygen-containing compound to low-carbon olefins
CN102295506B (en) Method for producing low-carbon olefin by using methanol
CN101318870B (en) Process for improving yield of ethylene and propylene
CN101306969B (en) Reaction device for preparing low-carbon olefin from oxygen-containing compounds
CN102276406B (en) Method for increasing yield of propylene
CN102295507B (en) Method for converting methanol or dimethyl ether into low-carbon olefin
CN102875289B (en) Method for preparing low-carbon olefins
CN102190542A (en) Method for coupling preparation of olefins from methanol and catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms
CN101279876B (en) Method for preparing ethylene and propone with oxocompound
CN102190540B (en) Method for producing propylene
CN101279874B (en) Method for preparing low-carbon olefin hydrocarbon with methanol or dimethyl ether
CN102372542A (en) Method for improving yield of ethylene and propylene
CN101293802B (en) Method for preparing light olefin hydrocarbon with methanol or dimethyl ether
CN102276395B (en) Method for producing ethylene and propylene
CN102276399B (en) Method for producing lower olefins from methanol and naphtha

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant