CN206624799U - Organic oxygen-containing compound olefin hydrocarbon apparatus - Google Patents
Organic oxygen-containing compound olefin hydrocarbon apparatus Download PDFInfo
- Publication number
- CN206624799U CN206624799U CN201720254117.1U CN201720254117U CN206624799U CN 206624799 U CN206624799 U CN 206624799U CN 201720254117 U CN201720254117 U CN 201720254117U CN 206624799 U CN206624799 U CN 206624799U
- Authority
- CN
- China
- Prior art keywords
- solid
- phase outlet
- gas
- outlet
- filter
- 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
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
- 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 utility model provides a kind of organic oxygen-containing compound olefin hydrocarbon apparatus.The device includes reactor, the first cyclone gas-solid separator, the second cyclone gas-solid separator, chilling tower and filter；Product gas outlet is provided with reactor, the first import, the first gaseous phase outlet and the first solid-phase outlet are provided with the first cyclone gas-solid separator, the first import is connected with product gas outlet；The second import, the second gaseous phase outlet and second solid phase outlet, the second import is provided with second cyclone gas-solid separator with the first solid-phase outlet to be connected；Chilling tower is connected with the first gaseous phase outlet, the second gaseous phase outlet；Filter is arranged in series between the second gaseous phase outlet and chilling tower.Said apparatus can carry out more fully gas solid separation to product gas, prevent these micro mists from entering chilling tower and causing equipment to block.
Description
Technical field
Organic synthesis field is the utility model is related to, in particular to a kind of organic oxygen-containing compound olefin hydrocarbon apparatus.
Background technology
The low-carbon alkenes such as ethene, propylene are basic materials important in modern petrochemical industry, existing olefin producing technologies pair
Petroleum resources rely on seriously, cause low-carbon alkene relation between supply and demand growing tension.It is lighter hydrocarbons that traditional ethene, propylene, which produce route,
(ethane, naphtha, light diesel fuel) oil pyrolysis chemical industry route, but this route is limited by that petroleum resources are limited, international oil price rises violently
Deng factors.Organic oxygen-containing compound, such as methanol and/or dimethyl ether alkene technology open to be had substantially by coal production
The new technology route of machine industrial chemicals, and wherein typical technology is methanol-to-olefins (MTO).Typically, methanol-to-olefins
Technique is that methanol is produced to the light olefin gaseous mixture based on ethene and propylene after fluidized catalytic reaction.
Currently, catalyst is developed on the basis of SAPO-34 molecular sieves used by most of MTO techniques.Although no
With some differences of the catalyst price of producer, but it is generally expensive, fluctuated in 200,000/ton of RMB, and in MTO
Technique carry out heavy industrialization or it is commercialized during also encounter the gas-particle separation problem of such as product gas.In methanol
In olefine reaction processed, catalyst is ciculation fluidized between reactor and regenerator, because the direct collision between catalyst granules
And catalyst moves caused abrasion in equipment surface, causes catalyst that the loss of catalyst fines occurs in use.
Particle diameter has been less than the gas-particle separation device of 10 μm, especially less than 5 μm of catalyst fines routine, such as cyclone separator
Through being difficult to separate them from product gas, and these catalyst fines and/or fine powder take product point to by product gas
Separating process middle and lower reaches workshop section, such as when taking in chilling tower, water scrubber and various heat exchangers, these unit efficiencies can be caused to drop
Low, operation exception, even equipment block and must not maintenance shut-downs, increase labor intensity, increase cost.
Patent CN 201310172475.4 discloses a kind of organic oxygen-containing compound olefin product gas-particle separation and changed
Hot systems and its technique, the patent are left in MTO product gas and added at least on process flow routes after three-stage cyclone separator
One heat exchanger and at least one filter, heat exchanger are used to reclaim the heat in product gas, and filter can be used for from product gas
In further separating catalyst fine grained and/or fine powder.But the technique and untreated MTO product gas leaves three-stage cyclone separation
Enter level Four after device and revolve catalyst entrained when dividing separator, this partial catalyst is separated by tetra-cyclone
Afterwards, still some catalyst can enter directly into chilling tower, in turn result in chilling tower bottom of towe, washing tower tray floor and various
Heat exchanger blocks.
Utility model content
Main purpose of the present utility model is to provide a kind of organic oxygen-containing compound olefin hydrocarbon apparatus, to solve existing skill
Solid particle removes halfway problem in organic oxygen-containing compound olefin product gas in art.
To achieve these goals, the utility model provides a kind of organic oxygen-containing compound olefin hydrocarbon apparatus, and it includes：
Reactor, product gas outlet is provided with reactor；First whirlwind gas-solid separator, set in the first whirlwind gas-solid separator
There are the first import, the first gaseous phase outlet and the first solid-phase outlet；First import is connected with product gas outlet；Second whirlwind is gas-solid
Separator, the second import, the second gaseous phase outlet and second solid phase outlet are provided with the second whirlwind gas-solid separator；Second enters
Mouth is connected with the first solid-phase outlet；Chilling tower, chilling tower are connected with the first gaseous phase outlet, the second gaseous phase outlet；And filtering
Device, filter are arranged in series between the second gaseous phase outlet and chilling tower.
Further, filter is at least one, and when filter is multiple, multiple filters are arranged in parallel second
Between gaseous phase outlet and chilling tower.
Further, multiple filters include purpose ceramic-film filter, metal powder sintered cartridge filter and electric precipitation mistake
It is at least one in filter.
Further, solid-phase catalyst outlet is additionally provided with reactor, reactor is internally provided with reaction chamber；Device
Also include：3rd whirlwind gas-solid separator, the 3rd whirlwind gas-solid separator are provided with triple feed inlet, the 3rd gaseous phase outlet and
Three solid-phase outlets；Triple feed inlet is connected with reaction chamber, and the 3rd solid-phase outlet is connected with solid-phase catalyst outlet；And the 4th whirlwind
Gas-solid separator, the 4th whirlwind gas-solid separator are provided with the 4th import, the 4th gaseous phase outlet and the 4th solid-phase outlet；4th
Import is connected with the 3rd gaseous phase outlet, and the 4th gaseous phase outlet is connected with product gas outlet, and the 4th solid-phase outlet and solid catalysis
Agent outlet is connected.
Further, device includes multiple chilling towers being set up in parallel.
Further, the 5th gaseous phase outlet is additionally provided with chilling tower；Device also includes water scrubber, water scrubber and the 5th gas
Mutually export and be connected.
Further, device includes multiple water scrubbers being arranged in parallel.
Further, device also includes heat exchanger, and heat exchanger is arranged in series between the first gaseous phase outlet and chilling tower.
Further, regenerated catalyst import is additionally provided with reactor；Device also includes regenerator, regenerator respectively with
Solid-phase catalyst outlet connects with regenerated catalyst import.
Further, device also includes back-blowing device, and blowback air outlet, blowback air outlet and mistake are provided with back-blowing device
Filter is connected.
Organic oxygen-containing compound olefin hydrocarbon apparatus in the utility model includes reactor, the first whirlwind gas-solid separator,
Second whirlwind gas-solid separator, chilling tower and filter；Product gas outlet is wherein provided with reactor；First whirlwind gas-
The first import, the first gaseous phase outlet and the first solid-phase outlet are provided with solid separator, the first import is connected with product gas outlet；
The second import, the second gaseous phase outlet and second solid phase outlet, the second import and first are provided with second whirlwind gas-solid separator
Solid-phase outlet is connected；Chilling tower is connected with the first gaseous phase outlet, the second gaseous phase outlet；Filter is arranged in series in the second gas phase
Between outlet and chilling tower.
, can be by product gas using the first whirlwind gas-solid separator and the second whirlwind gas-solid separator in said apparatus
Most of solid catalyst of entrainment is separated, and filter is set up between the second gaseous phase outlet and chilling tower, Neng Goujin
One step removes the catalyst micro mist and other little particle impurity of the small particle in product gas.This makes it possible to product gas is carried out more
Fully gas solid separation, prevent these micro mists from entering chilling tower and causing equipment to block.
Brief description of the drawings
The Figure of description for forming the part of the application is used for providing further understanding to of the present utility model, this practicality
New schematic description and description is used to explain the utility model, does not form to improper restriction of the present utility model.
In the accompanying drawings：
Fig. 1 shows the organic oxygen-containing compound olefin hydrocarbon apparatus schematic diagram according to a kind of embodiment of the utility model.
Wherein, above-mentioned accompanying drawing marks including the following drawings：
10th, reactor；20th, the first whirlwind gas-solid separator；30th, the second whirlwind gas-solid separator；40th, chilling tower；50、
Filter；60th, water scrubber；70th, heat exchanger；80th, regenerator.
Embodiment
It should be noted that in the case where not conflicting, the feature in embodiment and embodiment in the application can phase
Mutually combination.Describe the utility model in detail below with reference to the accompanying drawings and in conjunction with the embodiments.
As described by background section, organic oxygen-containing compound alkene exists solid in product gas in the prior art
Body particle removes halfway problem.In order to solve this problem, the utility model provides a kind of organic oxygen-containing compound system
Olefin hydrocarbon apparatus, as shown in figure 1, the device includes reactor 10, the first whirlwind gas-solid separator 20, the second whirlwind gas-particle separation
Device 30, chilling tower 40 and filter 50, are wherein provided with product gas outlet on reactor 10；First whirlwind gas-solid separator
The first import, the first gaseous phase outlet and the first solid-phase outlet are provided with 20, the first import is connected with product gas outlet；Second rotation
The second import, the second gaseous phase outlet and second solid phase outlet, the second import and the first solid phase are provided with wind gas-solid separator 30
Outlet is connected；Chilling tower 40 is connected with the first gaseous phase outlet, the second gaseous phase outlet；Filter 50 is arranged in series in the second gas phase
Between outlet and chilling tower 40.
In said apparatus provided by the utility model, the first whirlwind gas-solid separator 20 and gas-solid point of the second whirlwind are utilized
The most of solid catalyst carried secretly in product gas can be separated from device 30, and in the second gaseous phase outlet and chilling tower 40
Between set up filter 50, can further remove the catalyst micro mist and other little particle impurity of the small particle in product gas.
This makes it possible to carry out more fully gas solid separation to product gas, prevent these micro mists from entering chilling tower 40 and causing equipment to block up
Plug.
Specifically, the product gas of the production of reactor 10 processing enters the first whirlwind gas-solid separator 20, and the first whirlwind gas-
The lower of solid separator 20 discouraged enters the second whirlwind gas-solid separator 30, through this technique, most of solid for being carried secretly in product gas
Catalyst is separated.The gas that second whirlwind gas-solid separator 30 is separated is traveled further into filter 50, by residue
Micro mist filtering, prevent its block follow-up equipment.
In a kind of preferred embodiment, filter 50 is at least one, and when filter 50 is multiple, multiple filterings
Device 50 is arranged in parallel between the second gaseous phase outlet and chilling tower 40.So under the larger operating mode for the treatment of capacity, production can be improved
The treating capacity of product gas.It is also possible to by one or more of alternations, alleviate processing pressure and extend filter 50
Life-span.
The less micro mist of particle diameter in the removal product gas of the setting purpose of filter 50, any of dust removal field can be used
Filter type.In a kind of preferred embodiment, multiple filters 50 include purpose ceramic-film filter, metal powder sintered filter element
It is at least one in filter and electric precipitation filter.The better dust removal effect of this several filter, cost are relatively low.
Ceramic filter, its main body are mainly made up of filter supporting body, filter body and filter connector.Its
In, filter body uses aperture, and for 10 microns, the ceramic membrane of streamlined hollow barrel shape, wall thickness can be 4~5mm, filtering
Supporter is provided with below device body, top is provided with connector.Product gas is from the side surface of barrel-shaped filter body or weekly form
Enter the inner space of filter body on face, and the filter is left at the top of the inner space of filter body, wherein
Catalyst solid fine grained of most particle diameters more than 1 micron and/or fine powder are intercepted at outside filter.
Metal powder sintered cartridge filter, its be using stainless steel powder or metallic titanium powder as raw material, by powder classification, into
A kind of high-efficiency multiple filtering material made of the technical process such as type, sintering, mechanical welding processing.Its internal void bending configuration,
Crisscross, even aperture distribution, hole and filtering accuracy can be adjusted in comparatively wide scope, and filtration mechanism is typical case
In-depth filtration.
Preferably, the ceramic filter or the filtering accuracy of metal powder sintered cartridge filter that the utility model uses be
1~2 micron, preferably 1 micron.
As long as according to the above-mentioned set-up mode of the utility model, you can effectively remove the solid particle in product gas.One
In kind preferred embodiment, solid-phase catalyst outlet is additionally provided with reactor 10, reactor 10 is internally provided with reaction chamber；
Device also includes：3rd whirlwind gas-solid separator, the 3rd whirlwind gas-solid separator are provided with triple feed inlet, the 3rd gaseous phase outlet
With the 3rd solid-phase outlet；Triple feed inlet is connected with reaction chamber, and the 3rd solid-phase outlet is connected with solid-phase catalyst outlet；And the 4th
Whirlwind gas-solid separator, the 4th whirlwind gas-solid separator are provided with the 4th import, the 4th gaseous phase outlet and the 4th solid-phase outlet；
4th import is connected with the 3rd gaseous phase outlet, and the 4th gaseous phase outlet is connected with product gas outlet, and the 4th solid-phase outlet and solid phase
Catalyst outlet is connected.Two stage cyclone gas-solid separator is set in the internal series-connection of reactor 10, is advantageous to further improve admittedly
The removal effect of body particle.
The purpose for setting chilling tower 40 is to carry out chilling to the product gas of organic oxygen-containing compound alkene.A kind of preferred
Embodiment in, device includes multiple chilling towers 40 being set up in parallel.Multiple chilling towers 40 are arranged in parallel, and can increase processing
Amount.It is also possible to be used alternatingly, alleviate the operating pressure of individual equipment.
In a kind of preferred embodiment, the 5th gaseous phase outlet is additionally provided with chilling tower 40；Device also includes water scrubber
60, water scrubber 60 is connected with the 5th gaseous phase outlet.Water scrubber 60 is set up, the moisture in the gas phase that can be come out to chilling tower 40 enters
Row separation.Preferably, device includes multiple water scrubbers 60 being arranged in parallel.Similarly, multiple water scrubbers 60 are arranged in parallel, Neng Goujia
High throughput.It is also possible to be used alternatingly, alleviate the operating pressure of individual equipment.
In a kind of preferred embodiment, device also includes heat exchanger 70, and heat exchanger 70 is arranged in series in the first gas phase and gone out
Between mouth and chilling tower 40.Product gas that can be higher to temperature using heat exchanger 70 carries out precooling, to alleviate follow-up chilling tower
40 chilling pressure.
In a kind of preferred embodiment, regenerated catalyst import is also set up on reactor 10；Device also includes regenerator
80, regenerator 80 is connected with solid-phase catalyst outlet and regenerated catalyst import respectively.Set regenerator 80 can be to by anti-
The catalyst answered carries out regeneration treatment, is reused with reaching, resource reclaim, reduces the purpose of production cost.
In a kind of preferred embodiment, device also includes back-blowing device, blowback air outlet is provided with back-blowing device, instead
Flushing air outlet is connected with filter 50.Filter 50 will can be filtered down wherein after long-play using back-blowing device
Micro mist blowout equipment, remove enrichment or be deposited on filter 50 filter duct in catalyst solid fine grained and/or fine powder,
So as to play pulse cleaning filter layer and collect the purpose of micro mist.
In the application process of reality, by filter and/or the catalyst solid fine grained of whirlwind gas-solid separator separation
And/or fine powder, it is mixed in proportion with catalyst activity component-molecular sieve, binding agent, carrier, re-starts mashing, spraying
After drying and moulding, calcination activation, mixed in proportion with fresh catalyst or poising agent, the mixture formed enters in reactor
Used as fresh catalyst or poising agent.
Illustrated below by way of the device of methanol-to-olefins generation MTO product gas：
After methanol reacts into methanol to olefins reaction device, the MTO product gas of generation passes through some groups of series connection before this
Firsts and seconds whirlwind gas-solid separator (be arranged on inside reactor threeth and above-mentioned equivalent to the utility model
Four whirlwind gas-solid separators) separated.Most catalyst granules that MTO product gas carries separate with MTO product gas
Afterwards, MTO product gas subsequently departs from MTO reactors into three-level whirlwind gas-solid separator (above-mentioned equivalent to the utility model the
One whirlwind gas-solid separator).Solid particle (catalyst) concentration of MTO product gas in three-level whirlwind gas-solid separator porch
For 800~1200mg/m3, the concentration in three-level whirlwind gas-solid separator exit is 150~300mg/m3.Therefore, three-level is revolved
Wind gas-solid separator can separate most catalyst fines and/or fine powder, and MTO device reaction three-level whirlwind gas-
The concentration and size distribution of the gateway catalyst granules of solid separator are as shown in table 1.
Table 1
Known by table 1 and 83.8% (volume ratio) catalyst fines and/or fine powder are there are about in MTO product gas by three-level whirlwind
Gas-solid separator is separated.The product gas containing higher concentration catalyst that this part is separated enters reaction gas
Category Four cyclone gas-solid separator (the second whirlwind gas-solid separator above-mentioned equivalent to the utility model) is separated again afterwards.
For scale is 1,800,000 tons/year of methanol-to-olefins devices, enter per hour from reaction gas tetra-cyclone
The catalyst fines amount for entering chilling tower is as shown in table 2.
Table 2
In general, the total efficiency of separation of reaction gas Category Four cyclone gas-solid separator works as reaction gas between 70~75%
When the total efficiency of separation of Category Four cyclone gas-solid separator is 72%, as shown in Table 2, Category Four cyclone gas-solid separator enters to urgency
The catalyst fines amount of cold tower is up to 28.03kg/h, and this partial catalyst will be enriched with chilling tower, water scrubber, and with
Chilled water (chw), washing water are recycled into the tower bottom reboiler of separation of olefins tower, chilled water (chw) air heat exchanger, the tower of propylene rectification tower
Among bottom reboiler, washing water dry-type air cooler, the washing equipment such as water cooler, with the extension of plant running time,
Above-mentioned catalyst fines and/or fine powder in MTO product gas will be progressively enriched with said apparatus, and chilling can be caused when serious
Tower, the tower tray of water scrubber block；Catalyst fines and/or fine powder accumulation are changed in washing water air cooled heat exchanger, water cooling
The tower bottom reboiler etc. of hot device, separation of olefins tower, so as to cause system heat exchange efficiency to reduce, it is necessary to periodically enter to the said equipment
Row cleaning and safeguard, this reduces production efficiency, add labor intensity.
And the utility model is set between the outlet of MTO reaction gas Category Four cyclone gas-solid separators and the entrance of chilling tower
At least one filter is put, it is thin to remove the catalyst carried in MTO reaction gas Category Four cyclone gas-solid separator exported product gas
Particle and/or fine powder, these catalyst fines and/or fine powder are retained down by filter, and MTO reaction gas Category Four cyclones gas-
The quantity of catalyst fines and/or fine powder in solid separator exported product gas will greatly reduce, and this can be largely
The upper quantity for reducing the catalyst fines and/or fine powder that enter product gas separating technology middle and lower reaches workshop section with MTO product gas, from
And prevent chilling tower, water scrubber, chilled water (chw) cyclone hydraulic separators and the reduction of various heat exchanger operating efficiencies and anti-locking system behaviour
Make abnormal.
For 1,800,000 tons/year of MTO technologies, to ensure the separation of reaction three-level whirlwind gas-solid separator
Efficiency, the product gas throughput that Category Four cyclone gas-solid separator is entered by three-level whirlwind gas-solid separator dipleg is typically controlled
System marks or so vertical/hour 6000.Accordingly, the Al of use2O3For example following table of structural parameters and operating condition of purpose ceramic-film filter
Shown in 3.
Table 3
As seen from Table 3：In the utility model, the filter efficiency of filter is up to 80%, and it efficiently separates and retained
From the outlet of Category Four cyclone gas-solid separator into the catalyst fines and/or fine powder of chilling tower, MTO productions are significantly reduced
The segregational load of product qi leel separating process middle and lower reaches workshop section, it is different to avoid the equipment operation of MTO product gas separating technology middle and lower reaches workshop section
The problem of normal.
Preferred embodiment of the present utility model is the foregoing is only, is not limited to the utility model, for this
For the technical staff in field, the utility model can have various modifications and variations.It is all in the spirit and principles of the utility model
Within, any modification, equivalent substitution and improvements made etc., it should be included within the scope of protection of the utility model.
Claims (10)
- A kind of 1. organic oxygen-containing compound olefin hydrocarbon apparatus, it is characterised in that including：Reactor (10), product gas outlet is provided with the reactor (10)；First whirlwind gas-solid separator (20), the first import, first are provided with the first whirlwind gas-solid separator (20) Gaseous phase outlet and the first solid-phase outlet；First import is connected with the product gas outlet；Second whirlwind gas-solid separator (30), the second import, second are provided with the second whirlwind gas-solid separator (30) Gaseous phase outlet and second solid phase outlet；Second import is connected with first solid-phase outlet；Chilling tower (40), the chilling tower (40) are connected with first gaseous phase outlet, second gaseous phase outlet；AndFilter (50), the filter (50) are arranged in series between second gaseous phase outlet and the chilling tower (40).
- 2. device according to claim 1, it is characterised in that the filter (50) is at least one, and works as the mistake When filter (50) is multiple, multiple filters (50) are arranged in parallel in second gaseous phase outlet and the chilling tower (40) Between.
- 3. device according to claim 2, it is characterised in that multiple filters (50) include purpose ceramic-film filter, It is at least one in metal powder sintered cartridge filter and electric precipitation filter.
- 4. device according to any one of claim 1 to 3, it is characterised in that be additionally provided with the reactor (10) Solid-phase catalyst exports, and the reactor (10) is internally provided with reaction chamber；Described device also includes：3rd whirlwind gas-solid separator, the 3rd whirlwind gas-solid separator be provided with triple feed inlet, the 3rd gaseous phase outlet and 3rd solid-phase outlet；The triple feed inlet is connected with the reaction chamber, and the 3rd solid-phase outlet goes out with the solid-phase catalyst Mouth is connected；And4th whirlwind gas-solid separator, the 4th whirlwind gas-solid separator be provided with the 4th import, the 4th gaseous phase outlet and 4th solid-phase outlet；4th import is connected with the 3rd gaseous phase outlet, the 4th gaseous phase outlet and the product gas Outlet is connected, and the 4th solid-phase outlet is connected with solid-phase catalyst outlet.
- 5. device according to any one of claim 1 to 3, it is characterised in that described device includes multiple be arranged in parallel The chilling tower (40).
- 6. device according to claim 5, it is characterised in that be additionally provided with the 5th gas phase on the chilling tower (40) and go out Mouthful；Described device also includes water scrubber (60), and the water scrubber (60) is connected with the 5th gaseous phase outlet.
- 7. device according to claim 6, it is characterised in that described device includes multiple water scrubbers being arranged in parallel (60)。
- 8. device according to claim 5, it is characterised in that described device also includes heat exchanger (70), the heat exchanger (70) it is arranged in series between first gaseous phase outlet and the chilling tower (40).
- 9. device according to claim 4, it is characterised in that be additionally provided with regenerated catalyst on the reactor (10) and enter Mouthful；Described device also includes regenerator (80), and the regenerator (80) is exported respectively with the solid-phase catalyst and the regeneration Catalyst inlet connects.
- 10. device according to any one of claim 1 to 3, it is characterised in that described device also includes back-blowing device, Blowback air outlet is provided with the back-blowing device, the blowback air outlet is connected with the filter (50).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720254117.1U CN206624799U (en) | 2017-03-15 | 2017-03-15 | Organic oxygen-containing compound olefin hydrocarbon apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720254117.1U CN206624799U (en) | 2017-03-15 | 2017-03-15 | Organic oxygen-containing compound olefin hydrocarbon apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206624799U true CN206624799U (en) | 2017-11-10 |
Family
ID=60209483
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720254117.1U Active CN206624799U (en) | 2017-03-15 | 2017-03-15 | Organic oxygen-containing compound olefin hydrocarbon apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206624799U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109134182A (en) * | 2018-08-21 | 2019-01-04 | 陕西延长中煤榆林能源化工有限公司 | A kind of methanol to olefins reaction product gas and catalyst separation system and separating technology |
| CN109134182B (en) * | 2018-08-21 | 2024-05-17 | 陕西延长中煤榆林能源化工股份有限公司 | Separation system and separation process for product gas and catalyst in reaction of preparing olefin from methanol |
-
2017
- 2017-03-15 CN CN201720254117.1U patent/CN206624799U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109134182A (en) * | 2018-08-21 | 2019-01-04 | 陕西延长中煤榆林能源化工有限公司 | A kind of methanol to olefins reaction product gas and catalyst separation system and separating technology |
| CN109134182B (en) * | 2018-08-21 | 2024-05-17 | 陕西延长中煤榆林能源化工股份有限公司 | Separation system and separation process for product gas and catalyst in reaction of preparing olefin from methanol |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP2636439B1 (en) | Method for cleaning and separating mto reaction gas containing catalyst micropowders | |
| CN1263829C (en) | Stripping process and apparatus | |
| CN101766935B (en) | Combined type gas-liquid-solid three phase separation method and device | |
| CN103214333A (en) | System and process for gas-solid separation and heat exchange of alkene product prepared from organic oxygen-containing compound | |
| CN103524286B (en) | Methanol and C4-to-olefin quenched water and washing water airtight coupling treatment method and device | |
| CN108753356A (en) | A kind of multi-stage countercurrent catalytic cracking/cracking system and method | |
| CN104479761A (en) | Washing tower and coal gas purification and dust removal system with washing tower | |
| CN106732823A (en) | A kind of regenerating catalyst in fluidized bed method | |
| EA006143B1 (en) | Separation process and apparatus for removal of particulate material from delayed coking gas oil unit | |
| CN206624799U (en) | Organic oxygen-containing compound olefin hydrocarbon apparatus | |
| US20040184970A1 (en) | Stripper and a stripping process for removing the flue gas carried by regenerated catalyst | |
| JP2002537117A (en) | Gas-solid separation method | |
| US11857897B2 (en) | Gas cooling-scrubbing apparatus and method | |
| CN101708822A (en) | Method and device for removing liquid and solid of continuous reformed hydrogen | |
| CN209885776U (en) | Gas-solid separation device for organosilicon monomer synthesis fluidized bed reactor | |
| CN103111241A (en) | Low-temperature slurry reactor Fischer-Tropsch synthesis system and separation technology thereof | |
| CN114181730B (en) | Method for purifying water slurry of quenching tower of fluidized bed methanol conversion device and recovering catalyst fine powder | |
| CN1035773C (en) | Disengager stripper containing dissipation plates for use in an FCC process | |
| EP2445629B1 (en) | Apparatus and process for three-phase reaction | |
| CN104711006B (en) | A kind of F- T synthesis system and method | |
| CN204564102U (en) | A kind of F-T synthesis system | |
| CN109628131A (en) | A kind of solid-liquid separating method containing solid oil product | |
| CN208717192U (en) | Methanol to olefins reaction product gas and catalyst separation system | |
| CN202921106U (en) | Gas filter device for polycrystalline silicon production process | |
| CN1128854C (en) | Fluid catalytic cracking to hydrocarbon by comprehensive equipment of separating and stripping catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |