CN102532359B - Method for using rotating-stream tray in phase-phase polyethylene process and rotating-stream tray device - Google Patents
Method for using rotating-stream tray in phase-phase polyethylene process and rotating-stream tray device Download PDFInfo
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Abstract
The invention discloses a method for using a rotating-stream tray in a phase-phase polyethylene process and a rotating-stream tray device. The method comprises the following steps of: arranging a rotating-stream tray separator on a circulating pipeline, leading circulating air current out of the top of a fluidized bed, compressing, condensing, and performing gas-liquid separation in the rotating-stream tray separator to form stream which is rich in liquid phases and stream which is rich in gas phases; and spraying the stream which is rich in liquid phases into the fluidized bed from the upper part of a distributing plate, and introducing the stream which is rich in gas phases into a reactor from the lower part of the distributing plate for fluidizing a material and participating in polymerization, wherein the content of a condensate in the stream which is rich in liquid phases is 60-100 percent by weight of the total content of a condensate in a circulating air current; and the pressure drop through the rotating-stream tray separator is 1,500-6,500 Pa. According to the method and the device, the quantity of the condensate entering a fluidized bed reactor from the upper part of the distributing plate can be increased greatly, the phenomenon of liquid accumulation is avoided, the pressure drop of a gas-liquid separating device is reduced, the adjusting and controlling accuracy and ranges of the condensate quantity are increased, and the energy consumption of a system is lowered; and moreover, the form of the rotating-stream tray separator is optional, and operation is flexible.
Description
Technical field
The present invention relates to a kind of fluidized-bed and introduce working method and the device of phlegma, furtherly, relate to using method and the rotational flow plate device of spiral board in a kind of gas-phase polyethylene technique.
Background technology
Polyethylene is that a class is produced by the kinds of processes method, and the series of products thermoplasticity general-purpose plastics with various structures and characteristic is one of principal item of synthetic resins, is widely used in the fields such as agricultural, chemical industry, light industry, weaving, machinery and national defence.The poly method of industrial production mainly contains three kinds of slurry polymerization process, solution polymerization process and gaseous polymerizations.Wherein, it is simple that gas-phase polyethylene technique has flow process, and throughput is large, and the production handiness is strong, and the material consumption energy consumption is hanged down and the advantages such as safety performance is good, thereby become the main flow in polyethylene process.
Along with the development of national economy, the demand of polyvinyl resin constantly increases, and the polyethylene production that improves existing apparatus becomes the focus that industrial development is attracted attention.In traditional gas-phase polyethylene technique, heat of polymerization mainly removes by the temperature rise of circulating current, thereby poly space-time yield is subject to the restriction that reactor moves heat energy power, can't increase substantially.At the beginning of the eighties in last century, " gas-phase fluidized-bed polyethylene condensation pattern operating procedure " (referred to as " condensation process " or " condensing mode operation ") abroad appearred.Condensation process is by introducing the liquid of easy condensation, be cooling medium (being generally high ' alpha ' olefin and the inertia stable hydrocarbon of copolymerization), make it evaporate to strengthen shifting out of polymerization reaction heat in fluidized-bed reactor, thereby the space-time yield of reactor is significantly improved.The appearance of frozen state technique indicates that the polyethylene production technology has obtained the new breakthrough progress.
Introduce the mode of fluidized-bed according to phlegma, can be divided into two classes with having operational path now: to be phlegma directly bring reactor into by circulating current from the distribuor of fluidized bed bottom by certain device to a class; Another kind of is by certain tripping device, phlegma to be separated from circulating current, partly or entirely introduces bed from distribuor of fluidized bed top by shower nozzle or atomisation unit.In first kind of way, use certain flow-guiding structure can realize the band liquid operation of fluidized-bed, but the problem of thereupon bringing is, when continuing to increase condensing liquid quantity, too much liquid will be assembled at the bottom mixing section, cause particle easily to bond, lump, local superheating occurs, even " melt bed " when serious.Simultaneously, excessive phlegma is accompanied by the together discharging of gas, solid phase, causes temperature decline and pressure rising in feed bin, has reduced the charging efficiency of discharge system.Therefore, the first introducing mode has limited the further increase of condensing liquid quantity, and the space-time yield of reactor is difficult to increase substantially.In the second way, phlegma is introduced separately into fluidized-bed through after separating, and has not only improved the condensing liquid quantity that enters reactor, and can control what of the condensing liquid quantity that enters fluidized-bed with accurate measurement means.Therefore in recent years, investigator both domestic and external carries out the improvement of operational path mainly for the second phlegma introducing mode.
The US Patent No. 5541270 of BP company, US 5668228, US 5733510 and US 5804677 have proposed a kind of new phlegma and have introduced mode, this mode has been used as mechanical means such as separation vessel, cyclonic separator, scum dredger, mist eliminator, pump, compressor or nozzles the condensation liquid phase is separated and enrichment, and injects fluidized-bed reactor from grid distributor or discharge port with the upper part.
The US Patent No. 6455644B1 of Union Carbide Corporation, US 6815512B2, US 7025938B2 proposition gas-liquid separation do not need to use mechanical means such as separator, cyclonic separator, scum dredger, pump, compressor or atomizer, rely on elbow, threeway or other pipeline configuration, can be with the phlegma enrichment in circulation line, machinery-free parts and energy expenditure.But in this patent, the gas-liquid separation effect of disclosed guide-tube structure is limited, the phlegma content that returns to fluidized-bed from grid distributor top at most only accounts for 28.82% of phlegma total content circulating current, most condensed fluid is still from the Returning reactor of fluidized-bed bottom, if further improve the content of phlegma in circulating current, may cause the phenomenon of fluidized-bed bottom hydrops.
in the Chinese patent ZL 200810062156.7 that Zhejiang University delivers, be gas-liquid separator by setting up the gas-liquid jet-pump and transforming circulation line, circulating current is divided into two strands through after gas-liquid separator, stream strand is brought reactor by director by circulating current from the distribuor of fluidized bed bottom, the stream thigh that another one is rich in liquid phase is incorporated into the discharging port of fluidized bed top from one or more of grid distributor top, its power is from take reactor feed gas as dynamafluidal jet-pump, simultaneously can be directly from the bottom bulkhead extraction phlegma of fluidized-bed reactor, avoid the generation of fluidized-bed bottom hydrops phenomenon.
Therefore in the second phlegma introducing mode, the design of gas-liquid separation equipment and select has most importantly determined allocation proportion and the flow of the condensing liquid quantity that enters from the grid distributor upper and lower, and then the space-time yield of reactor has been produced material impact.Simultaneously, because there is certain droop loss in gas-liquid separator, if pressure drop is excessive, certainly will fluidizing gas velocity and the fluidization quality of bed will be affected.Therefore, the gas-liquid separation equipment that How to choose is suitable realizes that circulation gas separates with high-level efficiency, the low pressure drop of phlegma, and the steady running of assurance device is industry urgent problem always.
Summary of the invention
The invention provides using method and the rotational flow plate device of spiral board in a kind of gas-phase polyethylene technique, it can be used for anyly relating to thermopositive reaction and fluidized-bed reactor that need exterior cooling.The present invention is by setting up the spiral board separator on circulation line, part or all of phlegma is separated from circulating current, the stream thigh of liquid phase is rich in formation, spray in fluidized-bed from grid distributor top, can improve the condensing liquid quantity that enters bed and the handiness of regulation and control, reduce the temperature difference of grid distributor and bed, strengthen the stability of producing.
One of purpose of the present invention is to provide the using method of spiral board in this kind gas-phase polyethylene technique, described method comprises: circulating current is from fluidized-bed top derivation, after compressed, condensation, partly or entirely phlegma is separated from circulating current, the formed stream thigh that is rich in liquid phase sprays in fluidized-bed from grid distributor top, and the stream thigh that is rich in gas phase enters in reactor the fluidisation material and participates in polymerization from the grid distributor bottom.Described phlegma directly contact with material and evaporate remove heat.
Wherein, the present invention sets up the spiral board separator on circulation line, circulating current is derived from the fluidized-bed top, enters the spiral board separator after compressed, condensation, and gas-liquid separation occurs in the spiral board separator forms the stream thigh that is rich in liquid phase and the stream thigh that is rich in gas phase; Wherein, in the described stream thigh that is rich in liquid phase, phlegma content is the 60wt%～100wt% of phlegma total content in circulating current, and the pressure drop by the spiral board separator is 1500～6500Pa.
More precisely, described be rich in the liquid phase stream thigh and draw from the spiral board separator after, spray into grid distributor top in fluidized-bed by conveying equipment for fluid substances; Described be rich in the vapor phase stream thigh and draw from the spiral board separator after, enter in fluidized-bed the fluidisation material and participate in polymerization through the grid distributor bottom; Described spiral board separator is selected from external placed type spiral board separator or built-in spiral board separator.In the present invention, the pressure drop of being rich in the content of phlegma in the stream thigh of liquid phase and spiral board separator is subject to the impact of several factors, comprises speed, the liquid content of circulating current, the density difference of gas-liquid two-phase and the structure of spiral board separator etc. of circulating current after condensation.
Described spiral board separator comprises two kinds of optional forms, be respectively external placed type spiral board separator and built-in spiral board separator, consider the different separator form of rear selection according to the content of phlegma in circulating current, requirement and the pressure drop of gas-liquid separation.
The circulating current inlet pipe of described external placed type spiral board separator has certain depth of penetration, and is rich in the space formation fluid-tight between the outlet of liquid phase stream thigh, prevents that gas from flowing out from being rich in the outlet of liquid phase stream thigh; Simultaneously, described external placed type spiral board separator has again the liquid storage function, annular space space between described circulating current inlet pipe and external placed type spiral board separator wall has consisted of the liquid storage space, the liquid phase stream plume that is rich in after the spiral board separator separates enters this space, form liquid level difference, then discharge via being rich in the outlet of liquid phase stream thigh.
Described built-in spiral board separator is arranged on circulation line, and the stream thigh that is rich in liquid phase after separation is directly drawn by above liquid guiding tube spin current plate.
In general, described external placed type spiral board separator separated space is large, and the gas-liquid that is suitable for high phlegma content is separated fully, and described built-in spiral board separator separated space is little, is suitable for the gas-liquid sharp separation of low phlegma content.The present invention can be selected according to the actually operating situation.
1～500 ton/hour of described reaction raw materials airshed, pressure 2～10MPa, 20～150 ℃ of temperature; Flow by conditioned reaction unstripped gas can be controlled the flow that is rich in the liquid phase stream thigh, and the described throughput ratio that is rich in liquid phase stream plume amount and reactor feed gas is 1: (1～10).
Two of purpose of the present invention is to provide this kind to be used for the rotational flow plate device of the using method of above-mentioned gas-phase polyethylene technique spiral board.
Device of the present invention comprises: fluidized-bed polymerization reactor 1, and the fluidized-bed expanding reach 2 on described fluidized-bed polymerization reactor 1 top is provided with recycle gas and draws pipeline 3; Wherein, described pipeline 3 is connected with the spiral board separator after connecting successively compressor 4, condenser 5; Described spiral board separator is provided with and is rich in liquid phase stream thigh outlet 7 and is rich in vapor phase stream thigh outlet 8; Describedly be rich in liquid phase stream thigh outlet 7 and be communicated with conveying equipment for fluid substances 9, described be rich in the vapor phase stream thigh export 8 and the circulation line that passes into bottom fluidized-bed be communicated with; The liquid phase stream thigh that is rich in of drawing from the spiral board separator sprays in fluidized-bed from grid distributor top by conveying equipment for fluid substances 9, and the vapor phase stream thigh that is rich in of drawing from the spiral board separator is entered in reactor the fluidisation material and participated in polymerization by the grid distributor bottom.As previously mentioned, the spiral board separator in the present invention can be selected external placed type spiral board separator 61 or built-in spiral board separator 62.
When described spiral board separator was external placed type spiral board separator, this spiral board separator is selected had a circulating current import, and one is rich in the outlet of liquid phase stream thigh and an external placed type spiral board separator that is rich in the outlet of vapor phase stream thigh; Wherein, described circulating current import and be rich in liquid phase stream thigh outlet and all be positioned at cylinder body bottom; The described height of liquid phase stream thigh outlet that is rich in is lower than the circulating current import; Describedly be rich in vapor phase stream thigh outlet and be positioned at the cylindrical shell top.Gas-liquid separation occurs in described circulating current on spiral board under the effect of centrifugal force, discharge after liquid sedimentation.
In this described external placed type spiral board separator, its barrel diameter is 2～6 times of circulation line diameter, and blade outer end diameter is 0.65～0.85 of barrel diameter; The described liquid phase stream thigh exit diameter that is rich in is 10%～60% of circulating current inlet diameter; Being rich in vapor phase stream thigh exit diameter is 50%～100% of circulating current inlet diameter; It is highly that spiral board is apart from 40%～80% of cylinder body bottom distance that described circulating current inlet pipe inserts; Can regulate according to different gas-liquid separation condition and requirement.
Described spiral board separator also can be selected built-in spiral board separator, and it will be arranged in the circulation line that passes into the fluidized-bed bottom as inner member.Described spiral board separator is selected has a circulating current import, a built-in spiral board separator that is rich in the outlet of vapor phase stream thigh and liquid guiding tube.Wherein, described circulating current import is positioned at cylinder body bottom, and described stream thigh outlet of being rich in gas phase is positioned at the cylindrical shell top, and described liquid guiding tube is positioned at spiral board intercepting basin top; Gas-liquid separation occurs in circulating current on spiral board under the effect of centrifugal force, sedimentation does not occur under the effect of upstream liquid, but discharges by the liquid guiding tube above spiral board.
In this described built-in spiral board separator, its blade outer end diameter is 0.30～0.60 of barrel diameter; The described exit diameter that is rich in the vapor phase stream thigh is 50%～100% of circulating current inlet diameter; The exit diameter of described liquid guiding tube is 5%～20% of circulating current inlet diameter.Described liquid guiding tube has n, 1≤n≤12; It is equidistant arrangement on the circulation tube wall, and perpendicular to the circulation tube wall; ,, be staggered between different rows' liquid guiding tubes when many row's liquid guiding tubes are namely arranged greater than 1 when the row of described liquid guiding tube, the tube wall that prevents from circulating deforms because of unbalance stress.
In device of the present invention, the core component of spiral board separator is the taper spiral board, is arranged by a fixed angle of altitude by one group of swirl vane to form; Wherein, described blade number is 6～36,10～55 °, the blade elevation angle, perforation gas speed 2～20m/s, perforation kinetic energy factor F=5～30m/s (N/m
3)
0.5, high-tension unit middle punch kinetic energy factor can suitably increase.The structure of common cyclonic separator is seen accompanying drawing 3.
Can install wire mesh demister additional on described spiral board Membrane Separator Cylinder for CFB Boiler, with the separation efficiency of further raising phlegma.This wire mesh demister is that to be woven into the round shape net, to be pressed into voidage that double-deck wrinkle shape guipure makes again by the plastic wire that diameter is the wire of 0.1～0.5mm or 0.1～1.5mm be 98% wire mesh demister.
Described conveying equipment for fluid substances be selected from pump, compressor and take unstripped gas as dynamafluidal jet-pump in a kind of, extract the speeds match that the speed that is rich in the liquid phase stream thigh should increase with liquid level in the spiral board separator.Wherein, preferred jet-pump can be drawn unstripped gas ethene as the motive fluid of jet-pump, need not to provide extra power, the utilization system energy.
Compare with conventional art, a distinguishing feature of the present invention is to set up the spiral board separator on circulation line, partly or entirely phlegma is separated from circulating current, improves a condensing liquid quantity that sprays into from distribuor of fluidized bed top in bed.Than the separator of other types, the spiral board separator has advantages of high-level efficiency, low pressure drop and flexible operation.
Another notable feature of the present invention is that the spiral board separator has two kinds of optional forms, and external placed type spiral board separator has the liquid storage function concurrently, and the gas-liquid that is suitable for high phlegma content is separated fully; Built-in spiral board is suitable for the gas-liquid sharp separation of low phlegma content.
In fact whole, compare with prior art, the present invention has following advantage:
1) can improve the condensing liquid quantity that sprays into from grid distributor top in fluidized-bed reactor, reduce simultaneously the pressure drop that gas-liquid separation device produces, the phlegma content that enters from grid distributor top can reach 60%～100% of phlegma total content circulating current, the pressure drop of spiral board separator is 1500～6500Pa, strengthen on the one hand accuracy and the handiness of condensing liquid quantity regulation and control, reduce on the other hand system energy consumption;
2) enter the condensing liquid quantity of fluidized-bed from the grid distributor bottom less, avoid the generation of fluidized-bed bottom hydrops phenomenon;
3) can according to different gas-liquid separation conditions and require to select external placed type spiral board separator or built-in spiral board separator, increase the handiness of operation, can increase substantially the space-time yield of reactor and the stability of device operation, have very strong realistic meaning and using value.
Description of drawings
Fig. 1 is for using the gas-phase polyethylene frozen state process schematic representation of external placed type spiral board separator;
Fig. 2 is for using the gas-phase polyethylene frozen state process schematic representation of built-in spiral board separator;
Fig. 3 is external placed type spiral board cyclone separator arrangement schematic diagram;
Fig. 4 is built-in spiral board cyclone separator arrangement schematic diagram;
Fig. 5 is spiral board structure vertical view.
Embodiment
Fig. 1 and Fig. 2 are respectively the device of using external placed type spiral board and built-in spiral board in a kind of gas-phase polyethylene technique, comprise fluidized-bed polymerization reactor 1, the expanding reach 2 on fluidized-bed polymerization reactor 1 top is drawn pipeline 3 with circulating current and is communicated with, recycle gas is drawn pipeline 3 and is connected successively compressor 4, be connected with external placed type spiral board separator 61 or built-in spiral board separator 62 after condenser 5, two outlets of spiral board separator connect respectively two pipelines, one of them pipeline 7 is by valve 13 access conveying equipment for fluid substances 9, the outflow pipeline 14 of conveying equipment for fluid substances 9 is located at gas distribution grid 15 tops at fluidized-bed reactor 1 middle part, another export pipeline 8 access fluidized-bed polymerization reactor 1 bottoms of spiral board separator.
Circulating current from fluidized-bed expanding reach 2 by drawing after pipeline 3 derives, flow through compressor 4 and condenser 5, coagulated component in circulating current is through condensation, flow out from condenser 5, enter the spiral board separator, return to fluidized-bed 1 from gas distribution grid 15 tops and by pipeline 8 by pipeline 7 bottom fluidized-bed after gas-liquid separation, complete a circulation.The fresh feed gas that reacts required is added in the air-flow that passes into the fluidized-bed bottom by pipeline 16, and simultaneously, if conveying equipment for fluid substances 9 is selected jet-pump, fresh feed gas can add in fluidized-bed through jet-pump by pipeline 17.Catalyzer off and on or continuously adds fluidized-bed from catalyzer storage tank 10 by gas distribution grid 15 tops.Polymerisate is discharged to discharge tank 11 off and on or continuously, and discharge tank 11 is connected with product storage tank 12.
Fig. 3 is external placed type spiral board cyclone separator arrangement.The circulating current that carries partial condensation liquid enters external placed type spiral board separator 24 by inlet ductwork 18, clashing into the rear gas of blind plate 19 forces to pass through from the space of spiral board, the upward movement of spinning, phlegma is assigned on swirl vane 20 from blind plate 19, form liquid film and dispelled into drop by air-flow, drop is got rid of to the tower wall by centrifugal force with flow rotation, intercepting basin through cover cylinder 21 and ring flat-plate 22 compositions flows into downtake 23, discharges from outlet pipe 26.
Fig. 4 is built-in spiral board cyclone separator arrangement.The circulating current that carries partial condensation liquid enters built-in spiral board separator 34 by inlet ductwork 27, clashing into the rear gas of blind plate 28 forces to pass through from the space of spiral board, the upward movement of spinning, phlegma is assigned on swirl vane 29 from blind plate 28, form liquid film and dispelled into drop by air-flow, drop is got rid of to the tower wall by centrifugal force with flow rotation, sedimentation in the intercepting basin of cover cylinder 30 and ring flat-plate 31 compositions is discharged by liquid guiding tube 32.
Fig. 5 is the spiral board vertical view.Spiral board is made of blade 34, blind plate 38, cover cylinder 35, ring flat-plate 36 and downtake 37, cover cylinder 35 is connected to form intercepting basin with ring flat-plate 36, blind plate 38 is positioned at and covers 35 center, blade 34 is distributed in annular space between blind plate and cover cylinder, the dual-side of each blade respectively with blind plate 38 be connected cylinder and 35 be connected, blade plane becomes a α elevation angle with horizontal plane.
Embodiment 1:
Production of linear Low Density Polyethylene (LLDPE) in the fluidized-bed polymerization reactor of application external placed type spiral board separator shown in Figure 1, under the effect of Z-N catalyst system, 88 ℃ of polymeric reaction temperatures, pressure 2.1MPa, reactor superficial velocity 0.67m/s.External placed type spiral board separator barrel dliameter 3.2m, blade external diameter 2.2m, blind plate diameter 0.7m, 25 °, the blade elevation angle, the number of blade 16.Circulating current in pipeline 3 comprises hydrogen, nitrogen, methane, ethane, ethene, hexene and hexane, and pressure is 2.1MPa, and temperature is 86 ℃.Out contain 25% phlegma circulating current from condenser 5, liquid phase is hexene and hexane, and density is 615.2kg/m
3, density of gas phase is 28.0kg/m
3Through external placed type spiral board separator, in pipeline 7, the content of phlegma can reach 80% of phlegma total content in circulating current, and the spiral board separator pressure-drop is 1850Pa.The stream thigh that is rich in liquid phase in pipeline 7 is introduced in fluidized-bed by pump 9, and space-time yield is 270kg/m
3Hr, throughput has improved 200%.
Embodiment 2:
Production of linear Low Density Polyethylene (LLDPE) in the fluidized-bed polymerization reactor of application external placed type spiral board separator shown in Figure 1, under the effect of Z-N catalyst system, 87 ℃ of polymeric reaction temperatures, pressure 2.1MPa, reactor superficial velocity 0.70m/s.External placed type spiral board separator barrel dliameter 2.5m, blade external diameter 2.0m, blind plate diameter 0.6m, 20 °, the blade elevation angle, the number of blade 20.Circulating current in pipeline 3 comprises hydrogen, nitrogen, methane, ethane, ethene, iso-pentane, and pressure is 2.1MPa, and temperature is 84 ℃.Out contain 35% phlegma circulating current from condenser 5, liquid phase is iso-pentane, and density is 650.0kg/m
3, density of gas phase is 33.0kg/m
3Through external placed type spiral board separator, in pipeline 7, the content of phlegma can reach 85% of phlegma total content in circulating current, and the spiral board separator pressure-drop is 3020Pa.The stream thigh that is rich in liquid phase in pipeline 7 is introduced in fluidized-bed by jet-pump, the working fluid of jet-pump is unstripped gas ethene, flow 50t/h, 55 ℃ of temperature, pressure 2.7MPa, being inhaled fluid is the stream thigh that is rich in liquid phase in pipeline 7, flow is 80t/h, with the mass flux ratio of unstripped gas ethene be 1.6: 1, working fluid sprays into fluidized-bed after fluid mixes with being inhaled, space-time yield is 315kg/m
3Hr, throughput has improved 250%.
Embodiment 3:
Production of linear Low Density Polyethylene (LLDPE) in the fluidized-bed polymerization reactor of application external placed type spiral board separator shown in Figure 1, under the effect of Z-N catalyst system, 85 ℃ of polymeric reaction temperatures, pressure 2.3MPa, reactor superficial velocity 0.75m/s.External placed type spiral board separator barrel dliameter 2.5m, blade external diameter 2.0m, blind plate diameter 0.6m, 25 °, the blade elevation angle, the number of blade 18.Install mesh mist eliminator additional, string diameter 0.5mm, voidage 98% at external placed type spiral board Membrane Separator Cylinder for CFB Boiler top.Circulating current in pipeline 3 comprises hydrogen, nitrogen, methane, ethane, ethene, hexene and hexane, and pressure is 2.3MPa, and temperature is 82 ℃.Out contain 45% phlegma circulating current from condenser 5, liquid phase is hexene and hexane, and density is 650.0kg/m
3, density of gas phase is 33.0kg/m
3Through external placed type spiral board separator, in pipeline 7, the content of phlegma can reach 98% of phlegma total content in circulating current, and the spiral board separator pressure-drop is 3580Pa.The stream thigh that is rich in liquid phase in pipeline 7 is introduced in fluidized-bed by pump, and space-time yield is 360kg/m
3Hr, throughput has improved 300%.
Embodiment 4:
Production of linear Low Density Polyethylene (LLDPE) in the fluidized-bed polymerization reactor of the built-in spiral board separator of application shown in Figure 2, under the effect of Z-N catalyst system, 88 ℃ of polymeric reaction temperatures, pressure 2.5MPa, reactor superficial velocity 0.68m/s.Built-in spiral board separator barrel dliameter 0.6m, blade external diameter 0.35m, blind plate diameter 0.1m, 25 °, the blade elevation angle, the number of blade 10, spiral board top sustained height is installed 4 liquid guiding tubes, caliber 0.05m.Circulating current in pipeline 3 comprises hydrogen, nitrogen, methane, ethane, ethene, iso-pentane, and pressure is 2.5MPa, and temperature is 84 ℃.Out contain 10% phlegma circulating current from condenser 5, liquid phase is iso-pentane, and density is 645.5kg/m
3, density of gas phase is 30.0kg/m
3Through built-in spiral board separator, in pipeline 7, the content of phlegma can reach 60% of phlegma total content in circulating current, and the spiral board separator pressure-drop is 3420Pa.The stream thigh that is rich in liquid phase in pipeline 7 is introduced in fluidized-bed by pump, and space-time yield is 200kg/m
3Hr, throughput has improved 120%.
Embodiment 5:
Production of linear Low Density Polyethylene (LLDPE) in the fluidized-bed polymerization reactor of the built-in spiral board separator of application shown in Figure 2, under the effect of Z-N catalyst system, 85 ℃ of polymeric reaction temperatures, pressure 2.3MPa, reactor superficial velocity 0.70m/s.Built-in spiral board separator barrel dliameter 0.6m, blade external diameter 0.35m, blind plate diameter 0.1m, 20 °, the blade elevation angle, the number of blade 12,2 row's liquid guiding tubes are installed in the spiral board top, caliber 0.05m, 2 rows are staggered.Circulating current in pipeline 3 comprises hydrogen, nitrogen, methane, ethane, ethene, hexene and hexane etc., and pressure is 2.3MPa, and temperature is 83 ℃.Out contain 20% phlegma circulating current from condenser 5, liquid phase is hexene and hexane, and density is 618.7kg/m
3, density of gas phase is 28.0kg/m
3Through built-in spiral board separator, in pipeline 7, the content of phlegma can reach 65% of phlegma total content in circulating current, and the spiral board separator pressure-drop is 4955Pa.The stream thigh that is rich in liquid phase in pipeline 7 is introduced in fluidized-bed by jet-pump, the working fluid of jet-pump is unstripped gas ethene, flow 16t/h, 52 ℃ of temperature, pressure 2.7MPa, being inhaled fluid is the stream thigh that is rich in liquid phase in pipeline 7, flow is 50t/h, with the mass flux ratio of unstripped gas ethene be 3.2: 1, working fluid sprays into fluidized-bed after fluid mixes with being inhaled, space-time yield is 225kg/m
3Hr, throughput has improved 150%.
Embodiment 6:
Production of linear Low Density Polyethylene (LLDPE) in the fluidized-bed polymerization reactor of the built-in spiral board separator of application shown in Figure 2, under the effect of Z-N catalyst system, 88 ℃ of polymeric reaction temperatures, pressure 2.5MPa, reactor superficial velocity 0.67m/s.Built-in spiral board separator barrel dliameter 0.6m, blade external diameter 0.30m, blind plate diameter 0.08m, 25 °, the blade elevation angle, the number of blade 12, spiral board top installation 2 row's liquid guiding tubes, caliber 0.05m, 2 rows are staggered, install mesh mist eliminator additional above liquid guiding tube, string diameter 0.5mm, voidage 98%.Circulating current in pipeline 3 comprises hydrogen, nitrogen, methane, ethane, ethene and iso-pentane etc., and pressure is 2.5MPa, and temperature is 86 ℃.Out contain 30% phlegma circulating current from condenser 5, liquid phase is iso-pentane, and density is 650.4kg/m
3, density of gas phase is 30.0kg/m
3Through built-in spiral board separator, in pipeline 7, the content of phlegma can reach 70% of phlegma total content in circulating current, and the spiral board separator pressure-drop is 6210Pa.The stream thigh that is rich in liquid phase in pipeline 7 is introduced in fluidized-bed by jet-pump, the working fluid of jet-pump is unstripped gas ethene, flow 30t/h, 53 ℃ of temperature, pressure 2.7MPa, being inhaled fluid is the stream thigh that is rich in liquid phase in pipeline 7, flow is 60t/h, with the mass flux ratio of unstripped gas ethene be 2: 1, working fluid sprays into fluidized-bed after fluid mixes with being inhaled, space-time yield is 250kg/m
3Hr, throughput has improved 180%.
Claims (9)
1. the using method of spiral board in a gas-phase polyethylene technique, comprise: circulating current is from fluidized-bed top derivation, after compressed, condensation, partly or entirely phlegma is separated from circulating current, the formed stream thigh that is rich in liquid phase sprays in fluidized-bed from grid distributor top, the stream thigh that is rich in gas phase enters in reactor the fluidisation material and participates in polymerization from the grid distributor bottom, it is characterized in that:
Set up the spiral board separator on circulation line, gas-liquid separation occurs and forms the stream thigh that is rich in liquid phase and the stream thigh that is rich in gas phase in circulating current in the spiral board separator; Wherein, in the described stream thigh that is rich in liquid phase, phlegma content is the 60wt%～100wt% of phlegma total content in circulating current, and the pressure drop by the spiral board separator is 1500～6500Pa;
After the described stream thigh that is rich in liquid phase is drawn, spray into grid distributor top in fluidized-bed by conveying equipment for fluid substances from the spiral board separator;
After the described stream thigh that is rich in gas phase is drawn from the spiral board separator, enter in fluidized-bed the fluidisation material and participate in polymerization through the grid distributor bottom;
Described spiral board separator is selected from external placed type spiral board separator or built-in spiral board separator.
2. the method for claim 1 is characterized in that:
In described external placed type spiral board separator, annular space space between circulating current inlet pipe and external placed type spiral board separator wall has consisted of the liquid storage space, the stream plume that is rich in liquid phase after the spiral board separator separates enters this space, form liquid level difference, then discharge via the stream thigh outlet of being rich in liquid phase.
3. the method for claim 1 is characterized in that:
Described built-in spiral board separator is drawn above the stream thigh spin current plate separator that is rich in liquid phase after separation.
4. method as described in one of claim 1～3 is characterized in that:
1～500 ton/hour of reaction raw materials airshed, pressure 2～10MPa, 20～150 ℃ of temperature;
Describedly be rich in the stream plume amount of liquid phase and the throughput ratio of reactor feed gas is 1:(1～10).
5. rotational flow plate device that is used for the using method of one of claim 1～4 described a kind of gas-phase polyethylene technique spiral board, comprise: fluidized-bed polymerization reactor (1), the fluidized-bed expanding reach (2) on described fluidized-bed polymerization reactor (1) top is provided with recycle gas and draws pipeline (3), it is characterized in that:
Described pipeline (3) is connected with the spiral board separator after connecting successively compressor (4), condenser (5);
Wherein:
Described spiral board separator is provided with the stream thigh outlet (7) of being rich in liquid phase and the stream thigh outlet (8) of being rich in gas phase;
Described stream thigh outlet (7) of being rich in liquid phase is communicated with conveying equipment for fluid substances (9);
The described circulation line of stream thigh outlet (8) bottom passing into fluidized-bed that is rich in gas phase is communicated with;
The stream thigh that is rich in liquid phase of drawing from the spiral board separator sprays into grid distributor top in fluidized-bed by conveying equipment for fluid substances (9), and the stream thigh that is rich in gas phase of drawing from the spiral board separator is entered in fluidized-bed the fluidisation material and participated in polymerization by the grid distributor bottom.
6. device as claimed in claim 5 is characterized in that:
Described spiral board separator is for having a circulating current import, an external placed type spiral board separator (61) that is rich in the outlet of stream thigh and the stream thigh outlet that is rich in gas phase of liquid phase;
Wherein:
Described circulating current import and the stream thigh outlet of being rich in liquid phase all are positioned at cylinder body bottom;
The height that the described stream thigh that is rich in liquid phase exports is lower than the circulating current import;
Described stream thigh outlet of being rich in gas phase is positioned at the cylindrical shell top;
The barrel diameter of described external placed type spiral board separator is 2～6 times of circulation line diameter, and blade outer end diameter is 0.65～0.85 of barrel diameter;
The described stream thigh exit diameter that is rich in liquid phase is 10%～60% of circulating current inlet diameter;
The described stream thigh exit diameter that is rich in gas phase is 50%～100% of circulating current inlet diameter;
It is highly that spiral board is apart from 40%～80% of cylinder body bottom distance that described circulating current inlet pipe inserts.
7. device as claimed in claim 5 is characterized in that:
Described spiral board separator is for having a circulating current import, and one is rich in the stream thigh outlet of gas phase and the built-in spiral board separator (62) of liquid guiding tube, and is arranged in the circulation line that passes into the fluidized-bed bottom as inner member; Wherein:
Described circulating current import is positioned at cylinder body bottom;
Described stream thigh outlet of being rich in gas phase is positioned at the cylindrical shell top;
Described liquid guiding tube is positioned at above the spiral board intercepting basin;
The blade outer end diameter of described built-in spiral board separator is 0.30～0.60 of barrel diameter;
The described exit diameter that is rich in the stream thigh of gas phase is 50%～100% of circulating current inlet diameter;
The exit diameter of described liquid guiding tube is 5%～20% of circulating current inlet diameter.
8. device as claimed in claim 7 is characterized in that:
Described liquid guiding tube has n, 1≤n≤12; It is equidistant arrangement on the circulation tube wall, and perpendicular to the circulation tube wall;
, be staggered between different rows' liquid guiding tubes greater than 1 the time when the row of described liquid guiding tube.
9. device as described in one of claim 5～8 is characterized in that:
Described spiral board separator comprises the taper spiral board, is arranged by a fixed angle of altitude by one group of swirl vane to form; Wherein:
Described blade number is 6～36,10～55 °, the elevation angle, perforation gas speed 2～20m/s, perforation kinetic energy factor F=5～30m/s (N/m
3)
0.5
The plastic wire that to comprise by diameter on described spiral board Membrane Separator Cylinder for CFB Boiler be the wire of 0.1～0.5mm or 0.1～1.5mm is woven into the round shape net, is pressed into voidage that double-deck wrinkle shape guipure makes again is 98% wire mesh demister;
Described conveying equipment for fluid substances be selected from pump, compressor and take unstripped gas as dynamafluidal jet-pump in a kind of.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201010617116 CN102532359B (en) | 2010-12-31 | 2010-12-31 | Method for using rotating-stream tray in phase-phase polyethylene process and rotating-stream tray device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201010617116 CN102532359B (en) | 2010-12-31 | 2010-12-31 | Method for using rotating-stream tray in phase-phase polyethylene process and rotating-stream tray device |
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| CN102532359B true CN102532359B (en) | 2013-11-06 |
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| CN105254782B (en) * | 2015-10-14 | 2017-08-29 | 中国石油化工股份有限公司 | The gas-phase fluidized-bed polyethylene condensation state technique of undisturbed advance and retreat induced condensation operation |
| CN105435610B (en) * | 2015-12-03 | 2017-10-10 | 上海交通大学 | A kind of integrated multiple-effect device for meeting the denitration of industrial smoke deep desulfuration and dedusting |
| CN105646758B (en) * | 2016-03-25 | 2017-12-26 | 浙江大学 | A kind of method for preparing polymer |
| CN112274971B (en) * | 2020-09-30 | 2021-11-30 | 南京扬子精细化工有限责任公司 | Hydrogenation reaction product gas-liquid separation method for reducing device energy consumption |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6218484B1 (en) * | 1999-01-29 | 2001-04-17 | Union Carbide Chemicals & Plastics Technology Corporation | Fluidized bed reactor and polymerization process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6218484B1 (en) * | 1999-01-29 | 2001-04-17 | Union Carbide Chemicals & Plastics Technology Corporation | Fluidized bed reactor and polymerization process |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Sinopec Engineering Incorporation Co-applicant after: Zhejiang University Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Engrg Construction Co., SINOPEC Co-applicant before: Zhejiang University |
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Address after: No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: SINOPEC Group Patentee after: SINOPEC ENGINEERING Inc. Patentee after: ZHEJIANG University Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: SINOPEC ENGINEERING Inc. Patentee before: ZHEJIANG University |