CN101535756B - System for fluidizing solid particles including novel outlet for vessel - Google Patents
System for fluidizing solid particles including novel outlet for vessel Download PDFInfo
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- CN101535756B CN101535756B CN2007800429316A CN200780042931A CN101535756B CN 101535756 B CN101535756 B CN 101535756B CN 2007800429316 A CN2007800429316 A CN 2007800429316A CN 200780042931 A CN200780042931 A CN 200780042931A CN 101535756 B CN101535756 B CN 101535756B
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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
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00044—Temperature measurement
- B01J2208/00061—Temperature measurement of the reactants
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00245—Avoiding undesirable reactions or side-effects
- B01J2219/00247—Fouling of the reactor or the process equipment
Abstract
A system for fluidizing solid particles is provided, wherein the fluidized bed system includes a fluidized bed vessel, a fluidized bed section, a disengagement section, a recycle line, and a tapered outlet. Also provided is a method of fluidizing solids by providing a system as described above, fluidizing a bed comprising solid particles, and removing a recycle stream through the tapered outlet.
Description
The cross reference of related application
The application requires the No.60/860 of submission on November 20th, 2006,166 priority, and by reference its disclosure is combined in this article.
Technical field
The present invention relates generally to fluidized system, and the solid that is specifically related in the circular flow is carried the gas phase fluidization bed system of minimizing secretly.
Background technology
The fluidization of solid relates to the solid particle bed in the up gas that passes fluid bed flows " suspension ".Fluidized bed container can be used for various technologies, for example olefin cracking and polymerization technique.The method a kind of most economical and commonly used of making polymer is used the gas-phase polymerization of fluidized-bed reactor.
Usually, prepared in the gas fluidized-bed process of polymer by monomer, the gaseous flow that comprises a kind of or more kinds of monomers is passed through fluid bed continuously under reactive conditions in the presence of catalyst.This gaseous flow is taken out from fluid bed and is circulated back in the reactor.Simultaneously, from reactor, take out polymeric articles, and add new monomer and replace monomer polymerized.Heat heat cycles gas stream in reactor through polymerization.The cooling system outside through reactor removes this heat at another part of circulation.
Understand, what are directly related for the amount of the polymer of fluidized bed polymerization process preparation and the heat that can take out from fluidized bed reaction zone, because react the generating rate that the heat that is discharged is proportional to polymer.In the steady state operation of reaction process, the speed that removes heat from fluid bed must equal to generate the speed of heat, thereby makes bed temperature keep constant.As a rule, through refrigerating gas circular flow in the outside heat exchanger of reactor, heat is removed from fluid bed.
A requirement to fluidized-bed process is that gaseous recycle stream is enough to reaction zone is remained on fluidized state.In the fluidized bed polymerization process of routine, the amount of circulation of fluid that is used for removing heat of polymerization is greater than being used for supporting the amount that fluid bed and the solid that is used to make fluid bed fully mix required fluid.Speed is excessive to be made extra gas flow or flows through fluid bed, thereby obtains extra cooling capacity and make the mixed intensified of reactor bed.Yet,, must regulate the speed of gaseous flow in order to prevent excessive entrained solids from the gas that fluid bed takes out.
The conventional gas-phase fluidized-bed reactor that uses when olefin polymerization and/or alkadienes comprises the dilute phase (freeboard) of fluidised dense-phase bed and close phase surface (bed height) top.Dilute phase mainly comprises gas and small quantities of particles (particularly fine granular).Dense-phase bed usually but always do not remain on the cylindrical straight section of reactor.The dilute phase section is positioned at the dense-phase bed top.Dilute phase section (or breaking away from section) general diameter is bigger, also is called as expansion segment, reduces the amount that reactor gets into the fine granular of other part of reaction system of taking out of thereby be used to fall low gas velocity.Expansion segment generally is made up of the egg end of conical section and reactor.Reactor outlet is positioned at the top of egg end.
In reactor operating period, admixture of gas is discharged from the fluidized bed container top through the outlet that is positioned at the fluidized bed container top cover.This gas mixture streams is returned the import of fluidized bed container through closed circuit or pipeloop.Closed circuit comprises the necessary miscellaneous equipment of operating fluidized bed technology, for example recycle compressor or pump and recirculation cooler.When admixture of gas left the fluidized bed container top, breaking away from the fine granular (near the especially fine granular the reactor outlet) that exists in the section can be carried secretly and flow through recycle loop through circular flow by admixture of gas.Circular flow leaves reactor outlet, gets into reactor again through the equipment in the closed circuit and near the fluidized bed container bottom.After getting into fluidized bed container again, recyclegas or gas/flow flow through gas distributor usually gets back to fluid bed.
The fine granular of carrying secretly in the closed circuit can be piled up (lodge) in the equipment (for example recycle compressor or recirculation cooler) in closed circuit, causes each mass and operational issue.These fine granulars have promoted polymer growth and the fouling on the surface of pipeloop, recirculation cooler, compressor, reactor head bottom and distribution plate do not expected, and the reactor shutdowns that causes not expecting is to clean system.The particle that adheres in the circulatory system may with the fluid bed different technological conditions under continue polymerization in time, the polymer phase ratio that polymer that so forms and fluid bed form has visibly different character (for example, molecular weight, density and molecular weight distribution).Part particle finally discharges from circulatory system surface, carries through circulation of fluid (circular flow) and gets back in the fluid bed.These particles pollute polymeric articles and its character are had a negative impact, and for example improve the gel level in the final products such as plastic containers and film.In addition, fine granular may slowly stop up recirculation cooler or distribution plate, causes various operational issues.The obstruction of recycle unit or distribution plate may cause the reactor cyclic stop to remove the fine granular of accumulation.If reactor stops because of cleaning, then not only reduced the working time but also increased cleaning cost.
Attempted using various systems to prevent that fine granular from leaving from the fluidized bed container top.US5,382,638 have discussed the use cyclone separator makes fine granular separate with circular flow.US4,588,790 have described a kind of technology, and wherein expansion segment is only being used for to arrive the fluidized bed container outlet is separated fine granular before from admixture of gas device at admixture of gas.Other the method for the caused problem of fine granular that is used for solving closed circuit comprises preparation US 4; 383; Disclosed catalyst in 095 is so that the fine granular that produces in the technology is minimum and like US 6,180, the catalyst fine granular in the closed circuit is poisoned.Other background document comprises US3,089,824, JP 59 052524, DE 197 44 710 and FR 2 764 207.
Yet, have the needs that further reduce the amount of the solid particle that leaves fluidized bed container.Particularly, exist to reduce the needs of the amount of the polymer that leaves the gas-phase fluidized-bed polymerizing reactor top and catalyst fine granular.
Summary of the invention
In one embodiment, the invention provides the system that is used for that a kind of amount that makes the solid particle leave the fluidized bed container top reduces with the solid particle fluidised formization.In another embodiment, said fluidized system comprises: fluidized bed container; Fluid bed section in the said fluidized bed container; The disengaging section of said fluid bed section top, wherein said disengaging section comprises top cover; The pipeloop that is communicated with said disengaging section fluid; With the tapered outlet that comprises first port of export that is connected to said top cover and second port of export that is connected to said pipeloop.
In another embodiment; First port of export first the outlet cross section be second port of export second the outlet cross section at least about 1.2 times; And in another embodiment; First the outlet cross section be second the outlet cross section at least about 2.0 times, in another embodiment, first the outlet cross section be second the outlet cross section at least about 3.0 times.
In another embodiment; The first outlet cross section be break away from the section maximum cross section at least about 0.15 times; And in another embodiment; The first outlet cross section be break away from the section maximum cross section at least about 0.25 times, in another embodiment, the first outlet cross section be break away from the section maximum cross section at least about 0.35 times.
In any embodiment of here describing, the changeover portion of tapered outlet is a conical butt, and in another embodiment, the tapered outlet is parabolic cone shape.
In one type of embodiment; The present invention also provides a kind of method with fluidization of solid; Comprise step: fluidized system is provided, wherein said fluidized system comprise the fluid bed section in fluidized bed container, the said fluidized bed container, said fluid bed section top the disengaging section that comprises top cover, export with the said tapered that breaks away from the pipeloop that the section fluid is communicated with and comprise first port of export that is connected to said top cover and be connected to second port of export of said pipeloop; In said fluid bed section, will comprise the bed fluidization of multiple solid particle; From said fluidized bed container, take out circular flow with exporting through said tapered.In this embodiment, the speed of the circular flow of first port of export be about second port of export circular flow speed 71% or littler.
In the another kind of embodiment of this method, the speed of the circular flow of first port of export be about second port of export circular flow speed 25% or littler.In another embodiment, the speed of the circular flow of first port of export be about second port of export circular flow speed 11% or littler.
In another embodiment, the speed of the circular flow of first port of export is about 20 times of superficial velocity in the fluid bed section or littler.In another embodiment, the speed of the circular flow of first port of export is about 8 times of superficial velocity in the fluid bed section or littler.In another embodiment, the speed of the circular flow of first port of export is about 3.5 times of superficial velocity in the fluid bed section or littler.
In any embodiment of here describing, said multiple solid particle comprises polymer solids, for example polyethylene or polyacrylic polymer.
In the another kind of embodiment of this method, polymer solids comprises polyethylene polymer, and the pressure in the fluidized bed container is extremely about 350psig (2414kPa) of about 250psig (1724kPa), and the speed of the circular flow of first port of export is about 2.4-20m/s.Comprise that at polymer solids the speed of the circular flow of first port of export is about 2.4-15m/s in the embodiment of polyethylene polymer.Comprise in another embodiment of polyethylene polymer that at solid circular flow comprises about 2wt% or said multiple solid particle still less.
In any embodiment of here describing, term " cross section " can refer to diameter.
Can clearly be seen that other characteristics of the present invention and advantage through following detailed description.Yet; Detailed description and specific embodiment when should be appreciated that explanation preferred implementation of the present invention are merely exemplary, to those skilled in the art; According to the detailed description of this paper, can carry out various changes and improvement within the spirit and scope of the present invention.
Description of drawings
Fig. 1 is the sketch map of gas fluidised bed polymerisation system that comprises the outlet of prior art;
Fig. 2 is the sketch map with gas phase fluidization paradigmatic system of tapered outlet of the present invention;
Fig. 3 and Fig. 4 show the CFD analog result under two superficial gas velocities (SGV) value.
The specific embodiment
The system that is used for the solid particle fluidised formization that a kind of amount of leaving the solid particle at fluidized bed container top reduces is provided.This system can be used for any gas phase fluidization bed system.This system is specially adapted to take out of through the circular flow that leaves the gas-phase polymerization reactor top gas-phase polymerization system of (or carrying secretly) polymer and/or catalyst fine granular.In another kind of embodiment, except the fine granular that minimizing is carried secretly, this system can also reduce " popped rice shape material " (popcorn) or the carrying secretly of flaky substance (sheet).In one type of embodiment, the present invention is directed to a kind of gas fluidised bed polymerisation system and describe, but this only is an example and not limiting the scope of the invention that those skilled in the art will be appreciated that the application that other is suitable for.
With reference to figure 1, typical gas phase fluidization system comprises fluidized bed container 10, and it has disengaging section 14 fluid bed section 12 and that comprise top cover 13 (also claiming the dilute phase section).In one embodiment, top cover 13 is egg ends, breaks away from section 14 and also comprises conical section 11.
In order to ensure complete fluidization, circulation of fluid (being also referred to as the fluidization fluid here, can gas or gas/liquid combination) stream gets into reactor below fluid bed section 12.By gas distribution plate 18 so that circulation of fluid is evenly distributed to fluid bed section 12.The reaction heat that circulation of fluid generates in absorbing polymer when the bed or other reaction.
The unreacted portion in bed of circulation of fluid is left fluid bed section 12 tops and is got into disengaging section 14.Along with the disengaging section that circulation of fluid is passed fluid bed section 12 tops, most solid particle falls back in the bed.To in compressor 20, compress and, in heat exchanger 22, reaction heat (if existence) will be removed as the circulation of fluid that circular flow leaves fluidized bed container 10 tops through pipeloop 16, then circular flow returned fluidized bed container 10 through heat exchanger 22.Can utilize internal temperature sensor 19 to monitor the temperature of fluid bed.
Referring now to Fig. 2,, in this embodiment, the invention provides a kind of fluidized system that is used for the solid particle fluidised formization, this system comprises: fluidized bed container 10; Fluid bed section 12 in the fluidized bed container; The disengaging section 14 that comprises top cover 13 of fluid bed section 12 tops; The pipeloop 16 that is communicated with disengaging section 14 fluids; With the tapered outlet that comprises first port of export 26 that is connected to top cover 13 and second port of export 28 that is connected to pipeloop 16.In one type of embodiment, abscission zone 14 comprises conical section 11 and egg end 13.This paper alleged " tapered outlet " typically refers to has first outlet and second outlet and the wherein different any outlet of cross section (for example, diameter) of first and second outlets that fluid is communicated with.In one type of embodiment, no matter be which kind of shape, the cross section of first outlet is all greater than the cross section of second outlet.Its shape can be taper, parabolic cylinder shape or the like.
Can design fluidized bed container 10 according to the fluidized system of expectation.Referring to Fig. 2, in this embodiment, fluidized bed container 10 has the disengaging section 14 that is positioned at fluid bed section 12 tops, is fallen back in the bed so that possibly leave the gas entrained solid at fluid bed top.The disengaging section 14 of fluidized bed container 10 can be expansion segment, straight section or its combination.Break away from section 14 and can have the cross section (for example diameter) identical or bigger with fluid bed section 12.
Tapered outlet 24 can be Any shape and be made up of the material of the fluidization process that is fit to expectation.In one embodiment of the invention, tapered outlet 24 also comprises Frusto-conical changeover portion 30.In another embodiment of the invention, tapered outlet 24 also comprises the changeover portion 30 of parabolic cone shape.
Continuation is referring to Fig. 2, and in this embodiment, the first outlet cross section (for example diameter) of first port of export 26 is greater than the second outlet cross section (for example diameter) of second port of export 28.In one embodiment, the second outlet cross section is substantially equal to the cross section of pipeloop 16.Except as otherwise noted, alleged cross section is meant the internal cross section (for example internal diameter) of object member among this paper.Utilize the first bigger outlet cross section (for example diameter), near the gas prompt drop the fluidized bed container outlet is low.Be not bound by theory, can think that near the decline of the gas speed container outlet causes still less solid particle to be taken out of fluidized bed container 10 and circulate through pipeloop 16.In one embodiment; First the outlet cross section be second the outlet cross section at least about 1.2 times, preferably, first the outlet cross section be second the outlet cross section at least about 2.0 times; Even more preferably, first the outlet cross section be second the outlet cross section at least about 3.0 times.
In one type of embodiment, the first outlet cross section also influences the entrained solid grain amount with the ratio that breaks away from section maximum gauge 32.As shown in Figure 2, break away from section maximum gauge 32 and be the imperial palace cross section of the fluidized bed container 10 of fluid bed section 12 tops.In one embodiment of the invention, the first outlet cross section for break away from section maximum gauge 32 at least about 0.15 times, preferably at least about 0.25 times, more preferably at least about 0.35 times.
In another kind of embodiment; The present invention also provides a kind of method with fluidization of solid; Comprise the steps: to provide fluidized system, wherein said fluidized system comprise fluid bed section 12 in fluidized bed container 10, the fluidized bed container 10, fluid bed section 12 tops the disengaging section 14 that comprises top cover 13, export with the tapered that breaks away from the pipeloop 16 that section 14 fluids are communicated with and comprise first port of export 26 that is connected to top cover 13 and be connected to second port of export 28 of pipeloop 16; In fluid bed section 12, will comprise the bed fluidization of multiple solid particle; With from fluidized bed container 10, take out circular flow through tapered outlet 24.In these embodiments, the speed of the circular flow of first port of export 26 be second port of export 28 circular flow speed about 71% or littler, preferred about 25% or littler, even more preferably from about 11% or littler.
In any embodiment described herein, the speed of the circular flow of first port of export 26 is about 20 times or littler of superficial velocity in the fluid bed section 12, preferred about 8 times or littler, and more preferably from about 3.5 times or littler.Superficial velocity used herein is the cross-sectional area of the volume flow of fluidization stream divided by fluid bed section 12.As known in the art is that the method for this computational speed has been ignored the shared volume of fluidized solids.
The amount of from fluidized bed container 10, taking the solid that gets into pipeloop 16 out of also depends on by each locational speed in the density of the type of fluidized solids, pressure or fluidization stream and the fluidized bed container 10.For the paradigmatic system that catalyst fine granular or the polymer fine granular that comprises active catalyst possibly circulate in system and pile up in the position of not expecting, solid carry worth special concern secretly.In some embodiments, the present invention helps to reduce the entrainment of fine granular as far as possible, therefore is specially adapted to the fluidised bed polymerisation of alpha-olefin.Therefore, in one embodiment, said multiple solid particle comprises polymer solids.Polymer solids can be any other polymer for preparing in polyethylene, polypropylene or the fluidized system.
In one type of embodiment, the present invention also is specially adapted to various polymerization techniques, for example polyethylene and polymarization method for prodcing polyacrylates.In one embodiment; Polymer solids comprises polyethylene polymer; Pressure in the fluidized bed container 10 is extremely about 350psig (2414kPa) of about 250psig (1724kPa), and the speed of the circular flow of first port of export 26 is preferably the about 20m/s of about 2.4-, more preferably from about the about 15m/s of 2.4-.
As stated, exist solid can cause the various operational issues of fluidized system in the circular flow.Therefore, hope to reduce the solid that in circular flow, circulates as far as possible.In one type of embodiment, circular flow comprises about 2wt% or said multiple solid particle still less.
Polymerization technique
Embodiment of the present invention described herein is applicable to any gas fluidized-bed process.Gas-phase polymerization process is preferably (for example, to see United States Patent(USP) No. 4,543,399,4,588,790,5,028,670,5; 317,036,5,352,749,5,405,922,5,436,304,5; 453,471,5,462,999,5,616,661 and 5,668,228).
In one embodiment, technology of the present invention relates to a kind of gas-phase polymerization process of or more kinds of olefinic monomers, and said olefinic monomer has 2-30 carbon atom, preferred 2-12 carbon atom, more preferably 2-8 carbon atom.The present invention is specially adapted to the polymerization of two kinds or more kinds of following olefinic monomers: ethene, propylene, 1-butylene, 1-amylene, 4-methyl-1-pentene, 1-hexene, 1-octene, 1-decene.
Other monomer that can be used for method of the present invention comprises ethylenically unsaturated monomers, has the alkadienes of 4-18 carbon atom, conjugation or unconjugated diene, polyenoid, vinyl monomer and cycloolefin.The monomer that can also use comprises ENB, norbornadiene, isobutene, isoprene, vinyl benzo cyclobutane, styrene, the substituted styrene of alkyl, ethylidene norbornene, bicyclopentadiene and cyclopentene.
In one embodiment, prepared the copolymer of ethene, therein ethylene and a kind of or more kinds of 'alpha '-olefin monomers (having 3-15 carbon atom, preferred 4-12 carbon atom, more preferably 4-8 carbon atom) polymerization in gas phase process.
Reactor pressure in the gas-phase polymerization process can change from about 100psig (690kPa) to about 600psig (4138kPa); Be preferably about 200psig (1379kPa) to about 400psig (2759kPa), more preferably about 250psig (1724kPa) is to about 350psig (2414kPa).
The temperature of the fluid bed in the gas-phase polymerization process can be about 30-140 ℃, and preferably about 60-115 ℃, more preferably from about 70-110 ℃, most preferably from about 70-95 ℃.
In one embodiment of the invention, superficial velocity can be 0.4-1.5m/s, preferred 0.5-0.9m/s.
Other gas phase process that method of the present invention is suitable for comprises series connection or multistage polymerization technique.In addition, other gas phase process of the present invention's use comprises United States Patent(USP) No. 5,627; 242,5,665,818 and 5; 677,375 and the open EP-A-0 794 200 of European patent, EP-B1-0 649 992, EP-A-0802 202 and EP-B-634 421 in describe those.
In one embodiment, the present invention relates to be used for independent polymerising ethylene or polypropylene or with the polymerization technique of ethene or propylene and a kind of or more kinds of other monomer polymerizations, wherein other monomer comprises the alkene with 2-12 carbon atom separately.Use the metallocene catalyst of describing in the United States Patent(USP) No. 5,296,434 and 5,278,264 can prepare polymer.Yet the present invention is not limited to use any caltalyst set type.Therefore; The present invention can adopt metallocene catalyst, constrained geometry catalyst, Ziegler-Natta catalyst, chromium-based catalysts, ferrum-based catalyst, nickel-base catalyst and dual catalyst system, comprises the metallic compound that uses at least a metallocene and at least a 15 family's atoms (for example N).
Simulation
Fig. 3 and Fig. 4 show computational fluid dynamics (CFD) Simulation result.The CFD simulation is a kind of known method that fluid mechanics equation (for example, Navier Stokes equation) calculates gas flowfield of finding the solution.In this article, use CFD to simulate UNIPOL
TMThe flow field of reactor head (expansion segment).The result shows the advantage of the embodiment of employing tapered outlet design of the present invention.
Fig. 3 and Fig. 4 utilize two-dimentional axial symmetry geometry to obtain down at the superficial gas velocity (SGV) of 2.4ft/s and 2.8ft/s respectively.Each figure has simulated the outlet of four kinds of different geometries, comprising: (1) standard outlet design; (2) the diameter ratio is that 2: 1 and semi-cone angle are 30 ° tapered outlet (30 ° semi-cone angle makes the height of frustum of a cone equal 0.866 times of outlet diameter); (3) the diameter ratio is the tapered outlet of 3: 1 and height identical with (2) (outlet diameter 0.866 times); (4) the diameter ratio is 4: 1 and the height tapered outlet identical with (2).
Fig. 3 and Fig. 4 show the CFD analog result under aforesaid two kinds of superficial gas velocities (SGV).Particularly, Fig. 3 and Fig. 4 show the middle linear velocity of calculating and the relation of height of expansion segment.Should be noted that highly be top (this position is in the joint of cylindrical portion and conical section, also is called as " neck " of reactor), 0.0 position corresponding to reactor cylindricality section.Under the situation of standard design (no tapered outlet), the top of reactor is positioned at the position of 37.1 feet of neck tops.The velocity contour of relatively more different outlet designs is a reference point with this position mark for ease.
Can find out that from Fig. 3 and Fig. 4 the gas speed of expansion segment is substantially constant in 0 to 30 foot altitude range.More than the height, can see that the speed of giving vent to anger is along with the flow field raises rapidly near outlet at this.Fig. 3 and Fig. 4 show that the effect of tapered outlet is to delay speed to increase, and the point (or transition point) that speed is increased moves towards higher position.Compare with standard outlet design, the diameter ratio is that 2: 1 conical outlet can move about 1.2 feet with transition point towards higher position.The diameter ratio is that the tapered outlet of 3: 1 and 4: 1 is moved about 2.5 feet with transition point towards higher position.
Compare with the design of standard reaction device, the tapered reactor outlet can change gas flow effectively.The tapered outlet makes higher to the position of high-speed transition, and this estimates to reduce the particle entrainment under the given SGV.
Should be noted that for 3: 1 and tapered outlet design in 4: 1, the difference between the rate curve less relatively (all like this under two kinds of SGV).Therefore, can adopt the outlet diameter ratio is 3: 1 embodiment.
Shown in the CFD simulation, the effect of tapered outlet is the position that speed increases suddenly to occur near the rising expansion segment.For the diameter ratio is 3: 1 outlet, and this position has raise about 2.5 feet.
Therefore, the rising of this position has increased the effective depth of expansion segment with relatively low cost.Bound by theory can not thought, the rising of this position can advantageously be used in technology at least in two ways.Under the condition that all other variablees equate, embodiment of the present invention will improve the efficient (that is, increasing effectively " breaking away from height ") that breaks away from section, thereby reduce the amount of the fine granular of for example carrying secretly from fluid bed (for example, catalyst and resin spirit fine grained).This can reduce the caused problem of particle entrainment in the technology conversely, and these problems include but not limited to equipment (for example circulating air compressor, cooler, the distribution plate etc.) fouling in the circulatory system.
In addition, can also use embodiment of the present invention to reduce the reactor of (for example, reduce height and/or reduce diameter) with lower one-tenth the design expansion segment size.In other words, under the particle entrainment speed that equates, can reduce required expansion segment size, thereby reduce the cost of investment of reactor.
Except as otherwise noted; Phrase " basically by ... form " do not get rid of exist (no matter whether in specification, the mentioning) of other step, element or material; Prerequisite is that these steps, element and material do not influence basis of the present invention and novel characteristic, and the common impurity relevant with material with used element do not got rid of in this phrase.
For for simplicity, some number range is only clearly disclosed among this paper.Yet a certain lower limit can be used to put down in writing not the clearly scope of record with other lower limit combination, and is same, and a certain lower limit also can be used to put down in writing not the clearly scope of record with any upper limit combination.In addition, scope comprises each point or the independent value (even without clearly record) between the two-end-point.Therefore, each point or separately value itself can be used as the upper limit or lower limit and other point or value or other bound make up and be used to put down in writing the scope of clearly not putting down in writing separately.
By reference all prior art documents are combined in this article, prerequisite is that its disclosure does not contradict with description of the invention.In addition, all lists of references that this paper quotes (comprising test program, publication, patent, journal article etc.) all combine in this article by reference, and prerequisite is that its disclosure does not contradict with description of the invention.
Although preceding text are described the present invention to embodiment and embodiment, it will be appreciated by those skilled in the art that under the prerequisite that does not depart from the scope of the present invention with spirit, can design other embodiment in light of the disclosure herein.
Claims (11)
1. system that is used for the solid particle fluidised formization, said system comprises:
(a) fluidized bed container;
(b) fluid bed section in the said fluidized bed container;
(c) the disengaging section above the said fluid bed section, wherein said disengaging section comprises top cover;
(d) pipeloop that is communicated with said disengaging section fluid; With
(e) comprise the tapered outlet of first port of export that is connected to said top cover and second port of export that is connected to said pipeloop, the changeover portion of wherein said tapered outlet is conical butt or parabolic cone shape.
2. system as claimed in claim 1, the first outlet cross section of wherein said first port of export is at least 1.2,2.0 or 3.0 times that second of said second port of export exports cross section.
3. system as claimed in claim 1, the diameter of wherein said first port of export is at least 1.2,2.0 or 3.0 times of diameter of said second port of export.
4. like any described system among the claim 1-3, the first outlet cross section of said first port of export is at least 0.15,0.25 or 0.35 times of disengaging section maximum cross section.
5. like any described system among the claim 1-3, the diameter of said first port of export is at least 0.15,0.25 or 0.35 times of the diameter that breaks away from section.
6. the method with fluidization of solid comprises the steps:
(a) fluidized system is provided, wherein said fluidized system comprises:
(1) fluidized bed container;
(2) fluid bed section in the said fluidized bed container;
(3) the disengaging section above the said fluid bed section, wherein said disengaging section comprises top cover;
(4) pipeloop that is communicated with said disengaging section fluid; With
(5) comprise the tapered outlet of first port of export that is connected to said top cover and second port of export that is connected to said pipeloop, the changeover portion of wherein said tapered outlet is conical butt or parabolic cone shape;
(b) in said fluid bed section, will comprise the bed fluidization of multiple solid particle; With
(c) from said fluidized bed container, take out circular flow through said tapered outlet,
Wherein, the speed of the circular flow of said first port of export is less than 71%, 25% or 11% of the speed of the circular flow of said second port of export.
7. method as claimed in claim 6, the speed of the circular flow of wherein said first port of export is less than 20 times, 8 times or 3.5 times of the superficial velocity in the said fluid bed section.
8. like the method for claim 6 or 7, wherein said multiple solid comprises polymer solids.
9. method as claimed in claim 8, wherein said polymer solids comprises polyethylene or polyacrylic polymer.
10. like the method for claim 6 or 7, the pressure in the wherein said fluidized bed container be 250psig (1724kPa) to 350psig (2414kPa), the speed of the circular flow of said first port of export is 2.4-20m/s or 2.4-15m/s.
11. like the method for claim 6 or 7, wherein said circular flow comprises the said multiple solid particle less than 2wt%.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US86016606P | 2006-11-20 | 2006-11-20 | |
| US60/860,166 | 2006-11-20 | ||
| PCT/US2007/023750 WO2008063463A1 (en) | 2006-11-20 | 2007-11-13 | System for fluidizing solid particles including novel outlet for vessel |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101535756A CN101535756A (en) | 2009-09-16 |
| CN101535756B true CN101535756B (en) | 2012-05-02 |
Family
ID=38057507
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007800429316A Expired - Fee Related CN101535756B (en) | 2006-11-20 | 2007-11-13 | System for fluidizing solid particles including novel outlet for vessel |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP2084478A1 (en) |
| CN (1) | CN101535756B (en) |
| BR (1) | BRPI0719119A2 (en) |
| WO (1) | WO2008063463A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SG184469A1 (en) * | 2010-04-05 | 2012-11-29 | Dow Global Technologies Llc | Process for polymerizing olefin-based polymers containing high molecular weight fractions in condensed and super-condensed mode |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4588790A (en) * | 1982-03-24 | 1986-05-13 | Union Carbide Corporation | Method for fluidized bed polymerization |
| CN87103148A (en) * | 1986-04-30 | 1987-11-11 | 燃烧工程有限公司 | Fluidized bed combustor with integral solids separator |
| US5028670A (en) * | 1988-07-15 | 1991-07-02 | Bp Chemicals Limited | Process for the gas-phase polymerization of olefins in a fluidized-bed reactor |
| US5507531A (en) * | 1995-05-04 | 1996-04-16 | Ewal Manufacturing Company, Inc. | Seal enhancer for cylinder valve connection |
| CN1286700A (en) * | 1997-11-17 | 2001-03-07 | 波利亚里斯技术有限公司 | Method and apparatus for preparing polymers |
| CN1477131A (en) * | 2002-03-25 | 2004-02-25 | 三井化学株式会社 | Method for producing polyolefin |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| PT1644422E (en) * | 2003-07-11 | 2007-02-28 | Ineos Europe Ltd | Process for the (co-)polymerisation of ethylene in the gas phase |
| WO2005113615A2 (en) * | 2004-05-20 | 2005-12-01 | Univation Technologies, Llc | Gas olefin polymerization process |
-
2007
- 2007-11-13 BR BRPI0719119-7A patent/BRPI0719119A2/en not_active Application Discontinuation
- 2007-11-13 EP EP07840023A patent/EP2084478A1/en not_active Withdrawn
- 2007-11-13 CN CN2007800429316A patent/CN101535756B/en not_active Expired - Fee Related
- 2007-11-13 WO PCT/US2007/023750 patent/WO2008063463A1/en active Search and Examination
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4588790A (en) * | 1982-03-24 | 1986-05-13 | Union Carbide Corporation | Method for fluidized bed polymerization |
| CN87103148A (en) * | 1986-04-30 | 1987-11-11 | 燃烧工程有限公司 | Fluidized bed combustor with integral solids separator |
| US5028670A (en) * | 1988-07-15 | 1991-07-02 | Bp Chemicals Limited | Process for the gas-phase polymerization of olefins in a fluidized-bed reactor |
| US5507531A (en) * | 1995-05-04 | 1996-04-16 | Ewal Manufacturing Company, Inc. | Seal enhancer for cylinder valve connection |
| CN1286700A (en) * | 1997-11-17 | 2001-03-07 | 波利亚里斯技术有限公司 | Method and apparatus for preparing polymers |
| CN1477131A (en) * | 2002-03-25 | 2004-02-25 | 三井化学株式会社 | Method for producing polyolefin |
Also Published As
| Publication number | Publication date |
|---|---|
| EP2084478A1 (en) | 2009-08-05 |
| WO2008063463A1 (en) | 2008-05-29 |
| CN101535756A (en) | 2009-09-16 |
| BRPI0719119A2 (en) | 2013-12-10 |
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