CN206229322U - A kind of processing system of catalyst for producing propylene with methanol - Google Patents
A kind of processing system of catalyst for producing propylene with methanol Download PDFInfo
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- CN206229322U CN206229322U CN201621321504.4U CN201621321504U CN206229322U CN 206229322 U CN206229322 U CN 206229322U CN 201621321504 U CN201621321504 U CN 201621321504U CN 206229322 U CN206229322 U CN 206229322U
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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
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Abstract
A kind of processing system of catalyst for producing propylene with methanol, including：Process steam generation device, for providing the process steam produced by desalted water；First heating furnace, is provided with the first feeding line and the 3rd feeding line at charging aperture；Second heating furnace, charging aperture is provided with the second feeding line；MTP reactors, multiple beds are provided with it along longitudinal direction；Its top feed pipeline；Side entry feed pipeline；First gas distributor is provided with MTP reactors, first gas distributor is arranged between its top feed of MTP reactors mouthful and first beds.The processing system of catalyst for producing propylene with methanol of the present utility model, each beds are passed through by material from the top of MTP reactors and side line respectively, improve treatment effect；When carrying out steam treatment, it is to avoid using the process water of quenching column bottom of towe, and then avoid the influence of the methyl alcohol being mingled with the process water and dimethyl ether to steam treatment effect；When carrying out regeneration treatment, favorable regeneration effect.
Description
Technical field
The utility model belongs to coal chemical technology, and in particular to a kind of processing system of catalyst for producing propylene with methanol.
Background technology
Catalyst as MTP technologies core, the quality of its performance is directly connected to the yield situation of target product, therefore
Receive much concern.To improve catalyst performance, steam treatment of passing through need to be being entered to it before, on the one hand can dredge catalyst
Duct；On the other hand catalyst surface can be adjusted acid, and then extends catalyst service life, optimized product distribution, made anti-
Should be carried out to the direction for being more beneficial for generating propylene.
Preparing propylene from methanol (MTP) technique refers to coal base or the methyl alcohol of natural gas base synthesis as raw material, in the work of catalyst
Under, the chemical process technology of propylene is obtained through the production of MTP reactors.In art production process, MTP reactor outlets product heat
It is washed with chilled water in the quenching column for entering chilling train after changing, product temperatur is on the one hand further reduced, makes gas
Liquid initial gross separation；On the other hand the pH value for adding alkali lye to adjust logistics is then needed, makes it be in neutral.From quenching column bottom of towe out
Most of process water input methanol distillation column reclaims methyl alcohol therein and dimethyl ether, and remaining small part process water then enters technique
Turret is distilled out of, it is possible to the beds of MTP reactors are directly returned to, during the course of the reaction as diluent and heat absorption
Steam reduction reaction bed temperature, it is also possible to heated stove further heating after, to coming into operation before catalyst carry out vapor
Treatment.That is, the technique of process steam when carrying out to catalyst steam treatment in original technique from quenching column bottom of towe
Water, i.e. reactor outlet product can contain a small amount of methyl alcohol and diformazan through the process water after quenching column washing, this some processes water
Ether, so as to also inevitably be mingled with methyl alcohol and dimethyl ether in the process steam that is distilled out of from process steam tower, and methyl alcohol and
Used as reaction mass, (480 DEG C) can be reacted dimethyl ether with catalyst under the conditions of steam treatment, cause catalyst surface
Part carbon distribution, it is impossible to reach expected steam treatment effect；In addition, during steam treatment, vapor is from reactor head
Into, each beds are gradually penetrated, cause the steam treatment effect of each beds different, show as from upper
Gradually weaken under.
With the carrying out of MTP techniques, carbon distribution gradually increases on catalyst, and the active sites on catalyst are eventually completely covered
Point, the duct of blocking catalyst inactivates catalyst.Now need to regenerate catalyst, specifically use regeneration gas/nitrogen
Carbon distribution on gas mixed combustion burning-off catalyst.In regenerative process, regeneration gas/nitrogen mixture enters from MTP reactor heads,
Gradually penetrate each beds to be regenerated, when all air of regeneration gas for adding, all of bed inlet temperatures are 480
DEG C, and export there is no showing that regenerative process has been completed during temperature rise.The renovation process has that efficiency is low, the recovery time is long (about
150 hours), and each beds regeneration effect is difficult to that unified (catalyst of regeneration ending rear lower beds is carbon containing
Amount is higher than top) the problems such as.
Utility model content
The purpose of this utility model is to provide a kind of processing system of catalyst for producing propylene with methanol, for improving catalyst
Regeneration effect.
The technical solution of the utility model is as follows：
A kind of processing system of catalyst for producing propylene with methanol, including：
Process steam generation device, for providing the process steam produced by desalted water；
First heating furnace, is provided with the first feeding line and the 3rd feeding line at the charging aperture of first heating furnace,
First feeding line is used to be input into nitrogen in first heating furnace to be heated；3rd feeding line is used for will
Process steam from the process steam generation device is input into first heating furnace and is heated；
Second heating furnace, the charging aperture of second heating furnace is provided with the second feeding line, for regeneration gas to be input into
Heated in second heating furnace；
In MTP reactors, the MTP reactors multiple beds are provided with along longitudinal direction；
Its top feed pipeline, for the material by part from first heating furnace and part from the described second heating
The material of stove is delivered on first beds of the MTP reactors from top；
Side entry feed pipeline, for the material by part from first heating furnace and part from the described second heating
The material of stove is delivered on the beds of the second to the most end of the MTP reactors；
First gas distributor is provided with the MTP reactors, it is anti-that the first gas distributor is arranged at the MTP
Answer between its top feed mouthful of device and first beds, for the material being input into through its top feed pipeline to be uniformly distributed
To first beds.
Preferably, multiple second gas distributors, the second gas distributor difference are provided with the MTP reactors
Be arranged between each adjacent catalyst bed, for by the material being input into through side entry feed pipeline be respectively uniformly distributed to second to
Most end beds.
Preferably, in each described beds, upper temperature sensor, middle portion temperature are disposed with from top to bottom
Sensor and lower temperature sensor, the temperature of top, middle part and bottom for measuring each beds respectively.
Preferably, each described beds is in the plane where the upper temperature sensor, with plane
The heart is radially provided with multiple face temperature sensors along radial direction for the center of circle, for measuring each catalyst respectively
The temperature of diverse location in bed plane.
Preferably, the upper temperature sensor, middle portion temperature sensor, lower temperature sensor and plane TEMP
Sleeve pipe is arranged with device.
Preferably, the bottom of the MTP reactors is provided with bottom outlet, is provided with the bottom outlet
On-line detector, the content for detecting oxygen in discharging gas.
Preferably, the first valve and first flow are disposed with along Flow of Goods and Materials direction on the 3rd feeding line
Meter, is controlled for the conveying to vapor and conveying capacity.
Preferably, set gradually respectively along Flow of Goods and Materials direction on its top feed pipeline and the side entry feed pipeline
Have the second valve and second flowmeter, for respectively to the conveying of material that is input into from the MTP reactor heads and side line and
Conveying capacity is controlled.
Preferably, the 3rd valve and the 3rd flow are disposed with along Flow of Goods and Materials direction on second feeding line
Meter, for being controlled to nitrogen conveying and conveying capacity.
Preferably, the 4th valve and the 4th stream are disposed with respectively along Flow of Goods and Materials direction on the 3rd feeding line
Gauge, is controlled for the conveying to regeneration gas and conveying capacity.
The beneficial effects of the utility model are：
The processing system of catalyst for producing propylene with methanol of the present utility model, by material respectively from the top of MTP reactors and
Side line is passed through each beds, and the material intake of top and side line is controlled by corresponding valve and flowmeter, can
Make its top feed of MTP reactors consistent with side entry feed as much as possible, and make various loci on each beds as far as possible
Material it is uniform, improve treatment effect so that catalyst can keep more preferable state, be conducive to improving propylene in production process
Yield；When regeneration treatment and steam treatment is carried out to catalyst, each bed treatment effect is consistent；Water-filling is being entered to catalyst
During steam treated, it is to avoid using the process water of quenching column bottom of towe, and then avoid the methyl alcohol and diformazan being mingled with the process water
Influence of the ether to steam treatment effect.
Brief description of the drawings
Fig. 1 is the processing system structural representation in one embodiment of catalyst for producing propylene with methanol of the present utility model
Figure；
Fig. 2 is the longitudinal profile enlarged drawing of beds；
The horizontal section enlarged drawing of beds during Fig. 3.
Specific embodiment
The technical solution of the utility model and its effect are described further below by way of specific embodiment.Following reality
The mode of applying is merely to illustrate content of the present utility model, is not limited to protection domain of the present utility model.Using this practicality
The simple change that new design is carried out to the utility model is all in the scope that the utility model is claimed.
As Figure 1-3, the processing system of catalyst for producing propylene with methanol of the present utility model, including：
Process steam generation device 1, for providing the process steam produced by desalted water；
First heating furnace 31, is provided with the first feeding line 41 and the 3rd charging at the charging aperture of first heating furnace 31
Pipeline, first feeding line is used to be input into nitrogen in first heating furnace 31 to be heated；3rd feed pipe
Line is heated for that will be input into first heating furnace 31 from the process steam of the process steam generation device 1；
Second heating furnace 32, the charging aperture of second heating furnace 32 is provided with the second feeding line 42, for that will regenerate
Gas is input into second heating furnace 32 and is heated；
In MTP reactors 8, the MTP reactors multiple beds 9 are provided with along longitudinal direction；
Its top feed pipeline 7, described second is come from for the material by part from first heating furnace 31 and part
The material of heating furnace 32 is delivered on first beds 9 of the MTP reactors 8 from top；
Side entry feed pipeline 10, described second is come from for the material by part from first heating furnace 31 and part
The material of heating furnace 31 is delivered on the beds 9 of the second to the most end of the MTP reactors 8；
First gas distributor is provided with the MTP reactors 8, the first gas distributor is arranged at the MTP
Between its top feed mouthful of reactor 8 and first beds 9, the material for will be input into through its top feed pipeline 7 is equal
It is even to be distributed to first beds 99.
The processing system of catalyst for producing propylene with methanol of the present utility model, enters through top and side line respectively by by material
Material, ensures that the charging of each bed is identical, it is ensured that the treatment effect of each bed as much as possible；By setting for first gas distributor
Put, be more so that the charging of the first beds is uniform, the charging of each position is consistent with reaction, improves treatment effect.
The total amount that is passed through of regeneration gas is 30000-100000Nm3/ h, preferably 80000Nm3/h。
The process steam of the generation including low pressure steam pipe network, boiler or etc. synthesis drum of process steam generation device 1, produces
The water source of raw process steam is non-chilled water.Due to being mingled with methyl alcohol, dimethyl ether etc. in chilled water, steam treatment is being carried out
Catalyst surface carbon distribution can be caused as reaction raw materials and catalyst reaction when (480 DEG C).And low pressure steam pipe network, boiler
Or it is not chilled water that synthesis drum etc. produces the water source of process steam, it is to avoid above mentioned problem so that after steam treatment, a side
Surface catalysis agent duct is dredged, and another aspect catalyst surface is adjusted to acidity, and then is extended the service life of catalyst, improved and urge
The catalytic performance of agent, optimized product distribution, make reaction be carried out to the direction for being more beneficial for generating propylene, are conducive to improving propylene
Yield.Wherein, a special steam generator of " synthesis drum " this area, is natural circulation boiler and associated circulation boiler
Important component, in a device its Main Function be reclaim high-quality heat energy, waste heat boiler is constituted together with synthesis reactor,
So being also known as " synthesis drum ", thermal source is the heat release of methanol synthesis reactor catalyst, and water source is desalted water.Therefore from conjunction
Methyl alcohol is not contained into the process steam of drum.
In one embodiment, multiple second gas distributors, second gas are provided with the MTP reactors 8
Body distributor is respectively arranged between each adjacent catalyst bed 9, for the material difference that will be input into through side entry feed pipeline 10
It is evenly distributed to the second to most end beds 9.So that the charging everywhere of each beds of the second to most end is uniform, carry
High disposal effect.
In one embodiment, in each described beds 9, upper temp sensing is disposed with from top to bottom
Device, middle portion temperature sensor and lower temperature sensor, top, middle part for measuring each beds 9 respectively
And the temperature of bottom.By the top to each beds 9, middle part, temperature of lower measurement, judge corresponding catalyst bed
Whether the regeneration treatment in layer 9 to catalyst is complete.Because regenerative process is exothermic reaction, and regeneration gas is to move from the top down
, when regeneration treatment is not completed, the top of beds 9, middle part, the response situation difference of bottom, temperature are also different.When
When the top of beds 9, middle part, temperature of lower all same, illustrate that the regeneration situation of its upper, middle and lower is consistent, regeneration is complete.
In one embodiment, each described beds 9 is in the plane where the upper temperature sensor,
Multiple face temperature sensors are radially provided with as the center of circle along radial direction with the center of plane, for measuring each respectively
The temperature of diverse location in the plane of the beds 9.By various location temperature in the plane to corresponding catalyst bed 9
The measurement of degree, judges the uniformity that regeneration gas is distributed thereon, the regeneration situation of each several part on Judge plane.If each several part temperature
Unanimously, then explanation regeneration gas is evenly distributed, and the regeneration situation of each several part is consistent in plane.
In one embodiment, the upper temperature sensor, middle portion temperature sensor, lower temperature sensor peace
Sleeve pipe is arranged with the temperature sensor of face.Sleeve pipe facilitates the installation and taking-up of said temperature sensor, and convenient being used is drawn
Line is drawn, and it is connected with temperature indicating device, and measured temperature is shown to facilitate observation.
In one embodiment, the bottom of the MTP reactors 8 is provided with bottom outlet 15, and the bottom goes out
On-line detector 16 is provided with expects pipe line 15, the content for detecting oxygen in discharging gas.By with on-line detector 16
The regeneration feelings of catalyst in the content of oxygen in the bottom discharge of detection MTP reactors 8, detection MTP reactors 8 this entirety
Condition, when the content constant of oxygen is detected, the regeneration in MTP reactors to catalyst is completed, now oxygen in bottom discharge
Content in 10wt% or so.
In one embodiment, it is disposed with the first valve along Flow of Goods and Materials direction on the 3rd feeding line 43
6 and first flowmeter 5, it is controlled for the conveying to vapor and conveying capacity.It is preferably right by the control to vapor
Catalyst carries out steam treatment, improves the catalytic performance of catalyst.First valve 6 can be valve commonly used in the art, than
Such as hand valve；First flowmeter 5 can be flowmeter commonly used in the art.
In one embodiment, along Flow of Goods and Materials side on its top feed pipeline 7 and the side entry feed pipeline 10
To the second valve and second flowmeter is disposed with respectively, for respectively to being input into from the top of the MTP reactors 8 and side line
Material conveying and conveying capacity be controlled.
In one embodiment, it is disposed with the 3rd valve along Flow of Goods and Materials direction on second feeding line 41
With the 3rd flowmeter, for nitrogen conveying and conveying capacity be controlled.
In one embodiment, the 4th is disposed with respectively along Flow of Goods and Materials direction on the 3rd feeding line 42
Valve and the 4th flowmeter, are controlled for the conveying to regeneration gas and conveying capacity.
Second valve, the 3rd valve and the 4th valve can be valve commonly used in the art, such as hand valve；Second flow
Meter, the 3rd flowmeter and the 4th flowmeter can be flowmeter commonly used in the art.
When steam treatment is carried out, the process steam from first heating furnace 31 enter MTP reactors 8 it
Before, its temperature is 440-490 DEG C, such as 480 DEG C.
Its top feed amount of process steam is 1 with the mass ratio of each side entry feed amount summation:0.1-20, such as 1:9.
The processing system of catalyst for producing propylene with methanol of the present utility model as Figure 1-3 is when steam treatment is carried out
Running be：
Process steam from process steam generation device 1 is input into the first heating furnace 31 and is heated, then according to matter
Amount is than being 1:0.1-20 through purging 2-8h in its top feed pipeline 7 and the input MTP of side entry feed pipeline 10 reactors 8, is pushed up respectively
The process steam in portion is through first beds 9 in the input MTP of its top feed pipeline 7 reactors 8, the process steam warp of side line
The second to most end beds 9 in each input MTP of side entry feed pipeline 10 reactors 8, realize to the vapor of catalyst
Reason.
When that need not regenerate, the effect of steam treatment compares：
The utility model：When carrying out steam treatment using above-mentioned processing system of the present utility model, with one 500,000 tons/
As a example by the MTP reactors in year, loaded catalyst is 50 tons；Steam treatment condition is：Vapor inlet amount be 25 tons/it is small
When, treatment temperature is 480 DEG C, and process time is 48 hours.
Prior art：In other conditions just as in the case of, this practicality is replaced with the process steam in technique turret new
Process steam in the process steam generation device 1 of type, carries out steam treatment.
Catalyst after processing in above-mentioned two situations is used for the production process of preparing propylene from methanol, the MTP reactions for obtaining
The product distribution of device is shown in Table 1.
Table 1 carry out steam treatment with different vapor after MTP reactors product distribution
As shown in Table 1, steam treatment effect of the present utility model is more preferable, the catalytic performance of the catalyst obtained after treatment
More preferably, the production process of preparing propylene from methanol is used it for, in the product of the MTP reactors for obtaining, propylene content improves a lot.
Estimated 1 year can be with 3000 tons of propylene enhancing, according to 0.8 ten thousand yuan/ton of calculating, annual new output value is 24,000,000 yuan or so.
The processing system of catalyst for producing propylene with methanol of the present utility model carry out regeneration treatment when running be：
First, the process steam from process steam generation device 1 is input into the first heating furnace 31 and is heated, Ran Houfen
In not through its top feed pipeline 7 and the input MTP of side entry feed pipeline 10 reactors 8, the process steam of input is first through first gas
Distributor 81 and second gas distributor 82 carry out gas distribution, and each beds 9 are then blowed to again, after purging 2-8h, close
Close the first valve 6；The 3rd valve and the 3rd flowmeter of the second feeding line 41 are opened, is entered to the input nitrogen of the first heating furnace 31
Row heating, the nitrogen after heating is input into MTP reactors 8 through its top feed pipeline 7 and side entry feed pipeline 10 respectively, input
Nitrogen first carries out gas distribution through first gas distributor 81 and second gas distributor 82, and each beds are then blowed to again
9,2-8h is purged, then keep above-mentioned nitrogen to be passed through under state, open the 4th valve and the 4th on the second feeding line 42
Flowmeter, is heated to the input of the second heating furnace 32 regeneration gas, and the regeneration gas after heating is respectively through its top feed pipeline 7 and side
Mix with nitrogen in the input MTP of line feeding line 10 reactors 8, and through first gas distributor 81 and second gas distributor 82
Gas distribution is carried out, each beds 9 are then blowed to again, the carbon distribution on catalyst is burnt, realize catalyst again
It is raw.With the carrying out of regenerative process, regeneration gas replaces part nitrogen so that the gaseous mixture of nitrogen and regeneration gas (containing oxygen)
In, oxygen content progressively increases to 5-20wt%, preferably 10wt%.When the inlet temperature stabilization of each beds 9, and export
There is no during temperature rise, regenerative process is completed.Wherein, the total amount of regeneration gas is 30000-100000Nm3/ h, preferably 80000Nm3/h.
The effect for regenerating treatment compares：
The utility model：When carrying out regeneration treatment using above-mentioned processing system of the present utility model, with one 500,000 tons/year
MTP reactors as a example by, loaded catalyst be 50 tons；Process steam, nitrogen and regeneration gas are respectively through its top feed pipeline 7
It is input into each beds 9 simultaneously with side entry feed pipeline 10；Process steam purge 4h, nitrogen purging 4h, regeneration gas it is total
It is 80000Nm to measure3/ h, the amount from top input is 8000Nm3/ h, from side line input is always 72000Nm3/h；Regeneration gas is sky
Gas, oxygen content is eventually increased to 10wt% in gaseous mixture, and bed temperature is maintained at 480 DEG C in regenerative process, and the recovery time is
72 hours.
Comparative example 1:In the case of other conditions identical, process steam, nitrogen and regeneration gas in each step are passed through
Only it is input into MTP reactors through its top feed pipeline 7, each beds 9 is gradually regenerated, the total amount of regeneration gas is
80000Nm3/ h, the recovery time is 72 hours.
Comparative example 2:In other conditions just as in the case of, process steam, nitrogen and regeneration gas in each step are passed through
Only it is input into MTP reactors through its top feed pipeline 7, each beds 9 is gradually regenerated, the total amount of regeneration gas is
80000Nm3/ h, the recovery time is 150 hours.
Each layer catalyst after being processed in the case of above-mentioned three kinds is sampled analysis, the carbon distribution content such as table 2 of catalyst.
The carbon distribution content of each layer catalyst after the regeneration treatment of the various process of table 2
As shown in Table 2, more preferably, the recovery time is short, and each catalyst bed after regeneration for regeneration treatment effect of the present utility model
Carbon deposition quantity is more uniform on the catalyst of layer, and carbon deposition quantity is few.
Claims (10)
1. a kind of processing system of catalyst for producing propylene with methanol, it is characterised in that including：
Process steam generation device (1), for providing the process steam produced by desalted water；
First heating furnace (31), is provided with the first feeding line (41) and the 3rd and enters at the charging aperture of first heating furnace (31)
Expects pipe line (43), first feeding line is used to be input into nitrogen in first heating furnace (31) to be heated；Described
Three feeding lines (43) by the process steam from the process steam generation device (1) for being input into first heating furnace
(31) heated in；
Second heating furnace (32), the charging aperture of second heating furnace (32) is provided with the second feeding line (42), for will again
Heated in anger input second heating furnace (32)；
In MTP reactors (8), the MTP reactors multiple beds (9) are provided with along longitudinal direction；
Its top feed pipeline (7), described second is come from for the material by part from first heating furnace (31) and part
The material of heating furnace (32) is delivered on first beds (9) of the MTP reactors (8) from top；
Side entry feed pipeline (10), described second is come from for the material by part from first heating furnace (31) and part
The material of heating furnace (31) is delivered on the beds (9) of the second to the most end of the MTP reactors (8)；
First gas distributor is provided with the MTP reactors (8), it is anti-that the first gas distributor is arranged at the MTP
Answer between its top feed mouthful of device (8) and first beds (9), for the thing that will be input into through its top feed pipeline (7)
Material is evenly distributed to first beds (9).
2. processing system according to claim 1, it is characterised in that multiple second is provided with the MTP reactors (8)
Gas distributor, the second gas distributor is respectively arranged between each adjacent catalyst bed (9), for that will enter through side line
The material of expects pipe line (10) input is respectively uniformly distributed to the second to most end beds (9).
3. processing system according to claim 1 and 2, it is characterised in that in each described beds (9), by upper
Upper temperature sensor, middle portion temperature sensor and lower temperature sensor are disposed with downwards, for measuring each respectively
The temperature on the top, middle part and bottom of the beds (9).
4. processing system according to claim 3, it is characterised in that each described beds (9) is on the top
In plane where temperature sensor, multiple face temperatures are radially provided with along radial direction by the center of circle of the center of plane
Sensor, the temperature for measuring diverse location in each described beds (9) plane respectively.
5. processing system according to claim 4, it is characterised in that the upper temperature sensor, middle portion temperature sensing
Sleeve pipe is arranged with device, lower temperature sensor and plane temperature sensor.
6. the processing system according to any one of claim 1,2,4 or 5, it is characterised in that the MTP reactors (8)
Bottom be provided with bottom outlet (15), be provided with on-line detector (16) on the bottom outlet (15), be used for
The content of oxygen in detection discharging gas.
7. processing system according to claim 6, it is characterised in that along Flow of Goods and Materials on the 3rd feeding line (43)
Direction is disposed with the first valve (6) and first flowmeter (5), is controlled for the conveying to vapor and conveying capacity.
8. processing system according to claim 7, it is characterised in that its top feed pipeline (7) and the side line enter
Expects pipe line is disposed with the second valve and second flowmeter respectively on (10) along Flow of Goods and Materials direction, for respectively to from described
The conveying of the material of MTP reactors (8) top and side line input and conveying capacity are controlled.
9. processing system according to claim 8, it is characterised in that along Flow of Goods and Materials on second feeding line (41)
Direction is disposed with the 3rd valve and the 3rd flowmeter, for being controlled to nitrogen conveying and conveying capacity.
10. the processing system according to any one of claim 1,2,4,5 or 7-9, it is characterised in that the 3rd charging
Pipeline is disposed with the 4th valve and the 4th flowmeter respectively on (42) along Flow of Goods and Materials direction, for the conveying to regeneration gas
It is controlled with conveying capacity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621321504.4U CN206229322U (en) | 2016-12-05 | 2016-12-05 | A kind of processing system of catalyst for producing propylene with methanol |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621321504.4U CN206229322U (en) | 2016-12-05 | 2016-12-05 | A kind of processing system of catalyst for producing propylene with methanol |
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| Publication Number | Publication Date |
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| CN206229322U true CN206229322U (en) | 2017-06-09 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110054539A (en) * | 2019-05-10 | 2019-07-26 | 国家能源投资集团有限责任公司 | A kind of preparing propylene from methanol device and method |
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2016
- 2016-12-05 CN CN201621321504.4U patent/CN206229322U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110054539A (en) * | 2019-05-10 | 2019-07-26 | 国家能源投资集团有限责任公司 | A kind of preparing propylene from methanol device and method |
| CN110054539B (en) * | 2019-05-10 | 2022-05-20 | 国家能源投资集团有限责任公司 | Device and method for preparing propylene from methanol |
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