CN109422617A - Reaction-regenerative device and application thereof - Google Patents
Reaction-regenerative device and application thereof Download PDFInfo
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- CN109422617A CN109422617A CN201710766917.6A CN201710766917A CN109422617A CN 109422617 A CN109422617 A CN 109422617A CN 201710766917 A CN201710766917 A CN 201710766917A CN 109422617 A CN109422617 A CN 109422617A
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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
- C07C1/24—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by elimination of water
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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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/82—Phosphates
- C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
- C07C2529/85—Silicoaluminophosphates (SAPO compounds)
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Abstract
The present invention relates to a kind of reaction-regenerative devices and application thereof.The reaction-regenerative device includes reactor and regenerator；The reactor is connected by inclined tube to be generated with regenerator sloped tube with the regenerator；It is characterized in that, the reactor includes: (a) fast fluidized bed reaction zone；The second end that the fast fluidized bed reaction zone has the first end of injecting catalyst and flows out from the fast fluidized bed reaction zone for catalyst；(b) intend promoting reaction zone；The quasi- promotion reaction zone is connected with the mode of the fast fluidized bed reaction zone in fluid communication；(c) riser reaction zone；The riser reaction zone is connected with the quasi- mode of reaction zone in fluid communication that promoted.The reaction-regenerative device can be used for oxygenatedchemicals into the conversion reaction of alkene.
Description
Technical field
The present invention relates to a kind of reaction-regenerative devices and application thereof.
Background technique
Low-carbon alkene, i.e. ethylene and propylene, are two kinds of important basic chemical industry raw materials, and demand is being continuously increased.One
As, ethylene, propylene are produced by petroleum path, but due to the limited supply of petroleum resources and higher price, by
Petroleum resources produce ethylene, the cost of propylene is continuously increased.In recent years, people start to greatly develop alternative materials conversion second processed
The technology of alkene, propylene.Wherein, a kind of important alternative materials for low-carbon alkene production are oxygenatedchemicals, such as alcohols
(methanol, ethyl alcohol), ethers (dimethyl ether, ethyl methyl ether), esters (dimethyl carbonate, methyl formate) etc., these oxygenatedchemicals can
With by the energy conversions such as coal, natural gas, biomass come.Certain oxygenatedchemicals can achieve fairly large life
It produces, such as methanol can be made by coal or natural gas, and technique is very mature, and the production scale of 10,000 tons up to a hundred may be implemented.Due to
The popularity in oxygenatedchemicals source, along with the economy for being converted into low-carbon alkene technique, so being turned by oxygenatedchemicals
The technique for changing alkene (OTO) processed, is especially more and more paid attention to by the technique of preparing olefin by conversion of methanol (MTO).
Document US4499327, which is applied to preparing olefin by conversion of methanol technique to silicoaluminophosphamolecular molecular sieve catalyst, to have carried out in detail
Research, it is believed that SAPO-34 is the preferred catalyst of MTO technique.SAPO-34 catalyst has very high selectivity of light olefin,
And activity is also higher, and the reaction time that methanol can be made to be converted into low-carbon alkene is less than 10 seconds degree, is more even up to
In the reaction time range of riser.
MTO reactor includes the fluidizations pattern such as bubbling fluidized bed, turbulent fluidized bed, fast fluidized bed at present.For example, literary
It offers US6166282 and discloses technology and reactor that a kind of methanol is converted into low-carbon alkene, using fast fluidized bed reaction zone, gas
Mutually the lower Mi Xiangfanyingqu of gas velocity after the reaction was completed, after rising to the fast subregion that internal diameter rapidly becomes smaller, using special gas
Gu separation equipment initial gross separation goes out most entrained catalyst.Due to product gas and catalyst quick separating after reaction, effectively
The generation for preventing secondary response.It is calculated through simulation, compared with traditional bubbling fluidized bed reactor, the fast fluidized bed is anti-
Reserve needed for answering area's internal diameter and catalyst greatly reduces.Document CN1723262A is disclosed with the more of central catalyst return
Grade riser reaction unit is converted into low-carbon alkene technique for oxide, which includes multiple riser reactors, gas
Gu Disengagement zone, multiple offset components etc., each riser reactor respectively has the port of injecting catalyst, is pooled to setting
Disengagement zone separates catalyst and product gas.
Summary of the invention
The present invention provides a kind of new reaction-regenerative device.
Specifically, the present invention relates to a kind of reaction-regenerative device, including reactor and regenerator；The reactor and
The regenerator is connected by inclined tube to be generated with regenerator sloped tube；It is characterized in that, the reactor includes:
(a) fast fluidized bed reaction zone；The fast fluidized bed reaction zone has the first end of injection raw material and for first
The second end that product is flowed out from the fast fluidized bed reaction zone；
(b) intend promoting reaction zone；The quasi- reaction zone that promoted has the first end of the first product of injection and supplies the second product
The second end flowed out from the quasi- promotion reaction zone；The quasi- promotion reaction zone and the fast fluidized bed reaction zone are with fluid
The mode communicated is connected；
(c) riser reaction zone；The riser reaction zone has the first end of the second product of injection and for third product
The second end flowed out from the riser reaction zone；The riser reaction zone and the quasi- promotion reaction zone are in fluid communication
Mode be connected.
According to an aspect of the present invention, the fast fluidized bed reaction zone, the quasi- promotion reaction zone and the promotion
Tube reaction area has the central axis being overlapped.
According to an aspect of the present invention, the reactor further comprises: (d) reactor dense bed；The quasi- promotion
Reaction zone is configured in the reactor dense bed.
According to an aspect of the present invention, the reactor dense bed passes through reactor cycles inclined tube and the fast fluidization
Bed reaction zone is connected.
According to an aspect of the present invention, reactor dense bed lower part is configured with distribution rings, and the distribution rings are surround
Configuration is in the quasi- promotion reaction zone periphery.
According to an aspect of the present invention, the reactor further comprises: (e) reactor settling section；The riser
Reaction zone is configured in the reactor settling section.
According to an aspect of the present invention, mode phase of the reactor settling section with reactor dense bed in fluid communication
Even.
According to an aspect of the present invention, the reactor further comprises: (f) reactor level-one separation equipment；It is described
Reactor level-one separation equipment is configured at the second end of the riser reaction zone.
According to an aspect of the present invention, the reactor level-one separation equipment is cyclone separator.
According to an aspect of the present invention, the reactor further comprises: (g) reactor the second-order separation equipment；It is described
Reactor the second-order separation device configuration is in reactor settling section top.
According to an aspect of the present invention, the reactor the second-order separation equipment is cyclone separator.
According to an aspect of the present invention, the reactor further comprises: (h) reactor three-level separation equipment；It is described
Reactor three-level separation equipment is configured at outside reactor settling section.
According to an aspect of the present invention, negative pressure discharging type cyclonic separation is configured in the reactor three-level separation equipment
Device；The fluid inlet of the negative pressure discharging type cyclone separator is not attached to reactor the second-order separation equipment outlet gas line.
According to an aspect of the present invention, the reactor three-level separation equipment lower part is dense fluidized bed, and solid is close
Degree is greater than 400kg/m3；Dense fluidized bed bottom is configured with reactor fluidizing agent suction line.
According to an aspect of the present invention, the reactor three-level separation equipment is urged configured with product gas outlet and reactor
Agent feed opening；The reactor catalyst feed opening is connected with fast fluidized bed reaction zone.
According to an aspect of the present invention, the reactor further comprises: (i) reactor external warmer；The reaction
It is connected configured with the first gas line of return with reactor settling section at the top of device external warmer；Match reactor external warmer bottom
The first inclined tube is equipped with to be connected with fast fluidized bed reaction zone；The reactor external warmer is close configured with the second inclined tube and reactor
Phase bed is connected.
According to an aspect of the present invention, the reactor further comprises: (j) reactor stripper；The reactor
Stripper is connected with the mode of reactor dense bed in fluid communication；The reactor stripper is connected with inclined tube to be generated.
According to an aspect of the present invention, the fast fluidized bed reaction zone is adopted in place of being connected with the quasi- promotion reaction zone
Use conical transition；The quasi- promotion reaction zone is connected place with the riser reaction zone using conical transition.
According to an aspect of the present invention, the fast fluidized bed reaction zone is connected with regenerator sloped tube.
According to an aspect of the present invention, the fast fluidized bed reaction zone, the quasi- promotion reaction zone, the riser
The diameter ratio of reaction zone is (1.5~5): 1:(0.2~0.7).
According to an aspect of the present invention, the regenerator includes:
(1) burning tank renewing zone；The burning tank renewing zone has the first end for injecting regenerative raw materials gas and confession first again
The second end that production object is flowed out from the burning tank renewing zone；
(2) dense bed renewing zone；The dense bed renewing zone has the first end of the first regeneration product of injection and for second
The second end that regeneration product is flowed out from the dense bed renewing zone；The dense bed renewing zone and the burning tank renewing zone with
The mode of fluid communication is connected.
According to an aspect of the present invention, the regenerator further comprises:
(3) regenerator settling section；Mode phase of the regenerator settling section with the dense bed renewing zone in fluid communication
Even；
(4) regenerator level-one separation equipment and the second-order separation equipment；The regenerator level-one separation equipment and the second-order separation
Device configuration is in the regenerator settling section；
(5) external catalyst cooler for regenerator；The second gas line of return and regenerator are configured at the top of the external catalyst cooler for regenerator
Settling section is connected；The external catalyst cooler for regenerator bottom is connected configured with third inclined tube with burning tank renewing zone；The regenerator
External warmer is connected configured with the 4th inclined tube with dense bed renewing zone；
(6) degassing tank；It is connected configured with the third gas line of return with regenerator settling section at the top of the degassing tank；It is described de-
Gas tank bottom is connected with regenerator sloped tube；The degassing tank is connected configured with the 5th inclined tube with dense bed renewing zone.
According to an aspect of the present invention, the regenerator level-one separation equipment and the second-order separation equipment are cyclonic separation
Device, the regenerator level-one separation equipment and the second-order separation equipment are with the configuration substantially symmetrical about its central axis of regenerator settling section.
According to an aspect of the present invention, the regenerator further comprises: (7) regenerator three-level separation equipment；It is described
Regenerator three-level separation equipment is configured at outside regenerator settling section；The regenerator three-level separation equipment is configured with regenerated flue gas
Outlet and regenerator catalyst feed opening；The regenerator catalyst feed opening is connected with burning tank renewing zone.
According to an aspect of the present invention, negative pressure discharging type cyclonic separation is configured in the regenerator three-level separation equipment
Device；The fluid inlet of the negative pressure discharging type cyclone separator is not attached to regenerator the second-order separation equipment outlet gas line.
According to an aspect of the present invention, the regenerator three-level separation equipment lower part is dense fluidized bed, and solid is close
Degree is greater than 400kg/m3；Dense fluidized bed bottom is configured with regenerator fluidizing agent suction line.
According to an aspect of the present invention, the burning tank renewing zone is connected with inclined tube to be generated.
According to an aspect of the present invention, burning tank renewing zone exterior arrangement have regenerator recycle inclined tube, it is described again
Raw device circulation inclined tube is connected with the dense bed renewing zone.
According to an aspect of the present invention, the burning tank renewing zone is connected place with the dense bed renewing zone using circle
Tapering transition.
According to an aspect of the present invention, the diameter ratio of the burning tank renewing zone and the dense bed renewing zone is
(0.3~0.95): 1.
The invention further relates to a kind of purposes of reaction-regenerative device.
Specifically, conversion reaction of the reaction-regenerative device for oxygenatedchemicals to alkene.
According to an aspect of the present invention, in the fast fluidized bed reaction zone, linear velocity V1For 1.0~2.0 meter per seconds,
Residence time is 4~7 seconds；In the quasi- promotion reaction zone, linear velocity V2For 2.5~5 meter per seconds, the residence time is 1.5~
3.5 the second；In the riser reaction zone, linear velocity V3For 7~12 meter per seconds, the residence time is 0.8~1.4 second.
Beneficial effects of the present invention: the present inventor is the study found that MTO reaction belongs to fast reaction, and the product generated is rich
Containing low-carbon alkene, low-carbon alkene is easy to that secondary response occurs, and selectivity of light olefin is caused to reduce.Therefore, it is necessary to rationally advise
Reaction process is drawn, while being aided with gas-solid quick separating measure, the process of rationally control reaction reaches raising selectivity of light olefin
Purpose.Using the method for the present invention, three reaction zones, the linear velocity V in fast fluidized bed reaction zone are set1, quasi- promote reaction
Linear velocity V in area2It is V with the linear velocity in riser reaction zone3Relationship are as follows: V3>V2>V1, main reaction region is fast fluidization
Bed reaction zone, converts most of methanol, and methanol conversion reaches 70~85 weight %, and the most low-carbon alkene of production, obtains
To the first product.First product enters quasi- promotion reaction zone and is further continued for conversion one in high linear speed, under the short residence time
Divide methanol, methanol conversion reaches 90~96 weight %, while preventing olefin product back-mixing and secondary response occurs, and obtains second
Product.Second product enters riser reaction zone, and in higher linear speed, under the shorter residence time, remaining methanol is fallen in conversion.
For the quasi- Gas-particle Flows promoted in reaction zone and riser reaction zone close to plug flow, gas-solid back-mixing is small, can prevent to greatest extent
The generation of secondary response realizes that the target for improving selectivity of light olefin, the selectivity of low-carbon alkene can be up to 82 weight %.
Regenerator uses the two-stage regeneration technology of Highspeed Bed and dense bed, and catalyst transport all uses gravity stream inclined tube to convey,
Catalyst flow impetus is big, and reaction-regeneration cycle flowing is steady, achieves preferable technical effect.
Detailed description of the invention
Fig. 1 is the schematic diagram of reaction-regenerative device of the invention.
In Fig. 1,1 is reactor shell, and 2 be fast fluidized bed reaction zone, and 21 be fast fluidized bed reaction zone first end, 22
Reaction zone is promoted to be quasi- for fast fluidized bed reaction zone second end, 3,31 are promoted instead to intend being promoted reaction zone first end, 32 to be quasi-
Area's second end is answered, 4 be riser reaction zone, and 41 be riser reaction zone first end, and 42 be riser reaction zone second end, and 5 are
Reactor dense bed, 6 be reactor settling section, and 7 be reactor level-one separation equipment, and 8 be reactor the second-order separation equipment, and 9 are
Reactor three-level separation equipment, 91 be product gas outlet, and 92 be reactor catalyst feed opening, and 10 be reactor external warmer,
101 be the first gas line of return, and 102 be the second inclined tube, and 103 be the first inclined tube, and 11 be stripper, and 12 is oblique for reactor cycles
Pipe, 13 be reactor the second-order separation equipment outlet gas line, and 14 be inclined tube to be generated, and 15 be regenerator sloped tube, and 16 is former for reactor
Expect suction line, 17 be regenerator shell, and 18 be burning tank renewing zone, and 181 be burning tank renewing zone first end, and 182 be to burn
Tank renewing zone second end, 19 be dense bed renewing zone, and 191 be dense bed renewing zone first end, and 192 be dense bed renewing zone second
End, 23 be regenerator settling section, and 24 be regenerator level-one separation equipment, and 25 be regenerator the second-order separation equipment, and 26 be regenerator
Three-level separation equipment, 261 be regenerated flue gas outlet line, and 262 be regenerator catalyst feed opening, and 27 be regenerator outside heat removing
Device, 271 be the second gas line of return, and 272 be the 4th inclined tube, and 273 be third inclined tube, and 28 be degassing tank, and 281 return for third gas
Loop line, 282 be the 5th inclined tube, and 29 recycle inclined tube for regenerator, and 30 be regenerator the second-order separation equipment outlet gas line, and 33 are
Regenerative raw materials gas suction line.
The present invention is described in detail with reference to the accompanying drawing, it should be noted however that protection scope of the present invention is simultaneously
By this, this is not limited, and but is determined by the appended claims.
All publications, patent application, patent and the other bibliography that this specification is mentioned all draw in this for reference.
Unless otherwise defined, all technical and scientific terms used herein all has what those skilled in the art routinely understood to contain
Justice.In case of conflict, it is subject to the definition of this specification.
When this specification with prefix " well known to those skilled in the art ", " prior art " or its export material similar to term
Whens material, substance, method, step, device or component etc., object derived from the prefix is covered this field when the application proposes and is routinely made
Those of with, but also include also being of little use at present, it will but become art-recognized for suitable for those of similar purpose.
It should be strongly noted that two or more aspects (or embodiment) disclosed in the context of the present specification
Any combination, the technical solution formed therefrom it can belong to a part of this specification original disclosure each other, while
It falls under the scope of the present invention.
The present invention relates to a kind of reaction-regenerative devices.The reaction-regenerative device includes reactor and regenerator；It is described
Reactor is connected by inclined tube to be generated with regenerator sloped tube with the regenerator.
According to an aspect of the present invention, the reactor includes: reactor shell 1, fast fluidized bed reaction zone 2, intends
Promote reaction zone 3 and riser reaction zone 4.Fast fluidized bed reaction zone 2 has the first end 21 of injection raw material, and supplies first
The second end 22 that product is flowed out from fast fluidized bed reaction zone 2.The quasi- first end for promoting reaction zone 3 and there is the first product of injection
31, and the second end 32 flowed out in reaction zone 3 is promoted from quasi- for the second product.Riser reaction zone 4 has the second product of injection
First end 41, and for second end 42 that third product is flowed out from riser reaction zone 4.It is quasi- to promote reaction zone 3 and quickly stream
Change the mode of bed reaction zone 2 in fluid communication to be connected.The mode of riser reaction zone 4 and quasi- promotion reaction zone 3 in fluid communication
It is connected.
According to an aspect of the present invention, fast fluidized bed reaction zone 2, quasi- promotion reaction zone 3 and riser reaction zone 4
Central axis with coincidence.Preferably, fast fluidized bed reaction zone 2 is cylinder-shaped.It is quasi- to promote reaction zone 3 and riser reaction zone
The variation range of 4 geometry is very extensive, can be circle tube member, is also possible to triangular prism, rectangle or square
Wedge, preferably circle tube member.
According to an aspect of the present invention, fast fluidized bed reaction zone 2 is connected place using circular cone with the quasi- reaction zone 3 that promoted
Shape transition.
According to an aspect of the present invention, intend being promoted in place of reaction zone 3 is connected with riser reaction zone 4 using conical mistake
It crosses.
According to an aspect of the present invention, fast fluidized bed reaction zone 2, quasi- promote reaction zone 3, riser reaction zone 4
Diameter ratio is (1.5~5): 1:(0.2~0.7).
According to an aspect of the present invention, reactor further comprises reactor dense bed 5.Reactor shell 1 has determined
Reactor dense bed.The quasi- reaction zone 3 that promoted is configured in reactor dense bed 5.
According to an aspect of the present invention, reactor dense bed 5 is anti-by reactor cycles inclined tube 12 and fast fluidized bed
Area 2 is answered to be connected.
According to an aspect of the present invention, 5 lower part of reactor dense bed is configured with distribution rings, which exists around configuration
It is quasi- to promote 3 periphery of reaction zone.
According to an aspect of the present invention, reactor further comprises reactor settling section 6.Riser reaction zone 4 configures
In in reactor settling section 6.Reactor shell 1 has determined reactor settling section, in reactor settling section reaction product with urge
Agent separation.
According to an aspect of the present invention, mode phase of the reactor settling section 6 with reactor dense bed 5 in fluid communication
Even.
According to an aspect of the present invention, reactor further comprises reactor level-one separation equipment 7.Level-one separation is set
Standby 7 are configured at the second end of riser reaction zone 4.Level-one separation equipment is used to separate the product and catalyst in third product.
Level-one separation equipment, which can be, to set cyclone separator that reaction product is separated with catalyst, filter, strainer, shock
Standby, plate, taperer or any other equipment, preferably cyclone separator (referred to as one rotation).After a rotation separation, about 70%
The catalyst granules of granularity 20um or more is separated.
According to an aspect of the present invention, reactor dense bed, reactor settling section pass through reactor level-one separation equipment
It is connected with quasi- promotion reaction zone, the mode of riser reaction zone in fluid communication.
According to an aspect of the present invention, reactor further comprises reactor the second-order separation equipment 8.The second-order separation is set
It is standby to be configured at 6 top of reactor settling section, it is urged for further separate that reacted device level-one separation equipment do not separate
Agent fine powder.Reactor the second-order separation equipment can be the cyclone separator that can separate reaction product with catalyst, filtering
Device, strainer, percussion device, plate, taperer or any other equipment, preferably cyclone separator (referred to as two rotations).Through two rotations
After separation, 99~99.5% catalyst fines (referring generally to granularity 20um catalyst below) are separated and return to close phase
Bed.
According to an aspect of the present invention, reactor further comprises reactor three-level separation equipment 9.Three-level separation is set
It is standby to be configured at outside settling section 6.Configured with cyclone separator (referred to as three rotations) in the three-level separation equipment, the fluid of three rotations enters
Mouthful with the pipeline that is connected (the reactor the second-order separation device product tracheae between reactor settling section and reactor three-level separation equipment
Line 13) it is not attached to.The three-level separation equipment lower part is dense fluidized bed, and density of solid is greater than 400kg/m3；The dense fluidized
Bed bottom is configured with fluidizing agent suction line (not shown).That is: in three-level separation equipment, three rotations are preferably negative pressure row
Material formula cyclone separator, the dense fluidized bed of three-level separation equipment lower part, plays sealing, prevents product gas from passing through catalyst
Feed opening brings fast bed reaction zone into again.After three-level separation equipment, 99.9% or more catalyst fines are separated.
According to an aspect of the present invention, reactor three-level separation equipment 9 is urged configured with product gas outlet 91 and reactor
Agent feed opening 92.Reactor catalyst feed opening 92 is connected with fast fluidized bed reaction zone 2.
According to an aspect of the present invention, the pipeline that reactor catalyst feed opening is connected with fast bed reaction zone is equipped with
Solid buffer tank (not shown), reactor catalyst feed opening are connected by pipeline with solid buffer tank, solid buffer tank
The pipeline being connected with fast bed reaction zone is equipped with slide valve；The solid buffer tank top is equipped with nitrogen inlet pipeline.That is, using
The catalyst fines that three-level separation equipment separates are initially entered solid buffer tank by the mode of interval, when reaching a fixed number
After amount, fast bed reaction zone is delivered to by the nitrogen of solid buffer tank deck.
According to an aspect of the present invention, reactor further comprises reactor external warmer 10.Reactor external warmer
10 tops are connected configured with the first gas line of return 101 with reactor settling section 6.10 bottom of reactor external warmer is configured with the
One inclined tube 103 is connected with fast fluidized bed reaction zone 2.10 lower part of reactor external warmer configured with the second inclined tube 102 with react
Device dense bed 5 is connected.
According to an aspect of the present invention, reactor further comprises stripper 11.The stripper and reactor dense bed 5
Mode in fluid communication is connected.Reclaimable catalyst enters regenerator after stripping, through inclined tube 14 to be generated.Catalyst after regeneration
Enter fast fluidized bed reaction zone 2 through regenerator sloped tube 15.
According to an aspect of the present invention, the regenerator includes: regenerator shell 17, burning tank renewing zone 18 and close
Phase bed renewing zone 19.Burning tank renewing zone 18 has the first end 181 of injection regenerative raw materials gas, and supplies the first regeneration product from burning
The second end 182 flowed out in burnt tank renewing zone 18.Dense bed renewing zone 19 has the first end 191 of the first regeneration product of injection,
With the second end 192 flowed out from dense bed renewing zone 19 for the second regeneration product.Dense bed renewing zone 19 and burning tank regenerate
The mode of area 18 in fluid communication is connected.
According to an aspect of the present invention, burning tank renewing zone 19 is connected place with dense bed renewing zone 18 using cone
Transition.
According to an aspect of the present invention, the diameter ratio of burning tank renewing zone 19 and dense bed renewing zone 18 be (0.3~
0.95):1。
According to an aspect of the present invention, regenerator further comprises: regenerator settling section 23, the separation of regenerator level-one are set
Standby 24 and the second-order separation equipment 25, external catalyst cooler for regenerator 27 and degassing tank 28.Regenerator shell 17 has determined that regenerator is heavy
Section 23 drops.Regenerator settling section 23 is connected with the mode of dense bed renewing zone 19 in fluid communication.Regenerator level-one separation equipment
With the second-order separation device configuration in regenerator settling section 23.Regenerator level-one separation equipment and the second-order separation equipment are whirlwind point
From device, regenerator level-one separation equipment and the second-order separation equipment are with the configuration substantially symmetrical about its central axis of regenerator settling section 23.Regenerator
It is connected configured with the second gas line of return 271 with regenerator settling section 23 at the top of external warmer 27.27 bottom of external catalyst cooler for regenerator
Portion is connected configured with third inclined tube 273 with burning tank renewing zone 18.External catalyst cooler for regenerator 27 configured with the 4th inclined tube 272 with it is close
Phase bed renewing zone 19 is connected.It is connected configured with the third gas line of return 281 with regenerator settling section 23 at the top of degassing tank 28.Degassing
Pot bottom is connected with regenerator sloped tube 15.Degassing tank is connected configured with the 5th inclined tube 282 with dense bed renewing zone.
According to an aspect of the present invention, regenerator further comprises: regenerator three-level separation equipment 26.Regenerator three-level
Separation equipment 26 is configured at outside regenerator settling section 23.Regenerator three-level separation equipment 26 is configured with regenerated flue gas outlet 261
With regenerator catalyst feed opening 262.Regenerator catalyst feed opening 262 is connected with burning tank renewing zone 18.
According to an aspect of the present invention, the pipe that regenerator catalyst feed opening 262 is connected with burning tank renewing zone 18
Line is equipped with solid buffer tank (not shown), and regenerator catalyst feed opening is connected by pipeline with solid buffer tank, Gu
The pipeline that body surge tank is connected with burning tank renewing zone is equipped with slide valve；The solid buffer tank top is equipped with nitrogen inlet tube
Line.That is: by the way of interval, the catalyst fines that three-level separation equipment separates are initially entered into solid buffer tank, when
After reaching certain amount, burning tank renewing zone is delivered to by the nitrogen of solid buffer tank deck.
According to an aspect of the present invention, negative pressure discharging type cyclone separator is configured in regenerator three-level separation equipment.
The fluid inlet of negative pressure discharging type cyclone separator is not attached to regenerator the second-order separation equipment outlet gas line 30.
According to an aspect of the present invention, regenerator three-level separation equipment lower part is dense fluidized bed, and density of solid is big
In 400kg/m3；Dense fluidized bed bottom is configured with regenerator fluidizing agent suction line.
According to an aspect of the present invention, burning tank renewing zone 18 is connected with inclined tube 14 to be generated.By inclined tube to be generated, come from
The reclaimable catalyst of reactor enters burning tank renewing zone.
According to an aspect of the present invention, 18 exterior arrangement of burning tank renewing zone has regenerator to recycle inclined tube 29, regenerator
Circulation inclined tube is connected with dense bed renewing zone.
Reaction-regenerative device shown in FIG. 1 is operated in the following manner.
The reacted feed inlet lines 16 of raw material, fast fluidized bed reaction zone first end 21 are reacted into fast fluidized bed
Area 2 is contacted with the catalyst entered through regenerator sloped tube 15, obtains the first product.First product is from fast fluidized bed reaction zone
The outflow of two ends 22 promotes reaction zone first end 31 through quasi-, into quasi- promotion reaction zone 3.First product it is quasi- promoted reaction zone 3 after
Continuous reaction, obtains the second product.Second product is flowed out from quasi- promotion reaction zone second end 32, boosted tube reaction area first end into
Enter 41, into riser reaction zone 4.The reaction was continued in riser reaction zone 4 for second product, obtains third product.Third product
It is flowed out from riser reaction zone second end 42, into level-one separation equipment 7.Third product is after the separation of level-one separation equipment, greatly
Partial catalyst is separated into 6 bottom of settling section, and what gaseous products and part were not separated by level-one separation equipment
Catalyst enters the second-order separation equipment 8 and is separated again.Sedimentation is likewise entered by the catalyst that the second-order separation equipment is isolated
6 bottoms of section, and gaseous products do not enter three-level separation equipment 9 by the catalysis that the second-order separation equipment separates yet with part and carry out three times
Separation.Enter subsequent centrifugal station through product gas outlet 91 by the gaseous products after the separation of three-level separation equipment, and isolates
Catalyst through catalyst feed opening 92 return fast fluidized bed reaction zone 2.It is separated by level-one separation equipment, the second-order separation equipment
Out, the catalyst into settling section bottom be divided into three parts, a part enters external warmer 10 by the second inclined tube 102, changes
Fast fluidized bed reaction zone 2 is returned to through the first inclined tube 103 after heat；A part is after the stripping of stripper 11 through inclined tube 14 to be generated
Into regenerator coke-burning regeneration, the catalyst for regenerating completion returns to fast fluidized bed reaction zone 2 by regenerator sloped tube 15；One
Lease making crosses circulation inclined tube 12 back to fast fluidized bed reaction zone 2.
Regenerative raw materials gas is regenerated through regenerative raw materials gas suction line 33, burning tank renewing zone first end 181 into burning tank
Area 18 contacts with the catalyst entered through inclined tube 14 to be generated, obtains the first regeneration product.First regeneration product is regenerated from burning tank
Area's second end 182 flows out, through dense bed renewing zone first end 191, into dense bed renewing zone 19.First regeneration product is in close phase
Bed renewing zone 19 continues to regenerate, and obtains the second regeneration product.Second regeneration product is flowed out from dense bed renewing zone second end 192,
Into regenerator settling section 23.Regenerator level-one separation equipment and the second-order separation equipment are configured in regenerator settling section 23.The
After the second-order separation, most of catalyst is separated into 23 bottom of regenerator settling section two regeneration products, and gas phase produces
Product and part do not enter three-level separation equipment 26 by isolated catalyst and continue to separate.By the gas after the separation of three-level separation equipment
Phase product enters subsequent centrifugal station through regenerated flue gas outlet line 261, and the catalyst isolated is through regenerator catalyst
Feed opening 262 returns to burning tank renewing zone 18.Be reproduced device level-one separation equipment, the second-order separation equipment is isolated, into heavy
The catalyst of drop 23 bottom of section is divided into three parts, and a part enters external catalyst cooler for regenerator 27 by the 4th inclined tube 272, after heat exchange
Burning tank renewing zone 18 is returned to through third inclined tube 273；A part returns fastly after the degassing of degassing tank 28 through regenerator sloped tube 15
Fast fluidized bed reaction zone 2；A part returns to burning tank renewing zone 18 by regenerator circulation inclined tube 29.
The invention further relates to a kind of purposes of reaction-regenerative device.The reaction-regenerative device is used for oxygenatedchemicals extremely
The conversion reaction of alkene.
According to an aspect of the present invention, in the conversion reaction of oxygenatedchemicals to alkene, it is being enough oxygen-containing chemical combination
Object is converted under conditions of alkene, by contacting oxygen compound feedstock with catalyst, makes oxygenate conversion at alkene.
During by oxygenate conversion at alkene, using the charging containing oxygenatedchemicals.Made herein
Term " oxygenatedchemicals " is defined to include but is not necessarily to be confined to oxygen-containing hydrocarbon, such as fatty alcohol, ether, carbonyls
Or mixtures thereof (aldehyde, ketone, carboxylic acid, carbonic ester etc.).Preferred aliphatic portion should contain 1-10 carbon atom, more preferably
It is containing 1-4 carbon atom.Typical oxygenatedchemicals includes but is not necessarily to be confined to the linear chain or branched chain rouge of lower molecular weight
Fat alcohol and their unsaturated counterpart.The example of suitable oxygenatedchemicals includes but is not necessarily to be confined to: methanol,
Ethyl alcohol, normal propyl alcohol, isopropanol, C4-C10 alcohol, methyl ethyl ether, dimethyl ether, diethyl ether, diisopropyl ether, methyl formate, formaldehyde,
Dimethyl carbonate, methyl ethyl carbonate, acetone and its mixture.Preferably, for the oxygen-containing chemical combination of hydrocarbon conversion reaction
Object is selected from the group as composed by methanol, dimethyl ether and its mixture.Preferred oxygenatedchemicals is methanol.
During by oxygenate conversion at alkene, desired target product is alkene.Made herein
Term " alkene " is defined to include but is not necessarily to be confined to the alkene containing 1-4 carbon atom, preferably by ethylene
And propylene.
Catalyst suitable for being catalyzed the conversion reaction of oxygenatedchemicals to alkene includes: the mixing of molecular sieve and molecular sieve
Object.Silicoaluminophosphamolecular molecular sieve (SAPO) is one group of molecular sieve for being suitable for oxygenatedchemicals to olefin reaction, including
SAPO-5、SAPO-8、SAPO-11、SAPO-16、SAPO-17、SAPO-18、SAPO-20、SAPO-31、SAPO-34、SAPO-
35, SAPO-36, SAPO-37, SAPO-40, SAPO-41, SAPO-42, SAPO-44, SAPO-47, SAPO-56, and its contain metal
Form and its mixture.Preferably SAPO-18, SAPO-34, SAPO-35, SAPO-44 and SAPO-47, more preferably
SAPO-34, including its metalliferous form.Term " mixture " adopted here be it is synonymous with " composition ", be considered
The composition with two or more components, the ratio of the component can change, but regardless of they physical state how.
As replacing SAPO to form " MeAPSO " molecular sieve well known to one kind, this molecular sieve is also used for the present invention.With
In the method for preparing MeAPSO be well known for those skilled in the art.SAPO with substituent group, such as MeAPSO are also suitable
In the present invention.Suitable substituent group " Me " includes but is not necessarily to be confined to: nickel, cobalt, manganese, zinc, titanium, strontium, magnesium, barium and calcium.It is closing
At substituent group can be mixed when MeAPSO.In addition, substituent group can be mixed using a variety of methods after synthesizing SAPO or MeAPSO.
These methods include but are not necessarily to be confined to, ion exchange, dry-mixing, wet mixing conjunction, mechanical mixture and combinations thereof.
Molecular sieve can also be impregnated in solid composite and be preferably in solid particle, wherein the amount containing molecular sieve should meet
Effectively it is catalyzed desired conversion reaction.Solid particle may include the molecular sieve and basis material of catalytically effective amount, preferably
It is at least one filler and adhesive, to provide required performance to the solid composite, for example, required catalysis
Dilution agent degree, mechanical strength etc..This basis material is usually porous to a certain extent, and is usually had some non-
The catalytic activity of selectivity can be effective or invalid to desired chemical reaction is promoted with promoting to generate unwanted product
's.This basis material, for example, filler and adhesive, including the substance, metal oxide, viscous for for example synthesizing or naturally occurring
Soil, silica, aluminium oxide, silica-alumina, silica-magnesias, silica-zirconia, silica thorium oxide, oxidation
Silicon-beryllium oxide, silica-titania, silica-alumina thoria, silica-alumina, zirconia and these materials
Mixture.
Solid catalyst composition preferably includes 1~99 weight %, more preferable 5~90 weight %, and more preferable 10~
The molecular sieve of 80 weight %；And 1~99 weight %, more preferable 5~90 weight %, and the base of more preferable 10~80 weight %
Body material.
The preparation of solid catalyst composition containing molecular sieve and basis material such as solid particle is the general of this field
Usually know, therefore, is not discussed in detail here.
Catalyst may further include adhesive, filler or other materials, to provide better catalytic performance, abrasion performance
Property, regenerability and other required performances.Desirably, catalyst is fluidisable at reaction conditions.Catalysis
The partial size that agent should have be 20~3000 μ, it is desirable to 30~200 μ, it more desirable to be 50~150 μ.Catalyst can be with
Receive various processing to reach required physical and chemical properties.This processing includes but is not necessarily confined to, roasting, ball
Mill grind, crushes, milling, being spray-dried, hydro-thermal process, acid are handled, alkali process and combinations thereof.
According to an aspect of the present invention, the linear velocity V in fast fluidized bed reaction zone1, the quasi- line promoted in reaction zone
Speed V2It is V with the linear velocity in riser reaction zone3Relationship are as follows: V3>V2>V1.In fast fluidized bed reaction zone, linear velocity V1
For 1.0~2.0 meter per seconds, the residence time is 4~7 seconds；It is quasi- to be promoted in reaction zone, linear velocity V2For 2.5~5 meter per seconds, stop
Time is 1.5~3.5 seconds；In riser reaction zone, linear velocity V3For 7~12 meter per seconds, the residence time is 0.8~1.4 second.
For be at the temperature of light olefin by oxygenate conversion can be in very wide range, this is depended on,
It is at least partially dependent on, catalyst, the knot of regenerated catalyst portion and reactor assembly and reactor in catalyst mixture
Structure.Although these methods are not limited by temperature, if the temperature by this method control at 200~700 DEG C, desired
It is 250~600 DEG C of temperature, it is most desirable to which 300~500 DEG C of temperature then can achieve best result.Lower temperature
Lower reaction speed is normally resulted in, and the formation speed of desired Light olefin products can significantly slow down.But work as temperature
When degree is higher than 700 DEG C, this method will not generate the Light olefin products of optimised quantity, and form coke and light saturation on a catalyst
The speed of object then becomes too fast.
Light olefin will be formed in very wide pressure limit, although not necessarily generating by optimised quantity, the press packet
It includes but is not limited to, pressure is 0.1kPa~5MPa, and desired pressure is 5kPa~1MPa, and highly desirable pressure is 20kPa
~500kPa.Pressure except above-mentioned pressure limit can also be used and be not excluded in the scope of the present invention.It is lower and compared with
High pressure can apply detrimental effect to selectivity, conversion ratio, coking yield and/or reaction rate；But it still can generate light
Alkene, therefore, these pressure limits are considered as a part of the invention.
Weight space velocity WHSV for oxygenate conversion reaction, it is desirable to sufficiently high to maintain catalyst in reaction condition
Being in down and in the structure and design of reactor can fluidized state.Generally, WHSV is l~5000hr-1, it is desirable to 2
~3000hr-1, more desirably 5~1500hr-1。
Regenerative raw materials gas bag is included but is not necessarily confined to, simple O2、SO3、N2O、NO、NO2、N2O5And its mixture.
Air and with nitrogen or CO2Diluted air is all desired regeneration gas.Can be lowered to can for the concentration of oxygen in air
The level of control, so that the overheat of regenerator or the hot spot of generation drop at least.
In the conversion process of oxygenatedchemicals to alkene, carbonaceous sediment is accumulated for promoting the catalyst of conversion reaction
On.In certain situation, the accumulation of these carbonaceous sediments will lead to the catalytic capability of oxygen compound feedstock to light olefins
Decline.In this case, catalyst loses amount of activated.When catalyst no longer can be by oxygenate conversion at olefin product
When, catalyst is considered losing activity completely.As a nonessential step in oxygenatedchemicals into olefin reaction
Suddenly, partial catalyst is taken out from reactor, and from least part in the partial catalyst taken out in reactor
It is regenerated in regenerating unit.Pass through regeneration, it means that carbonaceous sediment is at least partly to be removed from catalyst.Again
Catalyst after life can be then returned in reactor through cooling or without cooling.It is as desired, for regenerated
The produced quantity of partial catalyst is account for the catalytic amount come out in reactor 0.1~99%.It more desirably is that the produced quantity is
0.2~50% is accounted for, is to account for 0.5~5% highly desirablely.Desirably, catalyst is reproduced carbon deposition quantity and accounts for catalytic amount
The level of 0.01~15 weight %.
Catalyst regeneration temperature should be at 250~750 DEG C, it is desirable at 500~700 DEG C.
Specific embodiment
[embodiment 1]
Using reaction-regenerative device shown in Fig. 1.Fast fluidized bed reaction zone quasi- promotes reaction zone, riser reaction zone
Diameter is respectively 8 meters, 2 meters, 1.2 meters；Burning tank renewing zone, dense bed renewing zone diameter be respectively 4 meters, 6 meters.
The methanol feedstock of 225t/h enters fast fluidized reaction zone through distribution grid, is 480 DEG C, methanol weight in reaction temperature
Amount air speed WHSV is 10h-1Under conditions of, it is contacted with SAPO-34 molecular sieve catalyst, fast fluidized reaction zone exports methanol and turns
Rate is 79.5%, and into after quasi- promotion reaction zone, reaction temperature is 485 DEG C, linear velocity V2For 4.5 meter per seconds, when gas-solid stops
Between be 2 seconds, intend promoted reaction zone methanol conversion be 97%, into after riser reaction zone, reaction temperature be 487 DEG C, line
Speed V3For 9 meter per seconds, the gas-solid residence time is 1 second, and the catalyst of inactivation enters the regeneration of regenerator burning tank from inclined tube to be generated
Area, the regeneration of dense bed renewing zone, regeneration temperature are 670 DEG C, and the carbon deposition quantity of catalyst after regeneration is 0.05wt%.
It is formed, is computed, methanol conversion with online gas chromatographic detection reactor three-level separation equipment exported product gas
It is 99.98%, low-carbon alkene (ethylene+propylene) is selectively 82.07%.
[embodiment 2]
Using reaction-regenerative device shown in Fig. 1.Fast fluidized bed reaction zone quasi- promotes reaction zone, riser reaction zone
Diameter is respectively 8 meters, 5.4 meters, 3 meters；Burning tank renewing zone, dense bed renewing zone diameter be respectively 5 meters, 6 meters.
The methanol feedstock of 225t/h enters fast fluidized reaction zone through distribution grid, is 480 DEG C, methanol weight in reaction temperature
Amount air speed WHSV is 10h-1Under conditions of, it is contacted with SAPO-34 molecular sieve catalyst, fast fluidized reaction zone exports methanol and turns
Rate is 79.4%, and into after quasi- promotion reaction zone, reaction temperature is 485 DEG C, linear velocity V2For 2.5 meter per seconds, when gas-solid stops
Between be 3.5 seconds, intend promoted reaction zone methanol conversion be 98%, into after riser reaction zone, reaction temperature be 489 DEG C,
Linear velocity V3For 7 meter per seconds, the gas-solid residence time is 1.5 seconds, and the catalyst of inactivation enters regenerator burning tank again from inclined tube to be generated
Raw area, the regeneration of dense bed renewing zone, regeneration temperature are 670 DEG C, and the carbon deposition quantity of catalyst after regeneration is 0.05wt%.
It is formed, is computed, methanol conversion with online gas chromatographic detection reactor three-level separation equipment exported product gas
It is 99.99%, low-carbon alkene (ethylene+propylene) is selectively 81.78%.
[embodiment 3]
Using reaction-regenerative device shown in Fig. 1.Fast fluidized bed reaction zone quasi- promotes reaction zone, riser reaction zone
Diameter is respectively 8 meters, 3 meters, 1 meter；Burning tank renewing zone, dense bed renewing zone diameter be respectively 2 meters, 6 meters.
The methanol feedstock of 225t/h enters fast fluidized reaction zone through distribution grid, is 470 DEG C, methanol weight in reaction temperature
Amount air speed WHSV is 12h-1Under conditions of, it is contacted with SAPO-34 molecular sieve catalyst, fast fluidized reaction zone exports methanol and turns
Rate is 78%, and into after quasi- promotion reaction zone, reaction temperature is 482 DEG C, linear velocity V2For 3.5 meter per seconds, gas-solid residence time
It is 2.6 seconds, the methanol conversion for intending promoting reaction zone is 97%, and into after riser reaction zone, reaction temperature is 486 DEG C, line
Speed V3For 12 meter per seconds, the gas-solid residence time is 1 second, and the catalyst of inactivation enters the regeneration of regenerator burning tank from inclined tube to be generated
Area, the regeneration of dense bed renewing zone, regeneration temperature are 670 DEG C, and the carbon deposition quantity of catalyst after regeneration is 0.85wt%.
It is formed, is computed, methanol conversion with online gas chromatographic detection reactor three-level separation equipment exported product gas
It is 99.97%, low-carbon alkene (ethylene+propylene) is selectively 81.56%.
[comparative example 1]
Using the consersion unit (quasi- to promote reaction zone and riser reaction zone) of only fast fluidized bed reaction zone,
Reaction temperature is 480 DEG C, methanol weight air speed WHSV is 10h-1Under conditions of, it is contacted with SAPO-34 molecular sieve catalyst.
It is formed, is computed, methanol conversion with online gas chromatographic detection reactor three-level separation equipment exported product gas
It is 99.6%, low-carbon alkene (ethylene+propylene) is selectively 79.33%.
[comparative example 2]
With [comparative example 1], only fast fluidized bed reaction zone is changed to turbulent fluidized bed reaction zone.
The methanol conversion of reactor outlet is 99.3%, and low-carbon alkene (ethylene+propylene) is selectively 78.24%.
Claims (32)
1. a kind of reaction-regenerative device, including reactor and regenerator；The reactor and the regenerator pass through inclined tube to be generated
It is connected with regenerator sloped tube；It is characterized in that,
The reactor includes:
(a) fast fluidized bed reaction zone；The fast fluidized bed reaction zone has the first end of injection raw material and supplies the first product
The second end flowed out from the fast fluidized bed reaction zone；
(b) intend promoting reaction zone；The quasi- reaction zone that promoted has the first end of the first product of injection and supplies the second product from institute
State the quasi- second end for being promoted and being flowed out in reaction zone；The quasi- promotion reaction zone and the fast fluidized bed reaction zone are in fluid communication
Mode be connected；
(c) riser reaction zone；The riser reaction zone has the first end of the second product of injection and for third product from institute
State the second end flowed out in riser reaction zone；The side of the riser reaction zone and the quasi- promotion reaction zone in fluid communication
Formula is connected.
2. reaction-regenerative device according to claim 1, which is characterized in that the fast fluidized bed reaction zone, described quasi-
Promoting reaction zone and the riser reaction zone has the central axis being overlapped.
3. reaction-regenerative device according to claim 1, which is characterized in that the reactor further comprises:
(d) reactor dense bed；The quasi- promotion reaction zone is configured in the reactor dense bed.
4. reaction-regenerative device according to claim 3, which is characterized in that the reactor dense bed passes through reactor
Circulation inclined tube is connected with the fast fluidized bed reaction zone.
5. reaction-regenerative device according to claim 3, which is characterized in that reactor dense bed lower part is configured with
Distribution rings, the distribution rings are around configuration in the quasi- promotion reaction zone periphery.
6. reaction-regenerative device according to claim 3, which is characterized in that the reactor further comprises:
(e) reactor settling section；The riser reaction zone is configured in the reactor settling section.
7. reaction-regenerative device according to claim 6, which is characterized in that the reactor settling section and reactor are close
The mode of phase bed in fluid communication is connected.
8. reaction-regenerative device according to claim 6, which is characterized in that the reactor further comprises:
(f) reactor level-one separation equipment；The reactor level-one separation equipment is configured at the second of the riser reaction zone
End.
9. reaction-regenerative device according to claim 8, which is characterized in that the reactor level-one separation equipment is rotation
Wind separator.
10. reaction-regenerative device according to claim 8, which is characterized in that the reactor further comprises:
(g) reactor the second-order separation equipment；The reactor the second-order separation device configuration is in reactor settling section top.
11. reaction-regenerative device according to claim 10, which is characterized in that the reactor the second-order separation equipment is
Cyclone separator.
12. reaction-regenerative device according to claim 10, which is characterized in that the reactor further comprises:
(h) reactor three-level separation equipment；The reactor three-level separation equipment is configured at outside reactor settling section.
13. reaction-regenerative device according to claim 12, which is characterized in that in the reactor three-level separation equipment
Configured with negative pressure discharging type cyclone separator；The fluid inlet and reactor the second-order separation of the negative pressure discharging type cyclone separator
Equipment outlet gas line is not attached to.
14. reaction-regenerative device according to claim 12, which is characterized in that under the reactor three-level separation equipment
Portion is dense fluidized bed, and density of solid is greater than 400kg/m3；Dense fluidized bed bottom is situated between configured with reactor fluidisation
Matter suction line.
15. reaction-regenerative device according to claim 12, which is characterized in that the reactor three-level separation equipment is matched
It is equipped with product gas outlet and reactor catalyst feed opening；The reactor catalyst feed opening and fast fluidized bed reaction zone phase
Even.
16. reaction-regenerative device according to claim 12, which is characterized in that the reactor further comprises:
(i) reactor external warmer；It is settled at the top of the reactor external warmer configured with the first gas line of return and reactor
Duan Xianglian；Reactor external warmer bottom is connected configured with the first inclined tube with fast fluidized bed reaction zone；The reactor
External warmer is connected configured with the second inclined tube with reactor dense bed.
17. reaction-regenerative device according to claim 16, which is characterized in that the reactor further comprises:
(j) reactor stripper；The reactor stripper is connected with the mode of reactor dense bed in fluid communication；It is described anti-
Device stripper is answered to be connected with inclined tube to be generated.
18. reaction-regenerative device according to claim 1, which is characterized in that the fast fluidized bed reaction zone with it is described
The quasi- reaction zone that promoted is connected place using conical transition；In place of the quasi- promotion reaction zone is connected with the riser reaction zone
Using conical transition.
19. reaction-regenerative device according to claim 1, which is characterized in that the fast fluidized bed reaction zone and regeneration
Inclined tube is connected.
20. reaction-regenerative device according to claim 1, which is characterized in that the fast fluidized bed reaction zone, described
Intend promotion reaction zone, the diameter ratio of the riser reaction zone is (1.5~5): 1:(0.2~0.7).
21. reaction-regenerative device according to claim 1, which is characterized in that the regenerator includes:
(1) burning tank renewing zone；The burning tank renewing zone has the first end of injection regenerative raw materials gas and supplies the first reproduction
The second end that object is flowed out from the burning tank renewing zone；
(2) dense bed renewing zone；The dense bed renewing zone has the first end of the first regeneration product of injection and for the second regeneration
The second end that product is flowed out from the dense bed renewing zone；The dense bed renewing zone and the burning tank renewing zone are with fluid
The mode communicated is connected.
22. reaction-regenerative device according to claim 21, which is characterized in that the regenerator further comprises:
(3) regenerator settling section；The regenerator settling section is connected with the mode of the dense bed renewing zone in fluid communication；
(4) regenerator level-one separation equipment and the second-order separation equipment；The regenerator level-one separation equipment and the second-order separation equipment
It is configured in the regenerator settling section；
(5) external catalyst cooler for regenerator；It is settled at the top of the external catalyst cooler for regenerator configured with the second gas line of return and regenerator
Duan Xianglian；The external catalyst cooler for regenerator bottom is connected configured with third inclined tube with burning tank renewing zone；It is taken outside the regenerator
Hot device is connected configured with the 4th inclined tube with dense bed renewing zone；
(6) degassing tank；It is connected configured with the third gas line of return with regenerator settling section at the top of the degassing tank；The degassing tank
Bottom is connected with regenerator sloped tube；The degassing tank is connected configured with the 5th inclined tube with dense bed renewing zone.
23. reaction-regenerative device according to claim 22, which is characterized in that the regenerator level-one separation equipment and
The second-order separation equipment is cyclone separator, and the regenerator level-one separation equipment and the second-order separation equipment are with regenerator settling section
Configuration substantially symmetrical about its central axis.
24. reaction-regenerative device according to claim 22, which is characterized in that the regenerator further comprises:
(7) regenerator three-level separation equipment；The regenerator three-level separation equipment is configured at outside regenerator settling section；It is described again
Raw device three-level separation equipment is configured with regenerated flue gas outlet and regenerator catalyst feed opening；The regenerator catalyst feed opening
It is connected with burning tank renewing zone.
25. reaction-regenerative device according to claim 23, which is characterized in that in the regenerator three-level separation equipment
Configured with negative pressure discharging type cyclone separator；The fluid inlet and regenerator the second-order separation of the negative pressure discharging type cyclone separator
Equipment outlet gas line is not attached to.
26. reaction-regenerative device according to claim 23, which is characterized in that under the regenerator three-level separation equipment
Portion is dense fluidized bed, and density of solid is greater than 400kg/m3；Dense fluidized bed bottom is situated between configured with regenerator fluidisation
Matter suction line.
27. reaction-regenerative device according to claim 22, which is characterized in that the burning tank renewing zone and it is to be generated tiltedly
Pipe is connected.
28. reaction-regenerative device according to claim 22, which is characterized in that burning tank renewing zone exterior arrangement
There is regenerator to recycle inclined tube, the regenerator circulation inclined tube is connected with the dense bed renewing zone.
29. reaction-regenerative device according to claim 22, which is characterized in that the burning tank renewing zone with it is described close
Phase bed renewing zone is connected place using conical transition.
30. reaction-regenerative device according to claim 22, which is characterized in that the burning tank renewing zone with it is described close
The diameter ratio of phase bed renewing zone is (0.3~0.95): 1.
31. conversion reaction of any reaction-regenerative device of claim 1-30 for oxygenatedchemicals to alkene.
32. purposes of the reaction-regenerative device according to claim 31 for the conversion reaction of oxygenatedchemicals to alkene,
It is characterized in that, in the fast fluidized bed reaction zone, linear velocity V1For 1.0~2.0 meter per seconds, the residence time is 4~7 seconds；Institute
It states in quasi- promotion reaction zone, linear velocity V2For 2.5~5 meter per seconds, the residence time is 1.5~3.5 seconds；The promotion tube reaction
In area, linear velocity V3For 7~12 meter per seconds, the residence time is 0.8~1.4 second.
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| CN113842842A (en) * | 2020-06-28 | 2021-12-28 | 中国石油化工股份有限公司 | Device and method for preparing olefin by catalytic conversion of methanol |
| CN113842842B (en) * | 2020-06-28 | 2022-08-30 | 中国石油化工股份有限公司 | Device and method for preparing olefin by catalytic conversion of methanol |
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| CN109422617B (en) | 2023-09-29 |
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