CN103242124B - A kind of reaction-regeneration system of organic oxygen-containing compound producing light olefins - Google Patents
A kind of reaction-regeneration system of organic oxygen-containing compound producing light olefins Download PDFInfo
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- CN103242124B CN103242124B CN201310192161.0A CN201310192161A CN103242124B CN 103242124 B CN103242124 B CN 103242124B CN 201310192161 A CN201310192161 A CN 201310192161A CN 103242124 B CN103242124 B CN 103242124B
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- 238000011069 regeneration method Methods 0.000 title claims abstract description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 18
- 239000001301 oxygen Substances 0.000 title claims abstract description 18
- 150000001875 compounds Chemical class 0.000 title claims abstract description 17
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 14
- 239000003054 catalyst Substances 0.000 claims abstract description 63
- 238000006253 efflorescence Methods 0.000 claims abstract description 17
- 206010037844 rash Diseases 0.000 claims abstract description 17
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 15
- 230000008929 regeneration Effects 0.000 claims abstract description 10
- 238000000034 method Methods 0.000 claims description 41
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 18
- 239000002245 particle Substances 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 2
- 239000000779 smoke Substances 0.000 claims description 2
- 230000008646 thermal stress Effects 0.000 abstract description 4
- 230000009849 deactivation Effects 0.000 abstract 1
- 230000002779 inactivation Effects 0.000 description 16
- 239000007789 gas Substances 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 13
- 230000008569 process Effects 0.000 description 12
- 239000000843 powder Substances 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 9
- 239000008187 granular material Substances 0.000 description 8
- 238000012545 processing Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000004913 activation Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 2
- 230000008642 heat stress Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000168486 Causus Species 0.000 description 1
- 229910004283 SiO 4 Inorganic materials 0.000 description 1
- 230000004308 accommodation Effects 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 125000001145 hydrido group Chemical group *[H] 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- 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
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a kind of reaction-regeneration system of organic oxygen-containing compound producing light olefins, described system comprises: reactor, works at 400-550 DEG C; Revivifier, works at 600-800 DEG C, de-carbon regeneration in described revivifier after catalyst deactivation; Decaying catalyst transport pipe; Regenerated catalyst road, in addition, also has at least one interchanger between described decaying catalyst transport pipe and described revivifier, for reducing the temperature of decaying catalyst when entering described revivifier and the difference of described revivifier working temperature.Reaction-regeneration system of the present invention effectively can reduce catalyzer causes catalyzer efflorescence loss problem because the violent temperature difference produces thermal stresses.
Description
Technical field
The present invention relates to a kind of reaction-regeneration system of organic oxygen-containing compound producing light olefins, also relate to a kind of method reducing the catalyzer efflorescence loss of organic oxygen-containing compound producing light olefins.
Background technology
Organic oxygen-containing compound, such as methyl alcohol and/or dimethyl ether low-carbon alkene technology open by the new technology route of coal production basic organic chemical industry raw material, and typical technology is methanol-to-olefins (MTO), and it take methyl alcohol as olefin production mixture.Typically, MTO complete set technology is made up of reaction technology and isolation technique.Reaction technology is designed to core with catalyst preparation and reactor development; Product slates and purity requirement are then the bases of exploitation separating technology.
The whole process of MTO technique can be divided into reaction-regeneration system and reaction gas separation system two portions.Reactive moieties only has gas-solid two-phase, and this catalyzed reaction is thermopositive reaction.The catalyzer of inactivation need fire charcoal regeneration in fluid bed regenerator, then, returns in fluidized-bed reactor and continues reaction.Reactor and revivifier are all provided with heat-transfering device.
MTO is actually the technique being converted into low-carbon alkene by synthesis gas through methanol.Some famous oil and chemical companies in the world, as Exxon Mobil Corporation (Exxon – Mobil), BASF AG (BASF), AP Oil company (UOP) and Hydro company (Norsk Hydro) all drop into substantial contribution and personnel, years of researches are carried out.
In general, organic oxygen-containing compound producing light olefins technology is increasingly mature, and reach can heavy industrialization or business-like degree, particularly various MTO technique, its technology is more ripe, industrialization experience is abundanter, and at present, the representational MTO technique of most mainly comprises: UOP/Hydro technique, change institute's (DMTO) technique and ExxonMobil technique greatly.
At present, although MTO technique is ripe, carry out the practical problems also encountered in heavy industrialization or business-like process in some engineerings in MTO technique.MTO reacting middle catalyst is easy to carbon distribution inactivation, successive reaction, regenerative operation need be carried out to catalyzer, in the reaction-regeneration system of fluidized-bed structure, the wearing and tearing that cold, causus, the mutual collision of the play of granules of catalyst and catalyzer produce in equipment surface motion, cause catalyzer that efflorescence loss in use occurs.Such as, particle diameter is less than 10 microns, is particularly less than the conventional gas-particle separation device of the granules of catalyst of 5 microns, such as cyclonic separator has been difficult to them to separate from product gas, these catalyst fines and/or fine powder by the product band of gas to product separating technique middle and lower reaches workshop section, such as, when taking in quench tower, water wash column, quenched water wet cyclone and various interchanger, the reduction of these plant efficiencies, operational anomaly can be caused, or even equipment blocks and maintenance shut-downs of having to, this will increase labour intensity and equipment running maintenance cost.Therefore, avoid MTO product gas hold the catalyst fines wrapped up in and/or fine powder under the arm to enter product separating technique best bet be exactly the growing amount reducing these catalyst fines and/or fine powder in reaction-regeneration system, namely reduce the efflorescence loss of catalyzer in reaction-regenerative process.
US6166282 discloses a kind of fast fluidized bed reactor for MTO technique, the document describes the internal structure of this MTO reactor in detail, the form that the distribution of material and the flow direction, especially catalyzer are separated in the reactor, but do not relate to the efflorescence loss how avoiding catalyzer.
CN101811071B discloses the control method of decaying catalyst coke-burning regeneration in methanol-to-olefins process, the method controls the oxygen level of regenerative combustion medium by increase auxiliary chamber, thus improve the efficiency of making charcoal of decaying catalyst, and then improve the regenerative power of decaying catalyst, finally reach the object improving yield of light olefins, but the document does not relate to the problem how avoiding catalyzer efflorescence loss yet.
Above-mentioned patent documentation is introduced with for referencial use in full at this.
But, so far, also do not find a good method reducing catalyzer efflorescence loss in reaction-regenerative process.The present invention is devoted to solve the problems of the technologies described above, and strives finding the Regulations solved the problem.
Summary of the invention
According to a first aspect of the invention, provide a kind of reaction-regeneration system of organic oxygen-containing compound producing light olefins, described system comprises: reactor, works at 400-550 DEG C; Revivifier, works at 600-800 DEG C, and decaying catalyst is de-carbon regeneration in described revivifier; Decaying catalyst transport pipe, is communicated with described reactor and described revivifier, enters in described revivifier for making decaying catalyst by described reactor; Regenerated catalyst road, be communicated with described revivifier and described reactor, enter in described reactor for making regenerated catalyst by described revivifier, it is characterized in that: between described decaying catalyst transport pipe and described revivifier, also there is at least one interchanger, for reducing the temperature of decaying catalyst when entering described revivifier and the difference of described revivifier working temperature.
Usually, the example of described organic oxygen-containing compound can be methyl alcohol and/or dme; The example of described low-carbon alkene can be ethene and/or propylene.Preferably, described interchanger is straight pipe type well heater or the jacketed type well heater of vertical arrangement; Described reactor and/or revivifier are reactor and/or the revivifier of fluidized-bed structure, and wherein, described reactor and/or internal regenerator have cyclonic separator for gas-particle separation or cyclonic separator cascade;
Preferably, the difference of the temperature of decaying catalyst when entering described revivifier and described revivifier working temperature is less than 200 DEG C; Described catalyzer is SAPO-34, and it is for having (SiO
4) and (AlO
4) the silicoaluminophosphamolecular molecular sieve catalyzer of unit; The heat transferring medium of described interchanger is the heat smoke of described revivifier generation or the pressurized air of heating.
According to a second aspect of the invention, a kind of method reducing the catalyzer efflorescence loss of organic oxygen-containing compound producing light olefins is provided, it is characterized in that: at least one interchanger is set between decaying catalyst transport pipe and catalyst regenerator, reducing the temperature of decaying catalyst when entering described revivifier and the difference of described revivifier working temperature.
In the above-mentioned methods, the difference of the temperature of described decaying catalyst when entering described revivifier and described revivifier working temperature is preferably less than 250 DEG C, is more preferably less than 200 DEG C, is most preferably less than 180 DEG C.
Accompanying drawing explanation
The Figure of description forming a specification sheets part of the present invention is used for being further explained the present invention; accompanying drawing of the present invention and explanation thereof are used for explaining the present invention in detail; to make those of ordinary skill in the art clearly understand essence of the present invention, it does not form any restriction to scope.
Fig. 1 is the schematic diagram of the reaction-regeneration system of organic oxygen-containing compound producing light olefins of the present invention.
Embodiment
The present invention is further explained in detail by the description below with reference to accompanying drawing, but below describe only for enabling general technical staff of the technical field of the invention clearly understand principle of the present invention and marrow, and do not mean that any type of restriction is carried out to the present invention.In accompanying drawing, equivalent or corresponding parts or the identical reference numerals of feature represent.
As shown in Figure 1, usually, the firsts and seconds whirlwind gas-particle separation device of the some groups of series connection of arranging in the expanding reach of MTO reactor top, MTO product gas and the overwhelming majority's (inactivation) to be generated granules of catalyst are separated, and (inactivation) to be generated granules of catalyst to be entered in revivifier by described reactor through pipeline and carries out de-carbon regeneration (activation); MTO product gas then leaves MTO reactor and enters three grades of whirlwind gas-particle separation devices, and MTO product gas is generally 800-900mg/m in solid particulate (a small amount of catalyst fines of carrying and/or the fine powder) concentration of three grades of whirlwind gas-particle separation device ingress
3, be generally 150-300mg/m in the concentration in three grades of whirlwind gas-particle separation device exits
3.Therefore, most catalyst fines and/or fine powder can be separated by three grades of whirlwind gas-particle separation devices, but still the catalyst fines of some particle diameter below 10 microns, particularly below 5 microns and/or fine powder, three grades of whirlwind gas-particle separation devices cannot be separated, they enter product separating technique middle and lower reaches workshop section with MTO product gas, and the equipment that have impact on product separating technique middle and lower reaches workshop section runs normally.
In order to reduce the catalyst fines and/or fine powder that enter product separating technique middle and lower reaches workshop section, best bet is exactly the growing amount reducing these catalyst fines and/or fine powder in reaction-regeneration system, namely reduces the efflorescence loss of catalyzer in reaction-regenerative process.
Usually, the particle diameter entering the live catalyst in the reaction-regeneration system of organic preparing low-carbon olefin from oxygen-containing compounds is 40-150 micron, theoretically, the gas-particle separation equipment of the complete available routine of the solid particulate of such particle diameter, such as 1-2 level cyclone cluster and/or cyclone cluster cascade are separated.
But in the process of organic oxygen-containing compound, such as methyl alcohol and/or dimethyl ether low-carbon alkene, need (inactivation) the to be generated catalyzer after by carbon deposit in reactor to be sent in revivifier by line of pipes and carry out coke-burning regeneration.Because the working temperature in revivifier is far above the working temperature of reactor, simultaneously, because line of pipes is longer, also there is the problem that (inactivation) to be generated catalyzer is lowered the temperature gradually in course of conveying, therefore, the temperature of reclaimable catalyst when entering revivifier and the temperature difference in revivifier very large.The violent temperature difference and frequently regenerative process will produce huge thermal stresses, this has larger impact to the physical properties of catalyzer, it is one of major reason of catalyzer efflorescence breakage, in addition, the wearing and tearing that the mutual collision of granules of catalyst and catalyzer produce in equipment surface motion are also the reasons causing granules of catalyst that efflorescence breakage in use occurs.
Catalyzer efflorescence breakage will cause the separation efficiency of the gas-solid cyclonic separator of 1-2 level to decline, a large amount of catalyst fines and/or fine powder is caused to be carried secretly in product separating technique middle and lower reaches workshop section, such as water wash column by MTO product gas, thus, considerably increase the wastage rate of catalyzer.At present, the price of catalyzer is very expensive, and a large amount of catalyst attritions not only increases the difficulty of subsequent technique, and also improves the Financial cost of system cloud gray model.
The present invention proposes first: between the transport pipe and revivifier of (inactivation) to be generated catalyzer, arrange at least one interchanger, before (inactivation) to be generated catalyzer enters revivifier, heat (inactivation) to be generated catalyzer, to improve its temperature, thus reduce the temperature difference of (inactivation) catalyzer to be generated and revivifier device inside, weaken the excessive heat stress that reclaimable catalyst produces in rapid heating or temperature-rise period, thus, avoid because temperature great change in (inactivation) the to be generated catalyzer short period of time produces huge and excessive heat stress, cause the problem of catalyzer efflorescence breakage, so in fact decrease the growing amount of catalyst fines and/or fine powder, thus reduce the efflorescence loss of catalyzer, these Industrial processes for organic oxygen-containing compound producing light olefins have great significance.
Now, composition graphs 1 and specific embodiment are described in further detail the present invention: as shown in Figure 1, reaction raw materials behind the close phase reaction district 1 that feed(raw material)inlet sparger 2 enters reactor and catalyzer react, product gas leaves reactor from the outlet 5 on reactor top, product gas entrained catalyst particles is in uphill process, granules of catalyst is separated in the settling section 4 of reactor gets off for the overwhelming majority, and remaining granules of catalyst is mainly separated by the gas-solid cyclonic separator 3 of 1-2 level.Catalyzer continuous carbon deposit, gradually inactivation after reaction in close phase reaction district 1, (inactivation) the to be generated catalyzer after carbon deposit enters reclaimable catalyst transport pipe 6, then after interchanger 10 is heated, enter regeneration in revivifier 7.Carbon deposit on reclaimable catalyst and regeneration gas react, regeneration gas is pressurized air, the useless flue gas produced in revivifier 7 is discharged by outlet 9, and regenerates the catalyzer after (activation) and enter in reactor by regenerated catalyst road 8, again participates in reacting.
In above process, because temperature when the useless flue gas produced in revivifier 7 is discharged from outlet 9 is higher, most Gao Shike is more than 800 DEG C, it can be used as the heat transferring medium that interchanger 10 uses completely, for heating (inactivation) the to be generated catalyzer going to revivifier 7, thus reduce the difference of the temperature of (inactivation) to be generated catalyzer when entering revivifier 7 and the working temperature in revivifier 7, to avoid reclaimable catalyst when entering revivifier 7, because bearing the violent temperature difference, inside produces huge thermal stresses, causes himself damaged by thermal stresses efflorescence.
Preferably, heat through above-mentioned interchanger 10, the difference of the temperature of (inactivation) to be generated catalyzer when entering revivifier 7 and the working temperature in revivifier 7 is less than 250 DEG C, is more preferably less than 200 DEG C, is most preferably less than 180 DEG C, such as, be less than 150 DEG C.
Below, by exemplary and non-limiting specific embodiment explains the present invention in further detail, essence of the present invention and marrow is clearly understood to make those of ordinary skill in the art.
Embodiment
Embodiment 1
Laboratory scale present system and technique shown in Fig. 1 is used to carry out the reaction-regenerative process of methanol-to-olefins product.
The interchanger 10 that the present embodiment 1 adopts is the jacketed type well heaters made by High-temperature resistant alloy material, and heating medium derives from the useless flue gas of revivifier 7, and its temperature is 800 DEG C.
The processing parameter that the present embodiment 1 adopts and experimental result thereof represent in the following Table 1.
Embodiment 2
Except changing except processing parameter, repeat the experimentation of embodiment 1, the processing parameter that the present embodiment 2 adopts and experimental result thereof are also illustrated in below in table 1.
Embodiment 3
Except changing except processing parameter, repeat the experimentation of embodiment 1, the processing parameter that the present embodiment 3 adopts and experimental result thereof are also illustrated in below in table 1.
Comparative example 1
Except not heating except being deleted by the well heater 10 shown in Fig. 1, to reclaimable catalyst, repeat the experimentation of embodiment 1, the processing parameter that this comparative example 1 adopts and experimental result thereof are also illustrated in below in table 1.
Table 1
From table 1 above: present system and method effectively reduce the catalyst fines of particle diameter mostly between 1-10 micron and/or the quantity of fine powder that 1-3 level whirlwind gas-particle separation device cannot be separated, prove: present invention process and method obviously slow down the efflorescence breakage of catalyzer in reaction-regenerative process, thus significantly reduce the segregational load of MTO product gas separating technology middle and lower reaches workshop section, avoid the problem of MTO product gas separating technology middle and lower reaches workshop section equipment operation exception, also improve the work-ing life of catalyzer simultaneously.
The term that this specification sheets is used and form of presentation are only used as descriptive and nonrestrictive term and form of presentation, are not intended to by any equivalents thereof exclude of the feature that represents and describe or its integral part outside when using these terms and form of presentation.
Although show and described several embodiment of the present invention, the present invention has not been restricted to described embodiment.On the contrary, those of ordinary skill in the art should recognize can carry out any accommodation and improvement to these embodiments when not departing from principle of the present invention and spirit, and protection scope of the present invention determined by appended claim and equivalent thereof.
Claims (8)
1. a reaction-regeneration system for organic oxygen-containing compound producing light olefins, described system comprises:
(1) reactor, works at 400-550 DEG C;
(2) revivifier, works at 600-800 DEG C, and decaying catalyst is de-carbon regeneration in described revivifier;
(3) decaying catalyst transport pipe, is communicated with described reactor and described revivifier, enters in described revivifier for making decaying catalyst by described reactor; With
(4) regenerated catalyst road, is communicated with described revivifier and described reactor, for making regenerated catalyst enter in described reactor by described revivifier,
It is characterized in that: between described decaying catalyst transport pipe and described revivifier, also there is at least one interchanger, for reducing the temperature of decaying catalyst when entering described revivifier and the difference of described revivifier working temperature,
Described interchanger is straight pipe type well heater or the jacketed type well heater of vertical arrangement, and the heat transferring medium of described interchanger is the heat smoke of described revivifier generation or the pressurized air of heating.
2. system according to claim 1, wherein, described organic oxygen-containing compound is methyl alcohol and/or dme; Described low-carbon alkene is ethene and/or propylene.
3. system according to claim 1, wherein, described reactor and/or revivifier are reactor and/or the revivifier of fluidized-bed structure.
4. system according to claim 1, wherein, described reactor and/or internal regenerator have cyclonic separator for gas-particle separation or cyclonic separator cascade.
5. system according to claim 1, wherein, the difference of the temperature of decaying catalyst when entering described revivifier and described revivifier working temperature is less than 200 DEG C.
6. system according to claim 1, wherein, described catalyzer is SAPO-34.
7. reduce a method for the catalyzer efflorescence loss of organic oxygen-containing compound producing light olefins,
It is characterized in that: at least one interchanger is set between decaying catalyst transport pipe and catalyst regenerator, reducing the temperature of decaying catalyst when entering described revivifier and the difference of described revivifier working temperature.
8. method according to claim 7, wherein, the difference of the temperature of described decaying catalyst when entering described revivifier and described revivifier working temperature is less than 200 DEG C.
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| CN102276383A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method of reducing runoff of catalysts in conversion of oxygen containing compounds to low carbon olefins |
| CN102276396A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for supplementing catalyst into methanol-to-olefin reaction and regeneration system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102276383A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method of reducing runoff of catalysts in conversion of oxygen containing compounds to low carbon olefins |
| CN102276396A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for supplementing catalyst into methanol-to-olefin reaction and regeneration system |
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| CN103242124A (en) | 2013-08-14 |
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