CN110343028A - A kind of method and apparatus reducing MTO device catalyst loss amount - Google Patents
A kind of method and apparatus reducing MTO device catalyst loss amount Download PDFInfo
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- CN110343028A CN110343028A CN201810284110.3A CN201810284110A CN110343028A CN 110343028 A CN110343028 A CN 110343028A CN 201810284110 A CN201810284110 A CN 201810284110A CN 110343028 A CN110343028 A CN 110343028A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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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 invention belongs to methanol-to-olefins fields, are related to a kind of method and apparatus for reducing MTO device catalyst loss amount.Wherein, MTO device scrubbing tower or chilling tower tower bottom extraction water slurry are divided into two strands, one returns to MTO reactor as the water slurry circulation containing catalyst, the catalyst being carried along into scrubbing tower or chilling tower water slurry in recycling reaction process gas, another strand is used as outlet water slurry.Method of the invention can reduce the catalyst concn in water slurry, outside scrubbing tower or the identical water slurry of chilling tower under the conditions of discharge capacity, reduce catalyst outlet loss amount, achieve the purpose that reduce MTO device catalyst loss amount.
Description
Technical field
The invention belongs to methanol-to-olefins fields, more particularly, to a kind of side for reducing MTO device catalyst loss amount
Method and device.
Background technique
Methanol-to-olefins (MTO) device be under special molecular sieve catalyst effect, with the reactor of fluid bed mode,
Under suitable temperature, pressure condition, methanol is converted to the technical process of production ethylene, propylene.In fluidized-bed process, catalyst
A certain proportion of loss can be generated with process, for MTO since the reaction process of generation is large-minded, the loss of catalyst is very big
A part is generated as process gas is discharged.MTO catalyst price is higher, and the loss of catalyst becomes the weight of MTO technique
Want production cost.How to reduce loss of the catalyst in reaction and process gas washing process is the master that MTO technique is sought always
Want problem.
It after MTO charging methanol enters reactor, is contacted with catalyst, under fluidized state, with suitable reaction condition
Reaction conversion is carried out, the light olefins such as ethylene, propylene are generated.Converted product process gas carries certain catalyst fines, warp
It crosses two-stage or three-stage cyclone separator altogether and carries out gas, solid separation, most of catalyst fines are by two-stage or three-stage cyclone separator
Recycling returns to catalyst bed, and small part catalyst fines enter scrubbing tower or chilling tower through technique Gas Cooler with process gas,
It is washed in the tower with water circulation counter current contacting, the catalyst detergent carried in process gas is got off, process gas is avoided to take
Band catalyst fines enter follow-up process, influence device long-period stable operation.Catalyst fines under washing enter scrubbing tower
Or chilling tower tower bottom water slurry system, with water slurry outlet transmitting system.The catalyst fines of this part constitute that MTO device is main to urge
Agent consumption.
In old process design, scrubbing tower tower bottom water slurry outlet, the water slurry amount and water slurry solid content of outlet are directly determined
The catalyst fines quantity of outlet.The two-stage or three-stage cyclone separator gross efficiency of reaction system are certain, into scrubbing tower tower
The catalyst amounts that bottom water starches system are certain, and under conditions of outer displacement is certain, the catalyst concn in water slurry is determined therefrom that, outside
Therefore catalyst fines quantity, that is, catalyst that draining slurry carries is determined in the loss amount of reaction system.In scrubbing tower or chilling
In the case that the outer displacement of tower is certain, the catalyst solid powder concentration in water slurry how is reduced, so that catalyst loss is reduced,
It is an important topic.
Summary of the invention
The purpose of the present invention is overcoming the drawbacks described above of the prior art, a kind of reduction MTO device catalyst loss amount is provided
Method and apparatus.This method can significantly reduce the solid content of scrubbing tower or chilling tower tower bottom water slurry, to reduce outlet
Catalyst loss reduces MTO device production cost, improves its economic benefit.
To achieve the goals above, the present invention provides a kind of method for reducing MTO device catalyst loss amount, MTO device
Scrubbing tower or chilling tower tower bottom extraction water slurry are divided into two strands, one returns to MTO reaction as the water slurry circulation containing catalyst
Device recycles the catalyst being carried along into scrubbing tower or chilling tower water slurry in reaction process gas, and another strand is used as outlet water slurry.
According to the method for the present invention, the extraction water slurry that scrubbing tower or chilling tower tower bottom contain catalyst fines is divided into two
Part, a part are gone to subsequent process flow and are handled as bottom stream is got rid of outside, qualified discharge；Another part is made
For circulating reflux, MTO reactor freshening is returned, recycles the catalyst fines carried in water slurry.The water slurry amount of freshening is according to water slurry
The principle that solid content and MTO device processing capacity (device produce load rate) match determines, occupies reaction because water slurry recycles
Device air speed and residence time determine suitable water slurry internal circulating load, under the premise of keeping enough reaction processing capacities to reach
Control and reduce the purpose of catalyst loss in reaction system water slurry；Ordinary priority considers that water slurry internal circulating load accounts for the charging of MTO methanol
The 5-10% of amount, water slurry internal circulating load and the ratio of outlet water slurry amount are inversely proportional with water slurry solid content.Preferably, water slurry circulation with
The ratio of outlet water slurry is 0.1-5:1, most preferably 1:1.After the water slurry freshening for carrying catalyst, on the one hand recycling catalysis
Agent makes scrubbing tower or the water slurry of chilling tower bottom extract total amount out and increase accordingly, play dilution water on the other hand due to the freshening of water slurry
The effect of slurry, under the premise of reactor two stage or three-stage cyclone separation system total efficiency are basically unchanged, the solid in water slurry contains
Amount will accordingly decline, and under the conditions of maintaining discharge capacity outside identical water slurry, the catalyst amounts that outlet water slurry carries are reduced, MTO dress
The catalyst loss set is effectively reduced.
It according to the method for the present invention, can be for by filter by the water slurry circulation that scrubbing tower or chilling tower return to MTO reactor
Or the slurry containing catalyst solid particle of rotary filter press, or contain catalyst solid to be filtered or rotary filter press
The water slurry of grain；Preferably the former, can reduce the water into MTO reactor, avoid generating shadow to MTO methanol of reaction inlet amount
It rings.
According to the method for the present invention, the position that the water slurry is recycled back into MTO reactor can be catalyst dense-phase bed,
Or the dilute phase section of MTO reactor, it is preferred to use injection reaction end (i.e. the dilute phase section of MTO reactor).
According to the method for the present invention, it can be to be separately provided that the water slurry, which is recycled back into the feed entrance point of MTO reactor,
It can be the methanol feed line of MTO reactor, i.e., merge with methanol feed line；Or position at two is returned to simultaneously.
With the method for the invention it is preferred to which the condition of water slurry circulation is adjusted.Specifically, the water slurry circulation
PH value be preferably 2~9, further preferably 3~6.The temperature of water slurry circulation is chilling tower or scrubbing tower column bottom temperature,
Preferably, temperature is 80 DEG C~200 DEG C, and pressure is 0.15~1.5MPaG, and catalyst solid content is 100~10000mg/L.
According to the method for the present invention, the water slurry circulation can be by the way of be atomized/not being atomized, it is preferable that returns to MTO
Reactor is sprayed into using atomizer, with contact-enhancing effect.
The second aspect of the present invention provides a kind of MTO device for reducing catalyst loss amount, as shown in Figure 1, MTO device is washed
It washs tower or chilling tower tower bottom is provided with the pipeline being connected to MTO reactor.The position that the pipeline is connected to MTO reactor can be with
For catalyst dense-phase bed, or the dilute phase section of MTO reactor；It the part that the pipeline is connected to MTO reactor can be single
Solely setting, can also merge with methanol feed line.
Using methods and apparatus of the present invention, the scrubbing tower tower bottom water slurry extraction of MTO device is increased；Extraction water slurry is divided into
Two strands, with amount outlet that can be same as the prior art, another strand of direct circulation return to MTO reactor freshening for one；Water slurry circulation
Afterwards, catalyst solid dust concentration reduces in water slurry, and outside scrubbing tower or the identical water slurry of chilling tower under the conditions of discharge capacity, reduction is urged
Agent outlet loss amount achievees the purpose that reduce MTO device catalyst loss amount.
Other features and advantages of the present invention will then part of the detailed description can be specified.
Detailed description of the invention
Exemplary embodiment of the invention is described in more detail in conjunction with the accompanying drawings.
Fig. 1 is a kind of process flow diagram for the method and apparatus for reducing MTO device catalyst loss amount of the present invention.
Description of symbols
1, reactor；2, three rotation of reaction；3, product Gas Cooler；4, scrubbing tower/chilling tower；
A, methanol；B, process gas after washing；C, outlet water slurry；D, water slurry is recycled.
Specific embodiment
The preferred embodiment of the present invention is described in more detail below.Although the following describe preferred implementations of the invention
Mode, however, it is to be appreciated that may be realized in various forms the present invention without that should be limited by the embodiments set forth herein.
Embodiment 1
The present embodiment uses certain MTO device:
Former process: methanol inlet amount 225t/h, scrubbing tower tower bottom water slurry extracted amount 15t/h, solid content 3500mg/ in water slurry
L, it is 15 × 1000 × 3500/1000/1000=52.5kg/h, the loss of this partial catalyst that catalytic amount is carried in outlet water slurry
Unit consumption is 52.5/225=0.233kg/t methanol.
The present embodiment modified flow, inlet amount is constant as shown in Figure 1:, and scrubbing tower tower bottom extracts water slurry 30t/h, outlet out altogether
Water slurry is still 15t/h, recycles water slurry Returning reactor 15t/h, due to increasing water slurry extraction total amount, in reaction rotation subsystem effect
Under the premise of rate is basically unchanged, the catalyst solid content in water slurry obtains " diluting ", and the catalyst solid content in water slurry is
3500 × 15/30=1750mg/L.When draining slurry is still 15t/h outside, then water slurry carries outlet catalytic amount are as follows: 15 × 1000
× 1750/1000/1000=26.25kg/h, this partial catalyst loss unit consumption become 26.25/225=0.117kg/t methanol.
The loss of reaction system catalyst greatly reduces.
In view of the catalyst fines that water slurry circulation carries are more, rotation subsystem reduces this part thin powder recovery efficiency,
Nonetheless, reaction system catalyst loss unit consumption can also reduce 25%, i.e. unit consumption is down to 0.175kg/t methanol, catalyst damage
Mistake rate is still decreased significantly.
Embodiment 2
The present embodiment uses certain MTO device:
Former process: methanol inlet amount 225t/h, because of methanol feedstock deficiency, device rate of load condensate is reduced to 70%, revolves subsystem
Operating condition off-target point, efficiency decline, catalyst consumption rise.Scrubbing tower tower bottom water slurry extracted amount 12t/h, it is solid in water slurry
Content 4000mg/L, it is 12 × 1000 × 4000/1000/1000=48kg/h, this part that catalytic amount is carried in outlet water slurry
Catalyst loss unit consumption is 48/ (225 × 70%)=0.305kg/t methanol.
The present embodiment modified flow, inlet amount is constant as shown in Figure 1:, and scrubbing tower tower bottom extracts water slurry 35t/h, outlet out altogether
Water slurry is still 12t/h, is recycled back into reactor 23t/h, due to increasing water slurry extraction total amount, revolves subsystem efficiency base in reaction
Under the premise of this is constant, the catalyst solid content in water slurry obtains " diluting ", and the catalyst solid content in water slurry is 4000
× 12/35=1371mg/L.When draining slurry is still 12t/h outside, then water slurry carries outlet catalytic amount are as follows: 12 × 1000 ×
1371/1000/1000=16.45kg/h this partial catalyst loss unit consumption becomes 16.45/ (225 × 70%)=0.105kg/
T methanol.
The loss of reaction system catalyst greatly reduces.
In view of the catalyst fines that water slurry circulation carries are more, rotation subsystem reduces this part thin powder recovery efficiency,
Nonetheless, reaction system catalyst loss unit consumption can also be down to 0.205kg/t methanol, under catalyst loss rate still has significantly
Drop.
Various embodiments of the present invention are described above, above description is exemplary, and non-exclusive, and
It is not limited to disclosed each embodiment.Without departing from the scope and spirit of illustrated each embodiment, for this skill
Many modifications and changes are obvious for the those of ordinary skill in art field.
Claims (10)
1. a kind of method for reducing MTO device catalyst loss amount, which is characterized in that MTO device scrubbing tower or chilling tower tower bottom
Extraction water slurry is divided into two strands, one returns to MTO reactor, recycle in reaction process gas as the water slurry circulation containing catalyst
The catalyst being carried along into scrubbing tower or chilling tower water slurry, another strand is used as outlet water slurry.
2. the method according to claim 1 for reducing MTO device catalyst loss amount, which is characterized in that by scrubbing tower or
The water slurry circulation that chilling tower returns to MTO reactor is the slurry containing catalyst solid particle through filtering or rotary filter press, or
For filtered or rotary filter press the water slurry containing catalyst solid particle.
3. it is according to claim 1 reduce MTO device catalyst loss amount method, which is characterized in that water slurry circulation with
The ratio of outlet water slurry is 0.1-5:1, preferably 1:1.
4. the method according to claim 1 for reducing MTO device catalyst loss amount, which is characterized in that water slurry internal circulating load
Account for the 5-10% of MTO methanol inlet amount.
5. the method according to claim 1 for reducing MTO device catalyst loss amount, which is characterized in that the water slurry follows
Ring returns to the catalyst dense-phase bed of MTO reactor and/or the dilute phase section of MTO reactor.
6. the method according to claim 1 for reducing MTO device catalyst loss amount, which is characterized in that the water slurry follows
Ring returns to the feed entrance point of MTO reactor and is to be separately provided and/or is MTO reactor methanol feeding line.
7. the method according to claim 1 for reducing MTO device catalyst loss amount, which is characterized in that the water slurry follows
The pH value of ring is 2~9, preferably 3~6.
8. the method according to claim 1 for reducing MTO device catalyst loss amount, which is characterized in that the water slurry follows
The temperature of ring is 80 DEG C~200 DEG C, and pressure is 0.15~1.5MPaG, and catalyst solid content is 100~10000mg/L.
9. the method according to claim 1 for reducing MTO device catalyst loss amount, which is characterized in that the water slurry follows
Ring is returned to MTO reactor and is sprayed into using atomizer.
10. a kind of MTO device for reducing catalyst loss amount, which is characterized in that MTO device scrubbing tower or the setting of chilling tower tower bottom
There is the pipeline being connected to MTO reactor.
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| CN201810284110.3A CN110343028A (en) | 2018-04-02 | 2018-04-02 | A kind of method and apparatus reducing MTO device catalyst loss amount |
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| CN201810284110.3A CN110343028A (en) | 2018-04-02 | 2018-04-02 | A kind of method and apparatus reducing MTO device catalyst loss amount |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115197738A (en) * | 2021-04-09 | 2022-10-18 | 中国石化工程建设有限公司 | Method and system for preparing olefin from methanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5264645A (en) * | 1991-03-07 | 1993-11-23 | Institut Francais Du Petrole | Process and apparatus for the catalytic conversion of a charge containing an oxygen compound comprising the quenching and simultaneous separation of the products formed and the catalyst |
| CN1942558A (en) * | 2004-04-15 | 2007-04-04 | 环球油品公司 | Wet scrubbing and recycle of effluent-contaminating catalyst particles in an oxygenate-to-olefin process |
| CN107382654A (en) * | 2017-09-01 | 2017-11-24 | 上海华畅环保设备发展有限公司 | Methanol-to-olefins chilled water (chw) ebullated bed separation method and device |
-
2018
- 2018-04-02 CN CN201810284110.3A patent/CN110343028A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5264645A (en) * | 1991-03-07 | 1993-11-23 | Institut Francais Du Petrole | Process and apparatus for the catalytic conversion of a charge containing an oxygen compound comprising the quenching and simultaneous separation of the products formed and the catalyst |
| CN1942558A (en) * | 2004-04-15 | 2007-04-04 | 环球油品公司 | Wet scrubbing and recycle of effluent-contaminating catalyst particles in an oxygenate-to-olefin process |
| CN107382654A (en) * | 2017-09-01 | 2017-11-24 | 上海华畅环保设备发展有限公司 | Methanol-to-olefins chilled water (chw) ebullated bed separation method and device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115197738A (en) * | 2021-04-09 | 2022-10-18 | 中国石化工程建设有限公司 | Method and system for preparing olefin from methanol |
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Application publication date: 20191018 |