CN204544211U - A kind of catalyst recovery system and MTO reaction system - Google Patents
A kind of catalyst recovery system and MTO reaction system Download PDFInfo
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- CN204544211U CN204544211U CN201520207866.XU CN201520207866U CN204544211U CN 204544211 U CN204544211 U CN 204544211U CN 201520207866 U CN201520207866 U CN 201520207866U CN 204544211 U CN204544211 U CN 204544211U
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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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The utility model provides a kind of catalyst recovery system and MTO reaction system.This catalyst recovery system comprises catalyst separation unit and catalyst recovery unit, and catalyst recovery unit is communicated with by the first pipeline with catalyst separation unit; This catalyst recovery system also comprises heat exchanger, and be arranged on the catalyst heating of the agent of self-catalysis in the future separative element on the first pipeline, heat exchanger and the first pipeline are isolated.The mixture of catalyst and gas product is separated at catalyst separation unit by the catalyst recovery system in the utility model, gas product is recovered, catalyst then enters heat exchanger, catalyst obtains heat by heat exchanger, moisture is wherein evaporated, avoid the caking phenomenon of catalyst, catalyst presents with the state of fine powder, thus avoids the blockage problem of catalyst at the first pipeline.
Description
Technical field
The utility model relates to chemical field, in particular to a kind of catalyst recovery system and MTO reaction system.
Background technology
MTO (Methanol to Olefins) refers to the technology being manufactured low-carbon alkene (ethene, propylene etc.) by methyl alcohol, key reaction principle is that methyl alcohol first dewaters and generates dimethyl ether (DME), and then the equilibrium mixture of DME and material benzenemethanol dewaters and continues to be converted into the low-carbon alkene based on ethene, propylene.Low-carbon alkene is most important basic organic chemical industry raw material, and the market demand is vigorous.Because petroleum resources are day by day exhausted, crude oil price remains high, and traditional low-carbon alkene production line (naphtha pyrolysis gained alkene) will face the challenge of raw material supply anxiety.MTO technology successful commercialization, by opening up a brand-new Modern Coal-based Chemical technology path, has resources advantage and economic advantages, has great importance to energy development.
MTO technique is as fluidized-bed reaction, catalyst constantly runs damage in course of reaction, reactor is entrained with in order to prevent catalyst granules, many groups one secondary cyclone is provided with in prior art reactor, reactor outlet pipeline is provided with a three-stage cyclone separator, three sides of screwing off arrange catalyst fines collecting tank, when catalyst fines is normal by the mode of pumping to dead catalyst tank, but because MTO reaction generates large water gaging, have following problem:
(1) reacting gas of a small amount of water entrainment enters in collecting tank with catalyst fines through three spin material legs, and temperature step-down makes catalyst agglomeration, and feed-line blocks, and cannot be transported to dead catalyst tank.
(2) in dead catalyst tank, owing to containing moisture in catalyst, very easily luming, making troubles to transporting entrucking from now on.
(3) a small amount of fuel gas can be carried secretly in catalyst segmentation, enter in dead catalyst tank, can contact with air, although the amount of combustible gas gas is little, still there is potential safety hazard.
Therefore, be necessary to propose a kind of method, to solve problems of the prior art.
Utility model content
Main purpose of the present utility model is to provide a kind of catalyst recovery system and MTO reaction system, to solve the problem that catalyst water content in prior art causes more greatly luming.
To achieve these goals, according to an aspect of the present utility model, provide this catalyst recovery system a kind of and comprise catalyst separation unit and catalyst recovery unit, catalyst recovery unit is communicated with by the first pipeline with catalyst separation unit; This catalyst recovery system also comprises heat exchanger, is arranged on the first pipeline, and the catalyst heating of the agent of self-catalysis in the future separative element, heat exchanger and the first pipeline are isolated.
Further, catalyst recovery system also comprises catalyst conveying pot, and be communicated with the first pipeline and arrange by the catalyst transport of catalyst separation unit to catalyst recovery unit, heat exchanger is arranged in catalyst conveying pot; The tank skin of catalyst conveying pot is provided with the first sweep gas entrance of isolating with heat exchanger.
Further, the catalyst inlet position of catalyst conveying pot is lower than the catalyst outlet position of catalyst separation unit.
Further, catalyst recovery system also comprises combustible gas processing unit, and combustible gas processing unit is arranged on the first pipeline between catalyst conveying pot and catalyst recovery unit.
Further, the first pipeline between catalyst conveying pot and combustible gas processing unit is provided with the second sweep gas entrance.
Further, the first pipeline between catalyst conveying pot and combustible gas processing unit is also provided with the first valve and the second valve, the second sweep gas entrance is arranged between the first valve and the second valve.
Further, the first pipeline between catalyst conveying pot and catalyst separation unit is also provided with the 3rd valve.
Further, catalyst separation unit also comprises cyclone separator and catalyst collection device, and catalyst collection device is communicated with by the second pipeline with cyclone separator, and is communicated with catalyst conveying pot by the first pipeline.
Further, cyclone separator comprises multi-cyclone.
Further, the top of catalyst conveying pot is provided with open top, arranges the 3rd pipeline between the entrance of the afterbody cyclone separator of multi-cyclone and open top.
According to another aspect of the present utility model, additionally provide a kind of MTO reaction system, this MTO reaction system comprises catalyst recovery system, and this catalyst recovery system is above-mentioned arbitrary catalyst recovery system.
Application the technical solution of the utility model, the mixture of catalyst and gas product is opened catalyst separation unit is separated, gas product is recovered, catalyst then enters heat exchanger, catalyst obtains heat by heat exchanger, moisture is wherein evaporated, avoid the caking phenomenon of catalyst, catalyst presents with the state of fine powder, thus avoid the blockage problem of catalyst at the first pipeline, and then save by artificial by caking catalyst from catalyst separation shipped to the process of catalyst recovery unit.
Accompanying drawing explanation
The Figure of description forming a application's part is used to provide further understanding of the present utility model, and schematic description and description of the present utility model, for explaining the utility model, is not formed improper restriction of the present utility model.In the accompanying drawings:
Fig. 1 shows the structural representation of the catalyst recovery system provided according to a kind of preferred embodiment of the utility model;
Fig. 2 shows the structural representation of the catalyst recovery system provided according to a kind of preferred embodiment of the utility model;
Fig. 3 shows A place partial enlarged drawing in the catalyst recovery system shown in Fig. 2.
Detailed description of the invention
It should be noted that, when not conflicting, the embodiment in the application and the feature in embodiment can combine mutually.Below with reference to the accompanying drawings and describe the utility model in detail in conjunction with the embodiments.
Introduce as background technology part, in prior art, there is the problem of catalyst agglomeration.In order to address this problem, in a kind of typical embodiment of the utility model, provide a kind of catalyst recovery system, as shown in Figure 1, this catalyst recovery system comprises: catalyst separation unit 10 and catalyst recovery unit 20, and catalyst recovery unit 20 is communicated with by the first pipeline 50 with catalyst separation unit 10; Above-mentioned catalyst recovery system also comprises: heat exchanger, is arranged on the first pipeline, and the catalyst heating of the agent of self-catalysis in the future separative element, heat exchanger and the first pipeline are isolated.
Application the technical solution of the utility model, the mixture of catalyst and gas product is opened catalyst separation unit 10 is separated, gas product is recovered, catalyst then enters heat exchanger 31, catalyst obtains heat by heat exchanger 31, moisture is wherein evaporated, avoid the caking phenomenon of catalyst, catalyst presents with the state of fine powder, thus avoid the blockage problem of catalyst at the first pipeline 50, and then save by artificial process caking catalyst being transported to catalyst recovery unit 20 from catalyst separation unit 10; And above-mentioned heat exchanger 31 and the first pipeline 50 are isolated, the heat transferring medium avoided in heat exchanger 31 directly contacts with catalyst and causes catalyst to be polluted, and realizes the heating utilizing heat exchanger 31 pairs of catalyst simultaneously.
Distance between above-mentioned catalyst separation unit and catalyst recovery unit can design according to needs of production, during distant between catalyst separation unit and catalyst recovery unit, power set are set by catalyst transport to catalyst recovery unit at catalyst transport unit, in a kind of preferred embodiment of the application, as shown in Figure 2, above-mentioned catalyst recovery system comprises catalyst conveying pot 32, to be arranged on the catalyst transport of catalyst separation unit 10 on the first pipeline 50 to catalyst recovery unit 20, heat exchanger 31 is arranged in catalyst conveying pot 32, the tank skin of catalyst conveying pot 32 is provided with the first sweep gas entrance 33 of isolating with heat exchanger 31.By above-mentioned catalyst transport unit, improve the transfer efficiency of catalyst, and optimize the technique effect improving catalyst and block in the first pipeline 50 further while utilizing conveying that this catalyst conveying pot 32 is catalyst to provide power, catalyst conveying pot 32 is also provided with sweep gas entrance simultaneously, carry out in the process of heat exchange at the thermal medium of catalyst and heat exchanger 31, the air-flow of coming in from sweep gas entrance makes catalyst catalyst conveying pot 32 in the random motion being similar to " Brownian movement ", namely the available heat contact area of catalyst and heat exchanger 31 is added, improve heat exchange efficiency.
In catalyst recovery system, such as arrange a size diameter is 2 meters, the catalyst conveying pot 32 of high 3 meters, not only can meet the catalyst last person amount of about 2 tons weekly, also be unlikely to because catalyst conveying pot 32 is excessive simultaneously, cause the increase of heat increase and the downstream transport pressure needing heat exchanger 31 to provide, therefore avoid the prolongation of machine cycle, reduce the depreciable cost of relevant device unit interval.
The position relationship of both utilizations can the motion of promoting catalyst such as in the another kind of preferred embodiment of the application, the catalyst inlet position of above-mentioned catalyst conveying pot 32 is lower than the catalyst outlet position of catalyst separation unit 10.As shown in Figure 2, utilize gravitional force that catalyst is transferred to catalyst separation unit 10 from catalyst conveying pot 32, decrease the Power output of production, reduce catalyst last person cost.Certainly, the set-up mode of above-mentioned two kinds of embodiments can be in conjunction with, to realize better catalyst transport effect.
In another embodiment of the application, above-mentioned catalyst recovery system also comprises combustible gas processing unit 40, and combustible gas processing unit 40 is arranged on the first pipeline 50 between catalyst conveying pot 32 and catalyst recovery unit 20.Remove by the combustible gas processing unit 40 shown in Fig. 2 the fuel gas be mixed with in catalyst, reduce the potential safety hazard in final catalyst recovery unit 20 processing procedure.
Because catalyst can not be separated with gas product with catalyst conveying pot 32 completely at catalyst separation unit 10, simultaneously in order to ensure the operability unloading catalyst process, all inoxidable or inert environments in catalyst separation unit 10 and catalyst conveying pot 32, in this inoxidable or inert environments, whole system is safe; But when the combustible gas scale of construction in catalyst is more, by catalyst transport to catalyst recovery unit 20 time, owing to touching the oxygen-containing gas such as air, potential safety hazard may be there is, the combustible gas processing unit 40 arranged in above-described embodiment can make the combustible gas Thorough combustion wherein in catalyst, thus reach the problem removed and be mixed with a certain amount of combustible gas in catalyst, reduce the potential safety hazard in final catalyst recovery unit 20 processing procedure.
In order to the catalyst recovery system that makes there is combustible gas processing unit 40, there is higher operating efficiency, the first pipeline 50 between preferred above-mentioned catalyst conveying pot 32 and combustible gas processing unit 40 is provided with the second sweep gas entrance 35.As shown in Figure 3, second sweep gas entrance 35 the smoothness that can ensure to be communicated with between catalyst conveying pot 32 with combustible gas processing unit 40 is set, ensure that carrying out smoothly of whole catalyst unloaded operation, so make catalyst recovery system there is higher operating efficiency.
In order to improve the operating efficiency of each structure of catalyst recovery system targetedly, as shown in Figure 3, the first pipeline 50 between preferred above-mentioned catalyst conveying pot 32 and combustible gas processing unit 40 is also provided with the first valve 34 and the second valve 36, second sweep gas entrance 35 is arranged between the first valve 34 and the second valve 36.Arranging of this structure can make the work of pipeline between dredging catalyst conveying pot 32 and combustible gas processing unit 40 have more directionality, improves the specific aim of dredging work, and then improves the operating efficiency of unloading in the carried catalyst course of work.During line clogging such as between catalyst conveying pot 32 and the second sweep gas entrance 35, the second valve 36 can be closed, open the first valve 34 simultaneously, air-flow is all circulated by the direction of the first valve 34 to catalyst conveying pot 32 after entering pipeline from the second sweep gas entrance 35, the unicity in direction adds air flow pressure, is more conducive to the blocking in dredging pipeline.Same method can process when the line clogging problem between the second sweep gas entrance 35 and combustible gas processing unit 40.Do not block under normal circumstances at pipeline simultaneously, when the catalyst in catalyst conveying pot 32 is transferred to the later stage of combustible gas processing unit 40, the first valve 34 can be closed and open the second valve 36 simultaneously, utilize air-flow accelerator activator to the transfer of combustible gas processing unit 40.
In order to save the use cost of catalyst recovery system, as shown in Figure 3, the first pipeline 50 between preferred above-mentioned catalyst conveying pot 32 and catalyst separation unit 10 is also provided with the 3rd valve 37, the 3rd valve 37 is utilized to control the conveying opportunity of catalyst, when catalyst isolated in catalyst separation unit 10 is less also do not meet transport condition time, 3rd valve 37 can be closed, open again when needs are carried; When catalyst shifts completely from catalyst separation unit, close the 3rd valve 37.
Those skilled in the art also can be provided with the opportunity that thermometer is used to refer to the separation of catalyst needs in the porch of catalyst conveying pot 32, this is because: because exothermic reaction or the endothermic reaction can make the temperature of final gas product and catalyst there are differences, therefore whether the diversity judgement catalyst that thermometer can be utilized to respond to gas product and catalyst final temperature shifts completely, during from catalyst separation unit 10 to catalyst conveying pot 32 transfer catalyst, when the temperature of temperature close to gas product of thermometer index display, can judge that catalyst shifts substantially completely, now can close the 3rd valve 37, cut-out catalyst separation unit 10 is communicated with catalyst conveying pot 32, carry out above-mentioned catalyst warm-up operation.
In above-mentioned catalyst recovery system, catalyst separation unit 10 can adopt the set-up mode of the catalyst separation unit of prior art routine to arrange, in a kind of preferred embodiment of preferred the application, above-mentioned catalyst separation unit 10 comprises: cyclone separator 11 and catalyst collection device 12, catalyst collection device 12 is communicated with by the second pipeline 60 with cyclone separator 11, and is communicated with catalyst conveying pot 32 by the first pipeline 50.Gas product and catalyst separately can be collected pretreated catalyst simultaneously by this structure.
After the mixture of gas product and catalyst enters cyclone separator 11, circumferential high velocity air is utilized gas product and catalyst to be separated, gas product leaves from the top of cyclone separator 11, catalyst, then because gravity fall is to catalyst collection device 12, reaches the object of collection catalyst while of gas product and catalyst separation.In order to the separating effect of optimization of catalysts, preferred above-mentioned cyclone separator 11 comprises multi-cyclone, with can making gas product and catalyst separation comparatively thorough.
In another preferred embodiment of the application, as shown in Figure 2, the top of above-mentioned catalyst conveying pot 32 is provided with open top, arranges the 3rd pipeline 70 between the entrance of the afterbody cyclone separator of multi-cyclone and open top.Under the prerequisite that catalyst separation unit 10 is connected with catalyst conveying pot 32, catalyst separation unit 10 and catalyst conveying pot 32 are formed a closed-loop path by the 3rd pipeline 70 and the first pipeline 50, and this kind of structure can make the gas pressure in catalyst conveying pot 32 be unlikely to excessive and cause catalyst emission difficulty.
Simultaneously the height on catalyst inlet distance ground is lower than the height on the catalyst outlet distance ground of catalyst separation unit 10, utilize the gravitional force of catalyst like this, catalyst transfers to catalyst conveying pot 32 from catalyst separation unit 10 gradually, simultaneously in catalyst conveying pot 32, the gas be mixed with in catalyst enters again catalyst separation unit 10 by Returning outlet, ensure that the dynamic circulation of whole process, be conducive to catalyst is transferred to catalyst conveying pot 32 continuity from catalyst separation unit 10.
In the another kind of typical embodiment of the utility model, additionally provide a kind of MTO reaction system, MTO reaction system comprises catalyst recovery system, and MTO reaction system is above-mentioned arbitrary catalyst recovery system.Catalyst recovery system in the utility model can make whole MTO reaction system more efficient.
The foregoing is only preferred embodiment of the present utility model, be not limited to the utility model, for a person skilled in the art, the utility model can have various modifications and variations.All within spirit of the present utility model and principle, any amendment done, equivalent replacement, improvement etc., all should be included within protection domain of the present utility model.
Claims (11)
1. a catalyst recovery system, comprising:
Catalyst separation unit (10);
Catalyst recovery unit (20), is communicated with by the first pipeline (50) with described catalyst separation unit (10);
It is characterized in that, described catalyst recovery system also comprises:
Heat exchanger (31), be arranged on described first pipeline (50), to heat from the catalyst of described catalyst separation unit (10), described heat exchanger (31) and described first pipeline (50) are isolated.
2. catalyst recovery system according to claim 1, it is characterized in that, described catalyst recovery system also comprises catalyst conveying pot (32), be communicated with described first pipeline (50) and arrange, by the catalyst transport of described catalyst separation unit (10) to described catalyst recovery unit (20), described heat exchanger (31) is arranged in described catalyst conveying pot (32);
The tank skin of described catalyst conveying pot (32) is provided with the first sweep gas entrance (33) of isolating with described heat exchanger (31).
3. catalyst recovery system according to claim 2, is characterized in that, the catalyst inlet position of described catalyst conveying pot (32) is lower than the catalyst outlet position of described catalyst separation unit (10).
4. catalyst recovery system according to claim 2, it is characterized in that, described catalyst recovery system also comprises combustible gas processing unit (40), and described combustible gas processing unit (40) is arranged on described first pipeline (50) between described catalyst conveying pot (32) and described catalyst recovery unit (20).
5. catalyst recovery system according to claim 4, it is characterized in that, the first pipeline (50) between described catalyst conveying pot (32) and described combustible gas processing unit (40) is provided with the second sweep gas entrance (35).
6. catalyst recovery system according to claim 5, it is characterized in that, the first pipeline (50) between described catalyst conveying pot (32) and described combustible gas processing unit (40) is also provided with the first valve (34) and the second valve (36), described second sweep gas entrance (35) is arranged between described first valve (34) and described second valve (36).
7. catalyst recovery system according to claim 2, it is characterized in that, the first pipeline (50) between described catalyst conveying pot (32) and described catalyst separation unit (10) is also provided with the 3rd valve (37).
8. catalyst recovery system according to claim 2, is characterized in that, described catalyst separation unit (10) comprising:
Cyclone separator (11);
Catalyst collection device (12), is communicated with by the second pipeline (60) with described cyclone separator (11), and is communicated with described catalyst conveying pot (32) by described first pipeline (50).
9. catalyst recovery system according to claim 8, is characterized in that, described cyclone separator (11) comprises multi-cyclone.
10. catalyst recovery system according to claim 9, it is characterized in that, the top of described catalyst conveying pot (32) is provided with open top, arranges the 3rd pipeline (70) between the entrance of the afterbody cyclone separator of described multi-cyclone and described open top.
11. 1 kinds of MTO reaction systems, described MTO reaction system comprises catalyst recovery system, it is characterized in that, the catalyst recovery system of described catalyst recovery system according to any one of claim 1 to 10.
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| CN201520207866.XU CN204544211U (en) | 2015-04-08 | 2015-04-08 | A kind of catalyst recovery system and MTO reaction system |
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| CN201520207866.XU CN204544211U (en) | 2015-04-08 | 2015-04-08 | A kind of catalyst recovery system and MTO reaction system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106563498A (en) * | 2016-11-03 | 2017-04-19 | 神华集团有限责任公司 | Method and device for cyclically utilizing methanol-to-olefin fine catalyst powder |
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2015
- 2015-04-08 CN CN201520207866.XU patent/CN204544211U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106563498A (en) * | 2016-11-03 | 2017-04-19 | 神华集团有限责任公司 | Method and device for cyclically utilizing methanol-to-olefin fine catalyst powder |
| CN106563498B (en) * | 2016-11-03 | 2019-05-24 | 神华集团有限责任公司 | A kind of method and device that methanol-to-olefin catalyst fine powder recycles |
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