CN1156416C - Process and system for preparing low-carbon olefin from methanol or dimethylether - Google Patents
Process and system for preparing low-carbon olefin from methanol or dimethylether Download PDFInfo
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- CN1156416C CN1156416C CNB011441887A CN01144188A CN1156416C CN 1156416 C CN1156416 C CN 1156416C CN B011441887 A CNB011441887 A CN B011441887A CN 01144188 A CN01144188 A CN 01144188A CN 1156416 C CN1156416 C CN 1156416C
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 20
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 230000008569 process Effects 0.000 title description 14
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title 1
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 239000007787 solid Substances 0.000 claims abstract description 31
- 239000003054 catalyst Substances 0.000 claims abstract description 27
- 239000002994 raw material Substances 0.000 claims abstract description 17
- 230000008929 regeneration Effects 0.000 claims abstract description 14
- 238000011069 regeneration method Methods 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims abstract description 3
- 239000000047 product Substances 0.000 claims description 19
- 239000012071 phase Substances 0.000 claims description 11
- 229930195733 hydrocarbon Natural products 0.000 claims description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 9
- 238000003672 processing method Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 230000002779 inactivation Effects 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 4
- 238000005516 engineering process Methods 0.000 abstract description 5
- 238000010517 secondary reaction Methods 0.000 abstract description 5
- 150000001335 aliphatic alkanes Chemical class 0.000 abstract description 4
- 239000002808 molecular sieve Substances 0.000 abstract description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 abstract description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 3
- 239000006227 byproduct Substances 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 abstract 2
- GHTGICGKYCGOSY-UHFFFAOYSA-K aluminum silicon(4+) phosphate Chemical compound [Al+3].P(=O)([O-])([O-])[O-].[Si+4] GHTGICGKYCGOSY-UHFFFAOYSA-K 0.000 abstract 1
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 18
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 13
- 239000003921 oil Substances 0.000 description 13
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 9
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 9
- 150000001336 alkenes Chemical class 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000010504 bond cleavage reaction Methods 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000007017 scission Effects 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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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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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a technological method and a system for using dimethyl ether or methanol to produce low-carbon alkene. The technology uses a silicon aluminum phosphate molecular sieve (SAPO34) as a catalyst and uses a gas and liquid parallel downflow type fluidized bed super short contact reactor, the catalyst is in contact with the raw materials in the gas and liquid parallel downflow type fluidized bed super short contact reactor, and the material flow direction is downward; after leaving the reactor, the catalyst and reaction products enter a gas and solid quick separator arranged below the reactor for quick separation to stop the reaction in time. The method effectively suppresses secondary reaction; the separated catalyst enters a regenerator for regeneration by burning carbon, the catalyst is continuously regenerated in the system, and the reaction is cyclic. The technological method and the system of the present invention reduce the generation of side product alkane, lower the difficulty degree of a subsequent separation technology and increase the yield of the low-carbon alkene. The conversion rate of the dimethyl ether or the methanol is higher than 98%, and the yield of the low-carbon alkene is higher than 93%.
Description
Technical field
The present invention relates to a kind of processing method and system thereof that produces low-carbon alkene by methyl alcohol or dme, belong to chemical engineering process
Technical field.
Background technology
Ethene, propylene are important basic Organic Chemicals.Traditional technology is mainly taked low-carbon alkenes such as light oil cracking production ethene, propylene such as petroleum naphtha.And the crude oil oil of China lays particular stress on, and petroleum naphtha, gas oil are under-supply; Crude oil price fluctuation aggravation on the world market, the price of light oil products such as petroleum naphtha also rises steadily, and cause the raw materials cost of ethene too high, and raw material accounts for 60～80% in production cost of ethylene, greatly reduce the economic benefit of manufacturing enterprise, even cause the big area loss of enterprise.In recent years, producing low-carbon alkene by dme or methanol decomposition becomes the research focus, and the silicoaluminophosphamolecular molecular sieves catalyzer is applied to this process.There are abundant Sweet natural gas, coal and ecological waste resource in China, can produce a large amount of synthetic gas by the chemical process to these resources, and synthetic gas can generate methyl alcohol or dme, technology maturation, and price is low.Silicoaluminophosphamolecular molecular sieves catalyzer (SAP034) catalysis dme or methanol to olefins process have feed stock conversion height, triolefin yield height, ethene, propylene product can modulation etc. advantage.Compare with traditional ethylene process, yield of ethene brings up to 50% by about 30%, and raw materials cost also reduces greatly.
At present, producing low-carbon alkene by methyl alcohol or dme, mainly is to adopt the SAP034 molecular sieve as catalyzer, with the processing method of raw material generation scission reaction.The general riser reactor that uses of this type of reaction in industrial production, U.S. associating oil product company is built in the industrial demonstration unit of Norway and the pilot plant of the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences all adopts this type of reactor.This reaction time is extremely short, reacts very easily inactivation of used catalyzer, need react continuously and reprocessing cycle.(Liu Zhongmin etc., synthetic gas are via dme or preparing low carbon olefinic hydrocarbon with methanol, and oil gas is processed, 1998 the 1st phases)
Chinese patent CN1166478A discloses a kind of technical process that makes continuous catalyst regenerating, and scission reaction is carried out in the ciculation fluidized reaction unit of a kind of upstriker dense bed.This installs mainly by the dense bed reactor, cyclonic separator, and catalyst regenerator, compositions such as continous way catalyst feed systems have been realized reaction and regenerated serialization on this device.In above-mentioned technological process, dme or methanol decomposition are produced the reaction path of low-carbon alkene, can be regarded as basically to be made up of two following committed steps:
Methyl alcohol or dme → alkene+water
Alkene → aromatic hydrocarbons+alkane
We can find that by dme or preparing low carbon olefinic hydrocarbon with methanol be a succession of reaction by above-mentioned two reactions steps, and purpose product alkene is intermediate product.For reducing the generation of by product alkane, increase the output of product alkene, just need catalyzer and gas products sharp separation, in time stopped reaction reduces the generation of secondary reaction.And in riser reactor, raw material and catalyzer enter from reactor lower part, and the logistics direction is up, and the axial mixing of catalyzer and gaseous fraction is all very serious, inevitably causes the generation of a large amount of secondary reactions, have reduced the output of alkene in the product.Generally the cyclonic separator particle residence time of Shi Yonging obviously can not be satisfied the needs of gas-solid sharp separation about 0.5 second.
Summary of the invention
The invention provides a kind of new process and system that produces low-carbon alkene by methyl alcohol or dme, make its generation that can effectively reduce secondary reaction, thereby reduce the generation of by product alkane, further increase the output of product alkene.
The present invention is achieved through the following technical solutions: a kind ofly produce the synthetic process of low-carbon alkene by methyl alcohol or dme, this method is carried out successively as follows:
A. raw material enters the ultrashort contact reactor of gas-solid cocurrent flow descending formula via inlet device from top, and the sparger of catalyzer in being arranged on inlet device distributes in advance, and the reactor of flowing through from top to bottom, its agent-oil ratio are 5～30;
B. catalyzer and raw material are 450～650 ℃ in temperature, and pressure is to contact in reactor under 0.01～1.0MPa condition, react, and the control residence time is 0.1～10 second;
C. the material that is come out by reactor bottom enters the gas-solid quick disconnector, carries out separating treatment, makes reaction product and catalyzer sharp separation, and isolated gas-phase product enters follow-up workshop section and handles, and promptly obtains the purpose product;
D. the catalyzer of reaction back inactivation enters stripper by the separator bottom, remove hydrocarbons on the catalyzer with stripped vapor, enter in the revivifier then, under 500～800 ℃ of temperature, carry out coke-burning regeneration, the heat that coke-burning regeneration generates is taken out by interchanger, and the catalyzer after the regeneration enters catalyzer from regenerator bottoms through ball valve and promotes line, is carried by lifting gas and enters inlet device, it is entered in the reactor, finish circulating reaction;
E. when system stops in emergency, regenerated catalyst is discharged into storage tank by control valve; When need replenished fresh catalyzer, the catalyzer in the storage tank entered gas by control valve and carries line participation circulating reaction.
In the above-mentioned processing method, raw material be pure Dimethyl ether, methyl alcohol or its respectively with the mixture of water, adopt gas phase or liquid phase feeding.
A kind of system that is used to realize above-mentioned processing method, this system comprises:
An inlet device that is arranged on reactor head, its inside are provided with a catalyst distributor and a feed(raw material)inlet;
The ultrashort contact reactor of gas-solid cocurrent flow descending formula fluidized-bed, its bottom links to each other with the gas-solid quick disconnector, and this gas-solid quick disconnector bottom is provided with a stripper;
A revivifier, this revivifier links to each other with stripper by pipeline; The interchanger that the heat that decaying catalyst coke-burning regeneration in the revivifier is generated is taken out, this interchanger links to each other with revivifier;
A catalyzer storage tank, its top links together by pipeline and the revivifier that control valve is housed, and its underpart promotes line by the pipeline that catalyst control valve is housed with regenerator and links to each other;
Regenerator bottoms promotes line by the pipeline that catalyst control valve is housed with regenerator and links to each other, and this regenerator promotes line and links to each other with inlet device.
In processing method of the present invention, its reactor has adopted gas-solid cocurrent flow descending formula fluidized-bed reactor, and the logistics direction in this reactor is descending, and the gas-solid axial backmixing is little, and radially concentration distribution is even, and its flow pattern is more near the ideal plug flow; The gas-solid residence time is short and consistent, helps making full use of the high-activity high-selectivity of catalyzer; The agglomeration of particles degree weakens greatly, makes gas velocity, particle speed and granule density radial distribution more even.Descending bed exit gas-solid speed is suitable, and when descending bed was longer, solid speed was faster than gas velocity, and the easier realization of gas-solid divides soon.Be applicable to the inlet device of this reactor, a catalyst distributor is equipped with in its inside, can realize granules of catalyst uniform fast, simple in structure, turndown ratio is big, pressure drop is little and equipment and abrasion of particles are little; Also used a kind of fast gas-solid separator, separation efficiency can reach more than 97%, and its particle residence time is below 100 milliseconds, the gas phase residence time is below 2 seconds, can realize the sharp separation of catalyzer and gas products, in time stopped reaction reduces the generation of secondary reaction.System of the present invention, can satisfy the needs of a large amount of heat releases in this reaction process, reaction one regeneration and the ultrashort contact process of plug flow, make that non-olefinic series products yield further reduces in the process, reduced the difficulty of follow-up separation process simultaneously, greatly improve the economy of process.Same fixed bed, fluidized-bed are compared, and the treatment capacity of dme or methyl alcohol improves greatly, and its transformation efficiency is greater than 98%, and the yield of ethene, propylene and butylene is greater than 93%.
Description of drawings
Fig. 1 is a process flow diagram of the present invention, wherein:
The 1st, the inlet device on the reactor, the 2nd, the feed(raw material)inlet, the 3rd, catalyst inlet, the 4th, the sparger in the reactor, the 5th, the ultrashort contact reactor of gas-solid cocurrent flow descending formula fluidized-bed, the 6th, wall-attached cutting type gas-solid quick disconnector, the 7th, later separation workshop section, the 8th, stripper, the 9th, stripped vapor, the 10th, revivifier, the 11st, follow-up waste heat recovery workshop section, the 12nd, interchanger, the 13rd, regeneration air, the 14th, catalyst control valve, the 15th, the catalyzer storage tank, the 16th, catalyst control valve, the 17th, ball valve, the 18th, regenerator promotes line.
Embodiment
Below in conjunction with description of drawings technical process of the present invention and embodiment:
Raw material (methyl alcohol or dme) enters reactor 5 by inlet device 1.This inlet device is a kind of catalyst inlet device that is applicable to the gas-solid cocurrent flow descending bed reactor, comprises the inlet of crust of the device and descending-bed reactor main body.Crust of the device is the turbulent flow mixing zone with the coaxial installation of descending-bed reactor main body, crust of the device top; Uniform carrier gas inlet pipeline on the sidewall circumference of shell; The catalyst transport pipeline is housed on the lower sides of carrier gas inlet, and loosening wind sparger is equipped with in the annular space bottom, and loosening wind inlet duct (CN12675434) is housed on the side wall of outer shell of sparger below.Catalyzer (SAP034) enters reactor 5 behind sparger 4, catalyzer contacts, reacts in reactor 5 with raw material.Reaction product and catalyzer together enter quick disconnector 6.This quick disconnector is a kind of wall-attached cutting type fast gas-solid separator, comprises transition section, gas-solid mixed phase inlet, separator main body, gas eduction tube and particle outlet.Transition section and reactor body link, and particle outlet and stripper plant link, gas eduction tube and follow-up gas solid separation system link (CN1267564).The isolating gas phase of quick disconnector is a reaction product, enters follow-up workshop section 7 and carries out further condensation separation.The catalyzer of reaction back inactivation enters stripper 8 by gas-solid quick disconnector 6 bottoms, uses the hydrocarbons on stripped vapor 9 stripping catalysts.The catalyzer of inactivation enters in the revivifier 10, and catalyzer is regenerated therein.The heat that the revivifier coke-burning regeneration generates is taken out by interchanger 12, and the flue gas of generation is to waste heat boiler, and the catalyzer after the regeneration enters regenerator stripping line 18 through ball valve 17, is carried through inlet device by lifting gas to enter in the down-flow reactor, finishes circulating reaction.Reaction conditions is the pressure 0.01～1.0MPa in the reactor, 450～650 ℃ of temperature of reaction, and the residence time is 0.1～10sec, agent-oil ratio 5～30; 500～800 ℃ of regeneration temperatures.When system stops in emergency, regenerated catalyst is discharged into storage tank 15 by control valve 14; When need replenished fresh catalyzer, the catalyzer in the storage tank entered regenerator by control valve 16 and promotes line 18 participation circulating reactions.
Embodiment 1:
React at gas-solid cocurrent flow descending formula circulating fluid bed reactor.Charging is a dme, liquid phase feeding, and catalyzer adopts SAPO34, and temperature of reactor is 460 ℃, and regenerator temperature is 510 ℃, and the residence time is 10 seconds, agent-oil ratio is 30, reacts under 0.01MPa.The dimethyl ether conversion rate is 99%, and in the hydro carbons resultant, the ethene proportion is 60%, and the propylene proportion is 25%, and the butylene proportion is 8%, and the yield of product low-carbon alkene is 93%.
Embodiment 2:
React at gas-solid cocurrent flow descending formula circulating fluid bed reactor.Charging is a dme, gas-phase feed, and catalyzer adopts SAPO34, and temperature of reactor is 530 ℃, and regenerator temperature is 650 ℃, and the residence time is 5 seconds, agent-oil ratio is 18, reacts under normal pressure.The dimethyl ether conversion rate is 99%, and in the hydro carbons resultant, the ethene proportion is 63%, and the propylene proportion is 24%, and the butylene proportion is 7%, and the yield of product low-carbon alkene is 95%.
Embodiment 3:
React at gas-solid cocurrent flow descending formula circulating fluid bed reactor.Charging is the mixture of dme and water, gas-phase feed, and catalyzer adopts SAPO34, and the mol ratio of dme and water is 1: 0.5, and temperature of reactor is 650 ℃, and regenerator temperature is 780 ℃, and the residence time is 0.2 second, and agent-oil ratio is 5, reacts under 0.95MPa.The dimethyl ether conversion rate is 99%, and in the hydro carbons resultant, the ethene proportion is 62%, and propylene is 24%, and butylene is 7%, and the yield of product low-carbon alkene is 94%.
Embodiment 4:
React at gas-solid cocurrent flow descending formula circulating fluid bed reactor.Charging is the mixture of methyl alcohol and water, liquid phase feeding, and catalyzer adopts SAPO34, and the mol ratio of methyl alcohol and water is 1: 0.2, and temperature of reactor is 600 ℃, and regenerator temperature is 750 ℃, and the residence time is 1 second, and agent-oil ratio is 10, reacts under normal pressure.The dimethyl ether conversion rate is 99%, and in the hydro carbons resultant, the ethene proportion is 59%, and propylene is 24%, and butylene is 10%, and the yield of product low-carbon alkene is 93%.
Embodiment 5:
React at gas-solid cocurrent flow descending formula circulating fluid bed reactor.Charging is a methyl alcohol, gas-phase feed, and catalyzer adopts SAP034, and temperature of reactor is 630 ℃, and regenerator temperature is 800 ℃, and the residence time is 3 seconds, agent-oil ratio is 18, reacts under 0.3MPa.Methanol conversion is 99%, and in the hydro carbons resultant, the ethene proportion is 62%, and propylene is 23%, and butylene is 8%, and the yield of product low-carbon alkene is 93%.
Claims (3)
1. processing method of producing low-carbon alkene by methyl alcohol or dme, this method is carried out successively as follows:
A. raw material enters the ultrashort contact reactor of gas-solid cocurrent flow descending formula fluidized-bed (5) via inlet device (1) from top, the sparger (4) of catalyzer in being arranged on inlet device (1) distributes in advance, the reactor (5) of flowing through from top to bottom, its agent-oil ratio is 5～30;
B. catalyzer and raw material are 450～650 ℃ in temperature, and pressure is to contact in reactor under 0.01～1.0MPa condition, react, and the control residence time is between 0.1～10 second;
C. the material that is come out by reactor bottom enters gas-solid quick disconnector (6), carries out separating treatment, makes reaction product and catalyzer sharp separation, and isolated gas-phase product enters follow-up workshop section (7) and handles, and promptly obtains the purpose product;
D. the catalyzer of reaction back inactivation enters stripper (8) by separator (6) bottom, remove hydrocarbons on the catalyzer with stripped vapor (9), enter then in the revivifier (10), under 500～800 ℃ of temperature, carry out coke-burning regeneration, the heat that coke-burning regeneration generates is taken out by interchanger (12), and the catalyzer after the regeneration enters regenerator from regenerator bottoms through ball valve (17) and promotes line (18), is carried by lifting gas and enters inlet device, it is entered in the reactor, finish circulating reaction;
E. when system stops in emergency, regenerated catalyst is discharged into storage tank (15) by control valve (14); When need replenished fresh catalyzer, the catalyzer in the storage tank (15) entered catalyzer by control valve (16) and promotes line (18) participation circulating reaction.
2. according to the described processing method of claim 1, it is characterized in that raw material be pure Dimethyl ether, methyl alcohol or its respectively with the mixture of water, adopt gas phase or liquid phase feeding.
3. system that is used to realize the described method of claim 1, this system comprises:
An inlet device (1) that is arranged on reactor head, its inside is provided with a catalyst distributor (4) and a feed(raw material)inlet (2);
A ultrashort contact reactor of gas-solid cocurrent flow descending formula fluidized-bed (5), its bottom links to each other with gas-solid quick disconnector (6), and this gas-solid quick disconnector (6) bottom is provided with a stripper (8);
A revivifier (10), this revivifier (10) links to each other with stripper (8) by pipeline; The interchanger (12) that the heat that decaying catalyst coke-burning regeneration in the revivifier is generated is taken out, this interchanger (12) links to each other with revivifier (10);
A catalyzer storage tank (15), its top links together by pipeline and the revivifier that control valve (14) is housed, and its underpart promotes line (18) by the pipeline that catalyst control valve (16) is housed with regenerator and links to each other;
Revivifier (10) bottom promotes line (18) by the pipeline that catalyst control valve (17) is housed with regenerator and links to each other, and this regenerator promotes line (18) and links to each other with inlet device (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011441887A CN1156416C (en) | 2001-12-14 | 2001-12-14 | Process and system for preparing low-carbon olefin from methanol or dimethylether |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB011441887A CN1156416C (en) | 2001-12-14 | 2001-12-14 | Process and system for preparing low-carbon olefin from methanol or dimethylether |
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| CN1156416C true CN1156416C (en) | 2004-07-07 |
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| CN101165019B (en) * | 2006-10-20 | 2010-06-16 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene |
| CN101177374B (en) * | 2006-11-07 | 2011-06-01 | 中国科学院大连化学物理研究所 | Method for producing propylene by carbinol or dimethyl ether |
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2001
- 2001-12-14 CN CNB011441887A patent/CN1156416C/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101723778B (en) * | 2009-11-27 | 2013-10-16 | 清华大学 | Coupling process method for preparing alkene with alcohol or ether and dehydrogenating alkane |
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