CN106914191A - The hydrocarbons fluidised-bed reaction method of methyl alcohol system - Google Patents
The hydrocarbons fluidised-bed reaction method of methyl alcohol system Download PDFInfo
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- CN106914191A CN106914191A CN201710185207.4A CN201710185207A CN106914191A CN 106914191 A CN106914191 A CN 106914191A CN 201710185207 A CN201710185207 A CN 201710185207A CN 106914191 A CN106914191 A CN 106914191A
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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
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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
- B01J8/1836—Heating and cooling the reactor
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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
- B01J8/1872—Details of the fluidised bed reactor
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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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- 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
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Abstract
The present invention relates to gas-solid fluidized bed reaction technology field, and in particular to a kind of hydrocarbons fluidised-bed reaction method of methyl alcohol system, the fluidized bed reaction zone (FB1) and the post-reaction treatment area on top of bottom are provided with；The post-reaction treatment area is provided with housing (2), reaction gas accumulation regions (15), reaction terminating controller (3) and gas solid separation area；Using conical fluidized bed reactor, by setting the Quick stop that product gas are quickly drawn, gas-solid pre-separation and the realization of chilling link are reacted between fluidized bed reaction zone and gas-solid Disengagement zone, reduce side reaction and reduce catalyst attrition, while realizing the control to flowing out catalyst temperature.
Description
Technical field
The present invention relates to gas-solid fluidized bed reaction technology field, and in particular to a kind of hydrocarbons fluidised-bed reaction side of methyl alcohol system
Method, is particularly suited for gas-solid fluidized bed methanol-to-olefins and aromatic hydrocarbons.
Background technology
Methyl alcohol producing olefinic hydrocarbons or aromatic hydrocarbons etc. are the important process technologies of Coal Chemical Industry, have obtained the great attention of various countries.A lot
Methyl alcohol producing olefinic hydrocarbons or aromatic hydrocarbons reaction use gas-solid fluidized bed or recirculating fluidized bed reaction method.
Current methyl alcohol hydrocarbon products technology, such as DMTO, SMTO, FMTP, FMTA, it is anti-using fluid bed or recirculating fluidized bed
Technology is answered, the catalyst for using is microspheric, about 50~70 microns of average diameter.Existing fluid bed the reaction of methanol conversion technology mesh
Preceding many reference FCC technologies.But methyl alcohol is converted has many differences with the condition of FCC, reaction is exothermic process, and catalyst price is held high
Expensive, catalyst is the pith of running cost.By taking 1,800,000 tons of devices of methyl alcohol processing capacity as an example, correspondence methyl alcohol charging per ton
Even if reducing by 0.1 kilogram of catalyst consumption amount, just it is roughly equivalent to reduce the operating cost of about 36,000,000 yuan/year.
What existing methanol-to-olefins or aromatic hydrocarbons technology course of reaction were used has fluid bed and the class of recirculating fluidized bed two.Recycle stream
Change the burning tank regeneration techniques that bed has used for reference FCC technologies.Recirculating fluidized bed easily can set gas-solid point in reactor end
From timely terminating reaction, the control to reacting is realized.But because methyl alcohol reaction green coke is far below FCC, between reactor and regenerator
Catalyst internal circulating load it is very low, 1/1/10th to 20 of agent alcohol than only correspondence FCC oil ratios.Using ciculation fluidized
During bed, in order that reaching density of catalyst and reserve or the air speed that reaction needs in reactor, catalyst can only be made in reactor
Itself repetitive cycling, and internal circulating load is far longer than internal circulating load original between reactor and regenerator；Necessarily increase the broken of catalyst
Broken and operation energy consumption.
The advantage of existing methyl alcohol conversion fluidized-bed reaction technology is that gas and catalyst flowing velocity are low；Course of reaction itself
Catalyst is only fluidized bed state, in addition to dilute a small amount of catalyst of carrying of gas, in reactor following for catalyst does not occur
Ring is conveyed.Fluidized-bed reaction process catalyst it is broken far fewer than recirculating fluidized bed.Existing fluidized-bed reactor is revolved using two-stage
Wind separator carries out gas solid separation, but because fluid catalyst interface is unintelligible, existing fluidized-bed reaction process is only by weight
Power sedimentation reduces the catalyst content of cyclone inlet gas, distant between reaction zone and gas-solid separator entrance, instead
Product gas are answered still to stop longer time after reaction is left in preferable fluid bed in catalyst environment, the real reaction time
It is uncertain, cause to react actual termination and control is difficult, cause side reaction to increase；In addition only by natural gravity sedimentation gas
Catalyst content is more, and catalyst content is general still in 5~10kg/m into the product gas of cyclone separator3。
In order to reduce catalyst consumption, what is continued to use in prior art is that the method raising for being further added by catalyst reclaimer is urged
Agent recovering effect.Such as DMTO reactors increased outside " three rotations " and " washing water deduster " outside reactor.Investment and
Energy consumption all increases more.
The content of the invention
Carried less it is an object of the invention to provide a kind of catalyst dilute phase, energy Quick stop reacts, the side reaction time is contracted
It is short, and reduce the hydrocarbons fluidised-bed reaction method of the methyl alcohol system of catalyst breakage and catalyst emission amount.
The hydrocarbons fluidised-bed reaction method of methyl alcohol system of the invention, after being provided with the reaction on the fluidized bed reaction zone of bottom and top
Treatment region；The post-reaction treatment area is provided with housing, reaction gas accumulation regions, reaction terminating controller and gas solid separation area；It is described
Fluidized bed reaction zone refers to use conical fluidized bed reactor, the fluidized bed reaction zone of catalyst taper formed therein that, its stream
The gas flow rate changed in bed reaction zone is less than flow speed value of the turbulent fluidized bed to the transition point of recirculating fluidized bed；
The fluidized bed reaction zone uses conical fluidized bed reactor, catalyst that cone is formed in conical fluidized bed reactor
Shape fluid bed, conical fluidized bed reactor flows to upward area and gradually expands along reaction raw materials, and the corresponding gas that reduces leaves cone
The speed of shape fluid bed, reduces the catalyst carrying amount of gas；The fluidized bed reaction zone top is in conical fluidized bed reactor
With upward area diminishing taper reaction gas accumulation regions are set in housing, reacting gas is departed from fluidized-bed reaction rapidly
Area；Reaction gas accumulation regions outlet set delivery pipe, delivery pipe outlet set reaction terminating controller, make reacting gas quickly with
Catalyst departs from and lowers the temperature, and realizes reaction terminating；
Gas solid separation area in housing sets two-stage series connection cyclone separator (two-stage series connection whirlwind in parallel more than two
Separator, i.e. first order cyclone separator gas vent are directly connected with second level cyclone separator gas access), every grade by simultaneously
The cyclone separator composition of row, two-stage series connection cyclone separator is provided with more than two, and every group is arranged in parallel；
L-type catalyst overflow standpipe is set outside housing and conical fluidized bed reactor, makes reaction terminating controller and two
The catalyst that level cyclones in series is isolated returns to fluidized bed reaction zone；(i.e. catalyst overflows catalyst overflow standpipe entrance
Stream standpipe upper end) catalyst in post-reaction treatment area to be drawn, outlet (i.e. catalyst overflow lower riser end) introduces catalyst
Fluidized bed reaction zone, catalyst overflow standpipe entrance is more than the cone of reaction gas accumulation regions；Conical fluidized bed reactor is provided with
Regenerated catalyst inlet and reclaimable catalyst are exported.
The hydrocarbons fluidised-bed reaction method of above-mentioned methyl alcohol system, further, it is pre- that the reaction terminating controller is provided with gas-solid
Separator；Gas-solid preseparator is provided with circumferential cyclone pipe, the gas of central tube, taper connection pipe and taper connection pipe respective amount
Body outlet and shell body, the central tube have the semi-cone angle that upward area gradually expands, and the taper connection pipe is two
More than, circumferentially, cross section is rectangle.During specific implementation, reaction terminating controller is also provided with reaction gas chilling area,
The quenching medium entrance in the reaction gas chilling area is arranged on gas outlet tube.
The hydrocarbons fluidised-bed reaction method of above-mentioned methyl alcohol system, further, between the central tube and cyclone pipe outlet
Flue is vertically arranged, gas flows out rear steering from cyclone pipe, and the annular space between flue and central tube is flowed upwards out.
The hydrocarbons fluidised-bed reaction method of above-mentioned methyl alcohol system, further, reaction terminating controller and two-stage series connection whirlwind
Air shooter is set between separator, makes the first order cyclonic separation of reaction terminating controller and two-stage series connection cyclone separator
Device gas inlet pipe is directly connected to, and the product gas from reaction terminating controller are directly entered two-stage series connection cyclone separator；Instead
The gas that should terminate outside controller enters cyclone separator through gas fairlead.During specific implementation, fairlead may be provided in and enter gas
In body delivery pipe, may be alternatively provided in first order cyclone inlet pipe or second level cyclone separator gas inlet pipe.
The hydrocarbons fluidised-bed reaction method of above-mentioned methyl alcohol system, further, sets on the pipeline of the reclaimable catalyst outlet
The catalyst controller that catalyst takes heat and recycling catalyst stripping one is equipped with, is realized to reaction temperature and circulation catalysis to be generated
The control that agent gas is carried, recycling catalyst stripper and the upper and lower arranged in series of catalyst heat collector；Catalyst heat collector water
Or methanol feedstock is to take thermal medium, saturated vapor, steam trap is pressed to be taken with catalyst in being produced when taking thermal medium using water
Hot device is connected as one.
The hydrocarbons fluidised-bed reaction method of above-mentioned methyl alcohol system, further, the reaction raw materials are at fluidized bed reaction zone bottom
Portion enters conical fluidized bed from reaction raw materials feed distributor, and the gas flow rate of conical fluidized bed is less than fast fluidized bed or circulation
The initial value of fluid bed, the gas flow rate of conical fluidized bed is controlled by no more than 1.2m/s；After conical fluidized bed completes reaction
Reaction gas accumulation regions and reaction terminating controller are upwardly into, direct chilling after the catalyst that most of gas is carried is isolated；
Then gas medium enters the two stage cyclone separator of series connection and continues separating catalyst, and final product gas is from reaction gas outlet
Outflow.During specific implementation, described fast fluidized bed or the initial value of recirculating fluidized bed are determined by catalyst property, this area skill
Art personnel can calculate, and understand, fast fluidized bed, recirculating fluidized bed on fluidization technology be not only flow velocity not
Together, but entirely different fluidization pattern.
The hydrocarbons fluidised-bed reaction method of above-mentioned methyl alcohol system, further, the gas flow rate of the conical fluidized bed is by stream
The average apparent flow velocity for changing the calculating of bed cross section is 0.6~1.0m/s, and conical fluidized bed reactor outlet gas flow velocity is less than
0.85m/s。
The hydrocarbons fluidised-bed reaction method of above-mentioned methyl alcohol system, further, conical fluidized bed reactor semi-cone angle be 0~
30°。
This method can be used to the reaction of methanol conversion and catalyst regeneration, and charging is air when being regenerated for catalyst,
Reaction gas is flue gas.
Invention effect：
Speed reduction when fluidized bed reaction zone makes gas leave conical fluidized bed, reduces catalyst carrying amount, is conducive to anti-
Should terminate and gas solid separation；The reaction of methanol conversion time normally only needs 2 seconds or so, due to methyl alcohol hydrocarbon reaction fluidized bed gas
Catalyst is carried, normal flow fluidized bed reactor cannot accurately control catalyst interface, by being catalyzed by certain space and time
Agent gravitational settling realizes catalyst initial gross separation, and reacting gas is still contacted with catalyst in a long time, generally reaches 20
More than second, period continues to react, it is impossible to which the termination of control reaction, side reaction ratio height is common problem.The present invention is adopted
The method that flashing reactor accumulation regions and reaction terminating controller are set in conical fluidized bed reactor is taken, both can be significantly
Shorten gas and leave the time after theoretical fluid bed charge level, but the quick catalyst that carries out is separated and gas chilled, makes reaction quick
Terminate, side reaction can be significantly reduced；Chilling also reduces chilling energy consumption after catalyst separation；Catalyst is reduced simultaneously to damage
Consumption.
Brief description of the drawings
The hydrocarbons fluidised-bed apparatus structure schematic diagram of reaction method implementation method one of Fig. 1 methyl alcohol systems of the invention；
Fig. 2 is reaction terminating controller concrete structure schematic diagram in Fig. 1；
Fig. 3 be Fig. 2 in A-A to cross-sectional view；
Reaction terminating controller another kind pattern concrete structure schematic diagram in Fig. 4 Fig. 1；
Reaction terminating controller another kind pattern concrete structure schematic diagram in Fig. 5 Fig. 1；
The hydrocarbons fluidised-bed reaction method implementation method two devices structural representation of Fig. 6 methyl alcohol systems of the invention.
Explanation is numbered in figure：
1 conical fluidized bed reactor, 11 reaction raw materials entrances, 12 reaction raw materials feed distributors, 13 reclaimable catalysts go out
Mouthful, 14 regenerated catalyst inlets, 15 reaction gas accumulation regions, 16 catalyst overflow standpipes, 18 inside heat removing pipes, 2 housings, 21 conveyings
Pipe, 22 reacting gas converge room, 23 reaction gas outlets, 3 reaction terminating controllers, 31 central tubes, 32 taper connection pipes, 33 rotations
Flow tube, the outlet of 34 flues, 35 gas outlet tubes, 36 air shooters, 37 shell bodies, 38 flues, 39 quenching medium entrances,
41 first order cyclone separator gas inlet pipes, 42 first order cyclone separator gas outlet tubes, 43 first order cyclone separators,
44 gas fairleads, 51 second level cyclone separator gas inlet pipes, 52 second level cyclone separator gas outlet tubes, 53 second
Level cyclone separator, 61 catalyst heat collectors, 62 recycling catalyst strippers, 63 steam traps, 64A first is stripped and fluidized
Media dispenser, the strippings of 64B second and fluidizing agent distributor, 65 catalyst circulation pipes, S steam, C1 regenerated catalysts, C are treated
Raw catalyst, Y reaction raw materials, PA conical fluidized bed reactor outlet logistics, P reactor product gases, L quenching mediums, γ tapers
Fluidized-bed reactor semi-cone angle, the lower plate angles of α 1, the upper plate arc angles of α 3, the lower plate arc angles of α 4, the foreboard angles of β 1, the back plates of β 2
Angle, Θ central tube semi-cone angles, R1 cyclone pipes inner side radius of curvature, R2 cyclone pipe lateral curvature radiuses, FB1 fluidized-bed reactions
Area, the catalyst zone that FB2 is separate.
Specific embodiment
The present invention is further detailed explanation with reference to the accompanying drawings and detailed description, it is intended to helps reader to understand
The features of the present invention and essence, but the drawings and specific embodiments content be not intended to limit it is of the invention can practical range.
Implementation method one：
As shown in figure 1, the hydrocarbons fluidised-bed reaction method of methyl alcohol system of the invention, is provided with the fluidized bed reaction zone FB1 of bottom
With the post-reaction treatment area on top；Post-reaction treatment area is provided with housing 2, reaction gas accumulation regions 15, reaction terminating controller 3 and gas
Gu Disengagement zone；
Fluidized bed reaction zone FB1 uses conical fluidized bed reactor 1, catalyst to be formed in conical fluidized bed reactor 1
Conical fluidized bed, conical fluidized bed reactor 1 flows to upward area and gradually expands along reaction raw materials Y, conical fluidized bed reactor 1
Semi-cone angle γ is 0~30 °；It is corresponding to reduce the speed that gas leaves fluid bed, reduce catalyst carrying amount；Fluidized bed reaction zone
FB1 tops set the upward diminishing taper reaction gas accumulation regions 15 of area in conical fluidized bed reactor 1 and housing 2,
Reacting gas is set to depart from fluidized bed reaction zone FB1 rapidly；In reaction gas accumulation regions 15, outlet sets delivery pipe 21, and delivery pipe 21 goes out
Mouth sets reaction terminating controller 3, reacting gas is quickly departed from catalyst and is lowered the temperature, and realizes reaction terminating；
Gas solid separation area in housing 2 sets two-stage series connection cyclone separator in parallel, and every grade by whirlwind arranged side by side point
From device composition, two-stage series connection cyclone separator is provided with more than two, and every group is arranged in parallel；During specific implementation, two-stage series connection whirlwind
Separator is provided with first order cyclone separator 43 and second level cyclone separator 53, and first order cyclone separator 43 is provided with the first order
Cyclone inlet 41 and first order cyclone separator gas vent 42, second level cyclone separator 53 is provided with second level whirlwind
Separator inlet 51 and second level cyclone separator gas vent 52, first order cyclone separator gas vent 42 and the second level are revolved
Wind separator inlet 51 is directly connected to；Second level cyclone separator gas vent 52 converge with reacting gas successively upwards room 22,
Reaction gas outlet 23 is connected；
In housing 2 and the outer setting L-type catalyst overflow standpipe 16 of conical fluidized bed reactor 1, make reaction terminating controller 3
Fluidized bed reaction zone FB1 is returned with the catalyst that two-stage series connection cyclone separator is isolated；The entrance of catalyst overflow standpipe 16 is
The catalyst in post-reaction treatment area is drawn in catalyst overflow standpipe upper end, and outlet is catalyst overflow lower riser end by catalyst
Fluidized bed reaction zone FB1 is introduced, the entrance of agent overflow standpipe 16 is more than the cone of reaction gas accumulation regions 15；Conical fluidized bed reacts
Device 1 is provided with regenerated catalyst inlet 14 and reclaimable catalyst outlet 13.
Air shooter 36 is set between reaction terminating controller 3 and two-stage series connection cyclone separator, makes reaction terminating
The first order cyclone separator gas inlet pipe 41 of controller 3 and two-stage series connection cyclone separator is directly connected to, and carrys out autoreaction end
Only the product gas of controller 3 are directly entered two-stage series connection cyclone separator；Gas outside reaction terminating controller is drawn through gas
Pipe 44 enters cyclone separator；During specific implementation, fairlead 44 may be provided in on air shooter 36, may be alternatively provided at the first order
On cyclone inlet pipe 41 or second level cyclone separator gas inlet pipe 51, in present embodiment, fairlead 44 is located at
On first order cyclone inlet pipe 4.
During specific implementation, reaction terminating controller 3 can using the structural shape shown in Fig. 2-3, by gas-solid preseparator and
Reaction gas chilling district's groups into；As shown in Fig. 2 gas-solid preseparator is provided with central tube 31, taper connection pipe 32 and taper connection pipe
(circumference here, i.e. cyclone pipe 33 are along the circumferencial direction cloth of taper connection pipe 32 to the circumferential cyclone pipe 33 of 32 respective amounts
Put), gas outlet tube 35 and shell body 37, there is central tube 31 semi-cone angle Θ, Θ that upward area gradually expands to be less than 15 °；
Taper connection pipe 32 is two or more, and circumferentially, cross section is rectangle；Taper connection pipe 32 has upper and lower plates and front and rear panel,
Upper and lower plates and front and rear panel can use flat board or arc plate structure, and in present embodiment, upper and lower plates and front and rear panel are using flat
Plate, such as Fig. 2, lower plate angle [alpha] 1 are less than 45 °, and such as Fig. 3, foreboard angle beta 1 and back plate angle beta 2 are less than 30 °；Cyclone pipe inner side curvature
Radius is R1, and cyclone pipe lateral curvature radius is R2；Flue 38 is vertically arranged between central tube 31 and cyclone pipe 33 are exported,
Flue 38 is with diameter greater than the diameter of gas outlet tube 35；Gas is that conical fluidized bed reactor outlet logistics PA flows from cyclone pipe 33
Go out rear steering, the annular space between flue 38 and central tube 31 is flowed upwards out, collect through flue outlet 34, gas outlet tube 35
Into reactor product gas P.During specific implementation, the cyclone pipe gas access flow velocity of gas-solid preseparator is set by 5~10m/s (meter per second)
Meter, outlet gas velocity is designed by 6~12m/s；First order cyclone separator gas access flow velocity is designed by 12~16m/s, the
Secondary cyclone gas access flow velocity is designed by 18~25m/s, and general professional and technical personnel has designed capacity.
During specific implementation, reaction terminating controller 3 also can be using the structural shape shown in Fig. 4, as shown in figure 4, gas-solid is pre-
Separator is provided with the circumferential cyclone pipe 33, gas vent of central tube 31, taper connection pipe 32 and the respective amount of taper connection pipe 32
Pipe 35 and shell body 37, the upward area of central tube 31 gradually expand；The cross section of taper connection pipe 32 is rectangle, with upper and lower plates and
Front and rear panel, in present embodiment, upper and lower plates use arc plate, front and rear panel to use flat board, upper plate arc angle α 3 and lower plate circular arc
Angle [alpha] 4 is less than 90 °；The quenching medium entrance 39 in reaction gas chilling area is arranged on gas outlet tube 35, and quenching medium L is from urgency
Cold medium entrance 39 is introduced.
During specific implementation, reaction terminating controller 3 can also only set gas-solid preseparator using the structural shape shown in Fig. 5；
As shown in figure 5, gas-solid preseparator is provided with the circumference of central tube 31, taper connection pipe 32 and the respective amount of taper connection pipe 32
Cyclone pipe 33, gas outlet tube 35 and shell body 37, the upward area of central tube 31 gradually expand；In central tube 31 and cyclone pipe 33
Flue 38 is vertically arranged between outlet, the diameter of flue 38 is equal to the diameter of gas outlet tube 35；Gas is anti-conical fluidized bed
Device outlet streams PA is answered to flow out rear steering from cyclone pipe 33, the annular space between flue 38 and central tube 31 is flowed upwards out, through gas
The outlet 34, gas outlet tube 35 of body pipe accumulates reactor product gas P.
In present embodiment, reaction raw materials feed distributor 12 is arranged on the bottom of conical fluidized bed reactor 1；Regeneration catalyzing
Agent C1 introduces conical fluidized bed reactor 1 from regenerated catalyst inlet 14, and reclaimable catalyst C draws from reclaimable catalyst outlet 13
Go out；Reaction raw materials Y enters in fluidized bed reaction zone FB1 bottoms autoreaction feed(raw material)inlet 11, reacted feedstock distributor 12
Into conical fluidized bed, with catalyst haptoreaction, the gas flow rate of conical fluidized bed is less than fast fluidized bed or ciculation fluidized
The initial value of bed, during specific implementation, the gas flow rate of conical fluidized bed is by the average apparent flow velocity that fluid bed cross section calculates
0.6~1.0m/s, conical fluidized bed reactor outlet gas flow velocity is less than 0.85m/s；Conical fluidized bed complete reaction after to
Upper entrance reaction gas accumulation regions 15 and reaction terminating controller 3, isolate direct chilling after the catalyst that most of gas is carried；
Then gas enters two-stage series connection cyclone separator continuation separating catalyst, and final product gas flows from reaction gas outlet 23
Go out.
The specific implementation process of present embodiment is：
The regenerated catalyst C1 for reaching requirement enters the fluid bed of conical fluidized bed reactor 1 from regenerated catalyst inlet 14
Reaction zone FB1, the reaction raw materials Y (i.e. methyl alcohol) after heat exchange is equal by reaction raw materials feed distributor 12 from reaction raw materials entrance 11
In even entrance fluidized bed reaction zone FB1, make the catalyst fluidization in it and reacted；Fluidized bed reaction zone FB1 is routinely
Turbulent fluidized bed conditional operation, gas flow rate will be less than the transformation flow velocity of fast fluidized bed or recirculating fluidized bed；After completing reaction,
Reacting gas PA is that conical fluidized bed reactor outlet logistics is directly entered reaction gas accumulation regions 15 and delivery pipe 21, in delivery pipe
21 outlets enter the central tube 31 of reaction terminating controller 3, and cyclone pipe 33 is entered through gas connection conduit taper connection pipe 32,
In cyclone pipe 33 it is rotated after enter shell body 37, catalyst under gravitational and centrifugal forces, along the inwall of shell body 37 to
In the catalyst zone FB2 of the lower separation for flowing into the top of reaction gas accumulation regions 15, gas is from gas outlet tube 35 or through flue 38
And the annular space between central tube 31 is that flue outlet 34 is flowed out, quenching medium enters from quenching medium entrance 39, makes reacting gas
Lower the temperature further terminating reaction, flowed out through the gas after over-quenching from housing 2 from flue outlet 34 or gas outlet tube 35
Space or be directly connected with first order cyclone separator gas inlet pipe 41 through air shooter 36, into first order whirlwind point
From device 43, most converge room 22 from reaction gas outlet pipe 23 through second level cyclone separator gas outlet tube 52, reacting gas afterwards
Outflow, the catalyst that two-stage series connection cyclone separator is reclaimed enters the catalyst zone FB2 of the separation of the top of reaction gas accumulation regions 15
Interior, catalyst returns to fluidized bed reaction zone FB1 through catalyst overflow standpipe 16, and reacted catalyst is exported from reclaimable catalyst
13 send out.
Implementation method two：
As shown in fig. 6, the hydrocarbons fluidised-bed reaction method of methyl alcohol system of the invention, the fluidized bed reaction zone of bottom and upper is provided with
The post-reaction treatment area in portion；Post-reaction treatment area is provided with housing, reaction gas accumulation regions, reaction terminating controller 3 and gas solid separation
Area；
The catalyst that catalyst takes heat and recycling catalyst stripping one is provided with the pipeline of reclaimable catalyst outlet
Controller, recycling catalyst stripper 62 and catalyst heat collector arranged in series about 61；Catalyst heat collector 61 water or first
To take thermal medium, present embodiment takes thermal medium to raw polyol using water, presses saturated vapor in generation, steam trap 63 with urge
Agent heat collector 61 is connected as one；
Inside heat removing pipe 18 is provided with fluidized bed reaction zone, the first stripping and fluidisation are additionally provided with catalyst controller
The strippings of media dispenser 64A and second and fluidizing agent distributor 64B, steam S are stripped and fluidizing agent distributor 64A from first
Catalyst stripping is carried out into recycling catalyst stripper 62, thermal medium water from the second stripping and fluidizing agent distributor 64B is taken
Realize taking heat into catalyst heat collector 61；Reclaimable catalyst C after taking heat and stripping sends out along catalyst circulation pipe 65；
Present embodiment other parts structure is with implementation method one.
The specific implementation process of present embodiment is：
The regenerated catalyst for reaching requirement enters fluidized bed reaction zone from regenerated catalyst inlet 14, and the methyl alcohol after heat exchange is anti-
Answer the reacted feedstock distributors of raw material Y to uniformly enter in fluidized bed reaction zone, make the catalyst fluidization in it and carry out
Reaction；Inside heat removing pipe 18 takes heat to fluidized bed reaction zone, controls the extent of reaction；After completing reaction, conical fluidized bed reactor
Outlet streams are directly entered reaction gas accumulation regions and delivery pipe 21, enter in reaction terminating controller 3 in the outlet of delivery pipe 21, and
Into cyclone pipe, gas-solid pre-separation is carried out, gas flows out from gas outlet tube 35, terminating reaction flows out from gas outlet tube 35
Gas be directly entered first order cyclone separator 43, second level cyclone separator 53 from air shooter 36 and realize two stage cyclone
Separate, reactor product gas P flows out from reaction gas outlet pipe, the catalyst that two-stage series connection cyclone separator is reclaimed is then through catalysis
Agent overflow standpipe 16 returns to fluidized bed reaction zone, and reacted catalyst takes heat into recycling catalyst stripper 62 and catalyst
Device 61, the reclaimable catalyst C after taking heat and stripping sends out along catalyst circulation pipe 65.
Embodiment：
Methanol to olefins reaction.Methyl alcohol feeds 1,800,000 tons/year, and product is ethene and propylene.
Reaction condition parameter：
Reaction time, 2.5 seconds, 495 DEG C of reaction temperature, reaction pressure 0.13MPaG, conical fluidized bed gas superficial flow velocity
0.8 meter per second, the gas residence time of conical fluidized bed layer to cyclone inlet center is 4 seconds, 80 tons of catalyst output/small
When, the catalyst bed layer height of conical fluidized bed is located at more than reaction raw materials feed distributor 2 meters；Conical fluidized bed reactor
Cone angle is 12 °, and in 4 meters of reaction raw materials feed distributor level above, the cone lower edge of reaction gas accumulation regions is entered away from reaction raw materials
4 meters of distributor of material, the meter per second of delivery pipe flow velocity 12；15 ° of the central tube cone angle Θ of reaction terminating controller, taper connection tube inlet
The meter per second of gas flow rate 5,9 meter per seconds of outlet；Air shooter, gas are set between reaction terminating controller and first order cyclone separator
The meter per second of body delivery pipe gas flow rate 15；Two-stage series connection cyclone separator, first order cyclone separator gas access flow velocity 15 are set
Meter per second, the meter per second of second level cyclone separator gas access flow velocity 21；First order cyclone separator and second level cyclone separator
It is respectively provided with 12 groups.
Claims (9)
1. a kind of methyl alcohol hydrocarbon fluidized bed reaction method, it is characterised in that：
It is provided with the fluidized bed reaction zone (FB1) and the post-reaction treatment area on top of bottom；The post-reaction treatment area is provided with housing
(2), reaction gas accumulation regions (15), reaction terminating controller (3) and gas solid separation area；
, using conical fluidized bed reactor (1), catalyst is in conical fluidized bed reactor (1) for the fluidized bed reaction zone (FB1)
Interior formation conical fluidized bed, conical fluidized bed reactor (1) flows to upward area and gradually expands along reaction raw materials (Y)；
Fluidized bed reaction zone (FB1) top sets upward area gradually in conical fluidized bed reactor (1) and housing (2)
The taper reaction gas accumulation regions (15) of diminution, make reacting gas depart from fluidized bed reaction zone (FB1) rapidly；In reaction gas accumulation regions
(15) outlet set delivery pipe (21), delivery pipe (21) outlet set reaction terminating controller (3), make reacting gas quickly with urge
Agent departs from and lowers the temperature, and realizes reaction terminating；
Gas solid separation area in housing (2) sets two-stage series connection cyclone separator in parallel more than two；In housing (2) and cone
Shape fluidized-bed reactor (1) sets outward L-type catalyst overflow standpipe (16), revolves reaction terminating controller (3) and two-stage series connection
The catalyst that wind separator is isolated returns to fluidized bed reaction zone (FB1)；Catalyst overflow standpipe (16) entrance is located after reacting
The catalyst for managing area is drawn, and catalyst is introduced fluidized bed reaction zone (FB1) by outlet, and catalyst overflow standpipe (16) entrance is anti-
Should be more than gas accumulation regions (15) cone；Conical fluidized bed reactor (1) is provided with regenerated catalyst inlet (14) and catalysis to be generated
Agent exports (13).
2. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 1, it is characterised in that the reaction terminating controller
(3) gas-solid preseparator is provided with, gas-solid preseparator is provided with central tube (31), taper connection pipe (32) and taper connection pipe
(32) the circumferential cyclone pipe (33) of respective amount, gas outlet tube (35) and shell body (37), the central tube (31) with to
The semi-cone angle that upper area gradually expands, the taper connection pipe (32) is two or more, and circumferentially, cross section is rectangle.
3. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 2, it is characterised in that the reaction terminating controller
(3) it is additionally provided with reaction gas chilling area；The quenching medium entrance (39) in the reaction gas chilling area is arranged on gas outlet tube (35)
On.
4. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 2 or claim 3, it is characterised in that in the central tube
(31) flue (38) is vertically arranged and cyclone pipe (33) outlet between, gas flows out rear steering from cyclone pipe (33), from gas
Annular space between pipe (38) and central tube (31) is flowed upwards out.
5. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 1, it is characterised in that reaction terminating controller (3)
Air shooter (36) is set and two-stage series connection cyclone separator between, makes reaction terminating controller (3) and two-stage series connection whirlwind
First order cyclone separator gas inlet pipe (41) of separator is directly connected to, the product gas from reaction terminating controller (3)
It is directly entered two-stage series connection cyclone separator；Gas outside reaction terminating controller enters cyclonic separation through gas fairlead (44)
Device.
6. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 1, it is characterised in that the reclaimable catalyst outlet
(13) the catalyst controller that catalyst takes heat and recycling catalyst stripping one is provided with pipeline, is realized anti-to catalyst
The control that temperature and recycling catalyst gas are carried is answered, recycling catalyst stripper (62) and catalyst heat collector (61) are gone here and there up and down
Connection arrangement；, to take thermal medium, pressure is full in being produced when taking thermal medium using water for catalyst heat collector (61) water or methanol feedstock
And steam, steam trap (63) connects as one with catalyst heat collector (61).
7. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 1, it is characterised in that the reaction raw materials (Y) exist
Fluidized bed reaction zone (FB1) bottom enters conical fluidized bed, the gas of conical fluidized bed from reaction raw materials feed distributor (12)
Flow velocity is controlled by no more than 1.2m/s.
8. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 7, it is characterised in that the gas of the conical fluidized bed
The average apparent flow velocity that rate of flow of fluid presses the calculating of fluid bed cross section is 0.6~1.0m/s, conical fluidized bed reactor outlet gas
Flow velocity is less than 0.85m/s.
9. the hydrocarbons fluidised-bed reaction method of methyl alcohol system as claimed in claim 1, it is characterised in that conical fluidized bed reactor
(1) semi-cone angle (γ) is 0~30 °.
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