TW200426156A - Fluidized bed methods for making polymers - Google Patents

Abstract

The invention relates to continuous gas fluidized bed methods for making a polymer featuring a condensing agent in a recycle stream; and also to methods for monitoring and providing continuity in a gas fluidized bed method for making a polymer featuring a condensing agent in a recycle stream. Certain ranges of Δρ, in some cases combined with certain ranges of values for An, can be used to find and define desirable operating states, i.e., the "steady state," "alert state," "corrective action state," "continuity impairment state" and/or " Δρ alarm state," for the gas fluidized bed reactor polymerization method (where Δρ, An and the particular states are disclosed herein).

Description

200426156 发明 Description of the invention: [Technical field to which the invention belongs] Generally speaking, the present invention relates to a continuous gas fluidized bed method for manufacturing polymers, which is characterized by a condensing agent in a circulating flow; and also about manufacturing polymers It is characterized by a condensing agent that monitors and provides continuity in a gas fluidized bed process in a circulating stream. [Prior art] In general, the polymerization system is exothermic. Therefore, in the production of polymers in a fluidized bed, the heat generated by the polymerization reaction must be removed to keep the reaction temperature in the bed in a desired range. Conventionally, the temperature of the fluidized bed of the reactor is controlled to a substantially isothermal temperature by continuously removing the heat of polymerization. The method is to circulate the gas leaving the fluidized bed to the condenser / heat outside the reactor. Exchanger and recycle the cooled gas stream back to the reactor. When the temperature of the recycle stream introduced or recycled into the fluidized bed polymerization reactor is higher than the dew point temperature, substantially no liquid is present, and therefore, this operation is referred to in the art as `` dry "Mode" method. However, it is clear that the recirculation stream does not have to be completely gaseous, but can include gas and liquid. In this method, the flow system cools the circulation stream below the dew point temperature, thereby converting a portion of the gas into The liquid is formed and the cooled circulating stream is introduced into the fluidized bed polymerization reactor. This mode of operation is referred to in this art as the f 'condensation mode π or `` condensation mode π method. Fluidization in condensation mode The bed reactor polymerization process has been disclosed, for example, in U.S. Patent Nos. 4,543,399 and 4,588,790 issued to Jenkins et al., Each of which describes the introduction of an inert liquid into the circulating stream to increase the dew point temperature of the circulating stream and allows the 85552 200426156 method to reach Operation at 17.4% liquid to weight ratio based on the total weight of the cooled circulating stream. The condensing mode method is considered to be advantageous because of its removal Polymerization capacity of the fluidized bed polymerization reactor is increased by the ability to generate a larger amount of heat from the polymerization reaction. Condensing mode fluidized bed reactor polymerization operating in a cooled circulating stream with a liquid-to-weight ratio higher than 17.4% Methods have been disclosed; however, such methods must be limited to a limited range of operating conditions to avoid destabilizing the fluidized bed and thus suspend the process. For example, US Patent 5,352,749 to DeChellis et al. Content, the ratio of fluidized bed density ("FBE") to the density of the sedimentary body (nSBDn) is required to remain higher than 0.59 throughout the fluidized bed polymerization process. In particular, 'this reference material reveals that `` the general rule is that a reduction in the ratio of FBD to SBD below 0.59' may involve the danger of fluidized bed disintegration and is to be avoided ". Regarding the different but still limited ranges of the operating conditions of the condensing mode fluidized bed polymerization reactors, they are disclosed in U.S. Patent Nos. 5,436,3G4 and 5,462,999 issued to Griffin et al. Each of these references defines the so-called "bulk density function (z)," (see, for example, the definition of z in column 12, lines 31_42 of US Patent 5,436,304), and states that Z is intended to be used throughout the fluidized bed polymerization process. Is kept at a value equal to or greater than the so-called calculated limit of the bulk density function (see, eg, column 12, lines 66-68 in US Patent 5,436,304) to avoid destabilizing the fluidized bed. Regarding yet another different but still limited range of operating conditions for a condensing-mode fluidized-bed polymerization reactor, it is disclosed in US Patent 6,391,985 issued to Gode et al. This reference will be Fluidized bed polymerization processes operating in a circulating flow and in a so-called `` turbulent system π '' as defined in t 85552 200426156 at a liquid-to-weight ratio of at least 17.5% (see, e.g., column 4, columns 20-27 and 52- Line 54; Column 2, Lines 3-9) Stated as "the state of the fluidized bed that exists between (1) the presence of identifiable bubbles and (2) the conditions of rapid fluidization, and / or the transition Velocities Uc and (b) at surface gas velocity The condition system between the conveying speeds Uk ". However, it is still necessary to confirm the wide range of operating conditions of the condensation mode fluidized bed reactor polymerization method. Limiting the condensation mode fluidized bed reactor polymerization method to a limited operating range, For example, as discussed above, in order to avoid destabilizing the fluidized bed, the benefits of condensing mode operation cannot be fully realized. Furthermore, the above references do not even point out that the polymer is characterized by a condensing agent. In the method of circulating flow, and / or in the method of manufacturing polymers characterized by a condensing agent in a gas fluidized bed method of circulating flow and providing continuity, focus on, for example, the lower fluidized bed density and The difference between the density of the upper fluidized bed. In the prior art paragraph of this application, the citation of any reference material does not recognize that any such reference material is the prior art of this application. [Summary of the Invention] One of the inventions A specific embodiment relates to a continuous gas fluidized bed method for manufacturing a polymer, which is characterized by a condensing agent in a circulating stream, which Including: In a reaction zone with a controlled reactor bed temperature, a lower fluidized bed density, an upper fluidized bed density, and a plurality of measurement positions n temperature, in the presence of a catalyst, a gas flow containing monomers and a condensing agent is caused. , Continuously pass through the fluidized bed; take out the polymerization product from the reaction zone, and a gas stream containing unreacted gas; recycle this gas stream and a sufficient amount of other monomers to the reaction zone to replace the polymerization by 85552 200426156 and polymerize the product The monomer being pumped off; the circulating stream is cooled to condense a portion thereof and form a liquid-containing mixture having a circulating stream dew point temperature, a reactor inlet temperature, and containing about 17.5% to about 70% liquid by weight Ratio, based on the total weight of the cooled circulating stream, where the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is greater than or equal to about 5 ° C; and the mixture is introduced into the reaction zone, Where the liquid in the mixture is vaporized; where Λρ satisfies the condition of 0 kg / m3 $ Δρ &lt; 70 kg / m3, and when Δρ-10 kg / m3, at least one critical number of Aη The project also meets the conditions of 0.25 $ Αη &lt; 0.8. Another embodiment of the present invention relates to a method for monitoring and providing continuity in a gas fluidized bed method characterized in that a condensing agent is circulated in a circulating flow in the manufacture of a polymer, which includes: monitoring a fluidized bed reaction zone Zone, where the reaction zone has controlled reactor bed temperature, lower fluidized bed density, upper fluidized bed density, and temperature at multiple measurement positions η; monitor the circulating flow into the reaction zone, where the gas stream has a reactor inlet Temperature; measure Δρ, and compare Δρ with at least one limit; and when Δρ-10 kg / m3, measure multiple Aη, and compare each Aη with lower and higher values. Each Aη and Δρ are as defined herein. DETAILED DESCRIPTION OF THE INVENTION Generally speaking, the present invention relates to a continuous gas fluidized bed process for the manufacture of polymers, which is characterized by a condensing agent in a circulating stream, and the polymer is produced while 85552 200426156 is characterized by a condensing agent in a circulating stream. A method for monitoring and providing continuity in a gas fluidized bed process. ′ Referring to FIG. 1, a typical commercial continuous gas fluidized bed reactor polymerization device &lt; non-limiting and not intended, the reaction tower includes a reaction zone 2 and an expansion zone 4. In the reaction zone: inside is the fluidized bed 6, which is contained in the reaction zone via a monomer such as ethylene introduced into the reactor, and whether it is obtained from the source via line 8, or, 'Secondary &amp;,' Springs 24, 16 and 8 are polymerized from a mixture of substances from source 10B to make <microparticle polymers or copolymerization products. The catalyst can be introduced into the reactor from the source M through the tube. For example, f is used with pure high-pressure nitrogen to feed the catalyst to the reactor. Although FIG. 1 illustrates a specific embodiment having a cylindrical reaction zone, a cylindrical shape is not necessary. For example, the reactor wall may be vertical, inclined, or may expand inwardly or outwardly as the height of the reactor is increased. Due to A, the reaction zone may have a geometric chirp such as a cylindrical, conical or rectangular shape. Moreover, the geometry of the expansion zone is not important, for example, it may be a cylindrical, conical, geometric shape φ or rectangular. The ratio of the height of the reaction zone 2 to the cross-sectional area can be changed according to, for example, the required production capacity and residence time, which means the ratio of the weight of the bed (expressed in pout) to the production rate (expressed in meters / hour meter). For a cylindrical reactor, the ratio of the height of the reaction zone 2 to the internal pressure varies depending on the desired capacity. For example, in a specific embodiment, the spoon is 1.1 to about 12.1, and In another specific embodiment, it is about 2.5: 1 to about 8: 1. The maximum internal cross-sectional area of the expansion zone 4 can also be changed. In a specific embodiment, it may be about 2 to about 3 times the cross-sectional area of the reaction zone 2A. 85552 -10- 200426156 During a continuous gas fluidized bed polymerization reaction, in the gas stream flowing through the fluidized bed, for example, part injuries may react below about 10% by weight. Most of the gas flow will not react in the fluidized bed, leaving the reaction zone 2 of the reaction tower and passing into the bed &lt; expansion zone 4, also known as freeboard zone. This gas stream carries with it microparticles. When the velocity of the gas stream decreases, this is due to the increase in the cross-sectional area of the expansion zone. Larger entrained particles will fall back into the fluidized bed, reducing the migration of particulate products away from the reaction tower. The smaller entrained particles that are carried away from the reaction tower in the line% are conventionally referred to as, fine powder &amp; springs may have a separator, such as a cyclone separator, to remove the entrained particles And return it to the fluid bed. Each of these characteristics is a conventional 0 other monomer, such as butene, which may be introduced into the mixture as appropriate, such as from source 18A through line 8 or from source 18B through line ^. In addition, catalyst promoter components may be introduced into the mixture as appropriate, such as from source 20 through line 8. If it is desired to introduce the catalyst and / or auxiliary catalyst components together, this combination can be introduced, for example, from a source 21 to a fluidized bed via line 13. Each of these characteristics is customary. Optionally, at least one molecular weight control agent, such as a chlorine bond transfer agent, is introduced into the mixture, such as from source 22A through line 8 or from source 22b through line 24. When the 'inert gas' such as nitrogen and ethane is present in the mixture, as long as it does not adversely affect the coupling reaction. Each of these characteristics is customary. The circulation line 24 continuously removes unreacted gas from the expansion zone 4. The circulating flow is passed through the compressor 26 to the condenser / heat exchanger to remove and react 85552 -11-200426156 heat from the exothermic polymerization process in the reaction zone 2. For example, conventional centrifugal compressors and shell and tube condensers can be used. In the specific embodiment of FIG. 1, the mixture is recirculated through the pipeline 8, through the turning plate 30 and the distribution plate 32, each of which contains multiple holes, and enters the fluidized bed 6 with the supplementary monomer to replace the polymerized polymer. For example, from source 10A and optionally from source 18A. Each of these characteristics is customary. The method for compressing, condensing, and reintroducing the circulating flow into the fluidized bed reactor can be changed by the arrangement described in Fig. 1, as is known in the art. For example, a single condenser may be used, or multiple condensers connected in parallel or in series may be used. Water is often the coolant of choice. The ability to remove heat from a fluidized bed reactor can be increased by chilling the coolant. The compressor can be located before or after the condenser (as shown in Figure 1), or between condensers if multiple condensers are used. In the specific embodiment shown in Fig. 1, the point of entry of the circulating flow, e.g., through line 8, is below the lowest point of the fluidized bed. Without wishing to be bound by theory, this entry mode is thought to provide a relatively uniform flow of the circulating flow throughout the reactor, keeping the fluidized bed suspended, and ensuring that the uniform circulating flow passes through the entire fluidized bed. In another embodiment, the circulating flow can be divided into a plurality of individual flows, and at least one of them can be directly introduced into the fluidized bed, for example, via line 8A. For example, as disclosed in U.S. Patents 6,001,938 and GB 1,398,965 issued to Chinh et al., Circulating flow can be distinguished into a liquid circulating flow and a gas-containing circulating flow. Then, the liquid circulating stream can be individually introduced into the side of the reactor through the direct feed line 8A, while the circulating stream containing gas can be introduced under the fluidized bed through the line 8 at the same time. Of course, as is well known in the art of -12- 85552 200426156, any number of split circulating flows can be used, and the split circulating flows can each have the same or different liquid to gas ratios. The gas fluidized bed reactor and its associated compression and cooling system are operated under pressure ... The polymerization device of the continuous gas fluidized bed reactor is contained in a pressure vessel. The reactor pressure may be from about 7 to about 70 kg / cm2. In another embodiment, the reactor pressure is about u to about 42: kg / cm². In another embodiment, the reactor pressure is about 14 to about 39 kg / cm2. 1 In another embodiment, the reactor pressure is about 17 to about 28 kg / cm2. In another specific embodiment, the reactor pressure is about 18 to about 24 kg / cm². Conventionally, the height of the fluidized bed in the reaction zone 2 is prevented from continuously increasing by extracting a part of the microparticle polymerization product, and the rate is equivalent to the formation rate of the product. For example, the particulate polymer product is removed through at least one product discharge system (,, PDS "). In the specific embodiment shown in Figure 丨, the example PDS system includes line 34 to feed the product into the discharge tank" in · " It can be removed intermittently or continuously from it through the valve 38, the tank 40 and the valve 42, as required, each of which is known in the art. In another specific embodiment, two parallel discharge systems exist and alternate during operation. The mixture entering the reactor through line 8 preferably contains not only new monomers from source 10A or 10B, but also at least one condensing agent, such as introduced from source 44 through line 16 to help remove the reactor The heat of polymerization is as known in the art. The condensate removed from the reactor, for example with polymer entering tank vat 36, can be collected, recycled to source 44, and transferred to line 16. If optional co-monomers are used, the optional co-monomers are removed from the reactor 85552 -13- 200426156, for example, with the polymer entering the tank 36, which can be collected, recycled to source 48, and transferred to the pipeline 16. Similarly, the combined monomers, co-monomers, and condensing agents removed from the reactor, such as accompanying polymer into tank 36, may be collected, recycled to source 牝, and transferred to line 16. Each of these characteristics is customary. Of course, it is also known in the art to combine some of the sources discussed above to reduce the amount of equipment necessary to perform this continuous gas fluidized bed reactor polymerization. For example, the condensing agent can be introduced with any or all of the monomers derived from source 10A, co-monomers selected, molecular weight control agents selected from source 22A, and catalysts. The invention is not limited to any particular type of polymerization or copolymerization. For example, the present invention can be applied to one or more of the following monomers and / or monomer types for permanent reaction or copolymerization reaction. · Olefin monomers, such as alkene, and olefin monomers, such as acetamidine, propylene, butadiene Ene], pentenylmethylpentene q, hexene-1, heptyl-1, octane-4, phenethylhydrazone, methylstyrene and p-methylstyrene, dibasic, which may be conjugated Or non-conjugated, such as I, cyclopentadiene, 2-methyl-1,3-cyclohexadiene, 5-methyl 4,3 · cyclohexadiene, cycloheptadiene, ethylene Beibei, and those containing at least one heart carbon-carbon double bond, such as butene, isoprene, chloroprene, 丨, pentadiene and 丨, hexamethylene difluoride; acetylene monomer, For example, acetylene, methylacetylene, and ethylacetylene; polar acetamyl precursors, such as vinyl acetate, vinyl acrylate, vinyl methacrylate, vinyl chloride, vinyl fluoride, methyl ethyl ether, and propionic acid Methyl esters, methyl methylpropionate, tetrafluoroethylene, and propionitrile; and aldehyde monomers such as formaldehyde and ethene. In the specific embodiment, this method is directed to the polymerization reaction of the association monomer 85552 -14- 200426156. In the other embodiment, the method is directed to the copolymerization reaction of at least two different olefin monomers. In a specific embodiment, the method is a copolymerization reaction of an olefin monomer and a diene monomer. In another embodiment, this method is directed to the copolymerization of at least two different fluorene monomers and diene monomers. In the other case, "Zwo" with eye shells, this method is for the copolymerization reaction of alkaloid early body and at least two different N-associated early body. In another eight-body embodiment, This method is a combination of two different smoke-associated monomer spots V and two different diammonium monomers ?, ^ z, / a. In another specific embodiment

This method is aimed at the copolymerization of the olefin iU cloth and the polar ethylenic monomer. In another specific implementation, the detection of γ-inhibition is based on the reaction of at least two different edging progenitors and polar acetamidine monomers. In another item, Jinyu Λ, this method is aimed at the copolymerization of olefin monomers and 5 # 2 associative monomers. ^ Different types of oblique sweeteners of different polarities. "[In another-specific embodiment This method, ... · The copolymerization reaction of ten to y two different fluorene hydrocarbon monomers with αα king / rain species of ethyl green xuan early body with different polarities. "丄 生生 / 布 系 在-Specific embodiment, This method is another one and touches the reference: 〇 Shan Yi association foot permanent closure reaction. In the other I &gt; 7 &gt; &lt; Yong3 reaction. In the renter's example, this method involves the co-polymerization of propylene, propylene and propylene. In another specific embodiment, Bu Bingkou Xi A takes this person. This method is aimed at the vinyl toilet Ding Jiao] ~ K reaction. In another specific-cloth-埽 and hexene-丨 the industry narrow people good @ h This Wanfa system is directed to the total reaction of the two groups. In another item, it is aimed at the copolymerization of propylene and mi. That is, this method is used in the method of the present invention—or multiple radical-catalyst catalysts—anionic catalysts, coordination = and may include butyrene catalysts, cationic 85552-15-200426156 sexual catalysts, and a Catalysts, which include transition metal components or metal alkadiene fluorene components, including single or multiple cyclopentadienyl components, and react with either metal alkyl, metal alkoxy, or anionic compound components. This catalyst may comprise one or more precursor compositions that are partially or fully activated. This catalyst may be modified by pre-polymerization to form a pre-polymer, which can be coated or carried on a machine or an organic support. As used herein, the term "catalyst" includes elements or compounds that may also be referred to as catalysts in this art. The term &quot; catalyst &quot; as used herein includes multiple components that can constitute a catalyst system, such as activators, solvents, and carriers. In particular, conventional catalysts can be of the Ziegler-Natta type, This technique is known to include solid catalysts, transition metal compounds, and co-catalysts, including organic compounds of metals, such as organometallic compounds, such as alkyl aluminum compounds. Ziegers supported on silicone can also be used. Le catalysts. In addition, 'conventional catalysts can be highly active catalyst types, meaning those who can manufacture a large amount of polymer in a relatively short time, thus making it possible to avoid removing catalyst residues from the polymer. Known high Active catalysts include solid metal catalysts containing transition metals, money, and halogen atoms. Conventional high-activity catalysts can also be used, which contain chromium oxide, which is activated by heat treatment and combined with a granular support based on refractory oxides. .Can also use metal alkadiene catalyst and metal alkadiene catalyst supported on silicone. The catalyst can be added in solid, slurry or solution. The catalyst can be gas, liquid, water , Or a mixture of gas and liquid, delivered to the reactor. If any of the catalysts or catalyst components used are sensitive to oxygen, moisture and / or air, the catalysts and / or components are stored in a conventional manner in In its storage tank, it is covered with an inert gas, such as nitrogen or argon, relative to the stored 85552 '16-200426156. In practice, the height of the catalyst added to the reactor can be changed to reduce the inflammatory zone. The amount of fine powder in the circulating stream. You 1 4 &gt; For example, adding a catalyst below the reactor can reduce the transfer of fine powder. In a specific embodiment, the catalyst used in the ethylene polymerization reaction It is a Ziegler-Natta type catalyst that includes σ-chlorinated 'and aluminum-based aluminum. In another embodiment, it is used as a catalyst for the copolymerization reaction of acetylene and butylene]: The system is a Ziegler-Natta type catalyst containing thorium trichloride and calcined indium. The operating temperature of the reaction bed is set and controlled at a temperature lower than the adhesion of the polymer particles or This is important, for example, to prevent the reactor from being polymerized. Objects or flakes are clogged and can grow quickly if the controlled reactor bed temperature reaches an excess. Controlled (Reactor bed temperature can be measured using any conventional method, such as using at least 'thermometers, * f Λ. Τ ^ Private couple thermistor or platinum resistance thermometer. The controlled reactor bed temperature can be controlled by any conventional method, such as by controlling the cooling capacity of the condenser, such as by adjusting the cooling water flow rate of the condenser, In order to: ask the response to the entrance of the stupid body, ask for the amount of one or more condensing agents in the circulating flow. Figure 2 shows a non-limiting schematic diagram, which is simplified from Figure 1. The point is that some components have been slightly "indicated" to indicate the typical other degree and pressure I position β of the fluidized-bed reactor polymerization device of the present invention. Of course, many other variations can be implemented without departing from the spirit or scope of the present invention. As a rule, the controlled reactor bed temperature is measured in a part of the fluidized bed that is removed from the distribution plate. Relative to the size indicated by ▼ in Figure 2a, which means starting at the surface of the distribution plate, such as 32, 85552 • 17- 200426156 in I, facing the fluidized bed and extending to the top of the reaction zone 2 of the reaction tower, This means that before entering the expansion zone 4 of the reaction tower, the measured reactor bed temperature is measured above the surface of the distribution plate facing the fluidized bed at a height greater than or equal to about 0.17Q. In another embodiment, the controlled reactor bed temperature is measured at a location that is greater than or equal to about 0.17Q and lower than or equal to about 0.6Q. In another embodiment, the controlled reactor bed temperature is measured at a location greater than or equal to about 0.33Q and lower than or equal to about 0.55Q. In another embodiment, the controlled reactor bed temperature is measured at a location greater than or equal to about 0.33Q and lower than or equal to about 0.48Q. In another embodiment, the controlled reactor bed temperature is measured at a location greater than or equal to about 0.18Q and lower than or equal to about 0.25Q. In a specific embodiment, Q is about 13.6 meters. In another embodiment, Q is about 16.64 meters. In another embodiment, Q is about 21.0 meters. In another specific embodiment, as shown in FIG. 2a, when Q is about 16.64 meters, the controlled reactor bed temperature is about 7.27 meters (about 0.44Q) above the surface of the distribution plate 32 facing the fluidized bed. Measures south. Controlling the reactor bed temperature is important to provide process continuity. Process continuity may be harmed or even lost, for example due to the formation of polymer lumps. If the temperature of the controlled reactor bed is too high, this type of block can grow rapidly by cohesion through polymer particle cohesion. If the polymer mass grows too large to be detached from the reactor, then as the microparticle polymerization product passes through the PDS, it may clog the reactor and cause loss of the continuity of the method. On the other hand, if polymer lumps enter the PDS, such lumps can disrupt the function of the system and / or its components, such as dryers, -18- 85552 200426156 extruder or transfer line, and so on The continuity of this method is adversely impacted. Controlling the temperature of the reactor fluidized bed is directly determined by three main factors: the rate of catalyst injection, (2) the reactor inlet temperature of the gas stream that is introduced or recycled to the reaction zone, and (3 The mass flow rate of the gas flow through the fluidized bed is, of course, equal to the surface gas velocity (nSGV &quot;) multiplied by the internal cross-sectional area of the reactor and multiplied by the recirculated gas density. SGV—Generally in the range of about 0.12 to about 2.44 meters / second. In a specific embodiment, the SGV is about 0.21 to about 1.8 meters / second. In another specific embodiment, the SGV is about 0.65 to about 0.90 m / s. In another embodiment, the minimum speed required for SGV minus fluidization is greater than about 0.09 m / s. In another embodiment, the SGV minus the minimum fluidization speed is greater than about 0.21 m / s. In another embodiment, the minimum fluidization speed minus SGV is greater than about 0.275 m / s. In another embodiment, the ratio of SGV to the minimum fluidization speed is about 2 to about 20. In another embodiment, the ratio of SGV to the minimum fluidization speed is about 3 to about 10. -Of course, the amount of liquid introduced into the bed, whether accompanied by a circulating stream and / or through individual direct feed streams, into the fluidized bed can also indirectly affect the bed temperature of the controlled reactor, because when the heat When it is removed from the fluidized bed to vaporize the incoming liquid, its vaporization is used to reduce the temperature of the controlled reactor bed. The rate of catalyst injection is generally controlled by the rate of polymerization. Since this polymerization reaction is exothermic, the polymerization rate controls the rate of heat generation. The temperature of the reactor fluidized bed is controlled to a substantially isothermal level by continuously removing the heat generated by the polymerization reaction under stable operating conditions. The stable operating state includes the operating state of the polymerization method, in which the main factor of the system is 85552 -19- 200426156, which has not changed substantially, after a reasonable period of time, such as at least about one hour. Therefore, 'in a stable operating state, the heat generated by the polymerization reaction is balanced by the heat removed by cooling, and the total amount of material introduced or recycled into the system is removed by It is balanced by the amount of microparticle polymerization products. In a specific embodiment of the manufacture of polyethylene from ethylene, the controlled reactor bed temperature is from about 10 to about 115. (:. In another specific embodiment of the production of polyethylene, the controlled reactor bed temperature is about 105. (: to about ii (TC. In the production of polyethylene and Ding Hui r -1 poly ( In a specific embodiment of ethylene-co-butene_1), the controlled reactor bed temperature is about 8 (TC to about 95. (:.) In the manufacture of poly (ethylene-co-butene-1) In another specific embodiment, the controlled reactor bed temperature is about 80 C to about 90 C. In another specific embodiment for manufacturing poly (ethylene-co-butadiene), the controlled reactor The bed temperature is about 85. (: to about 89t :. In another specific embodiment for manufacturing poly (acetyl-co-butyrene-1), the controlled reactor bed temperature is about 85 ° C to About 88 ° C. In a specific embodiment of making poly (ethylene_co-hexene4) from ethylene and hexene-1, the controlled reaction is a bed temperature of about 78 ° C to about 90 ° C In another specific embodiment of the manufacture of poly (ethylene-co-hexane) _1, the controlled reactor bed temperature is about 100 ° C to about 110 ° C. Many polymers and copolymers can use this Invented by the method of the invention. The &quot; copolymer &quot; Polymers with the same monomeric subunits. Therefore, containing three different monomers, the silicon polymer chains (also known as trimerization) are included in the "copolymer" -word, which contains more than The same is true of three different polymer chains. The term &quot; polymer &quot; as used herein includes 85552 '20-200426156 homopolymers and copolymers. Bis: A polymer containing a series of asymmetric carbon atoms For example, polypropylene or water saccharin is known to exist in different stereoregular forms. For example, 'if the polymer chain exists in a fully elongated planar shape «, then it is formed ... Substituents (&quot; for polyacrylamide, and poly (phenylene) for phenyl) are above or below the plane of the main chain, which is referred to as the same row, when adjacent groups of two units are replaced. When it is above and below, it is called opposite row, when two adjacent substituents are on the plane, and the next-phase Zheng group (&quot; triad group) is below, and vice versa. Is referred to as a heterodyne '@ when the substituents are randomly above and below this plane At the same time, the system is called disorderly. See 'for example, 〇—〇—' Heji shoulder, McGmw-Hill, New York, 1970, pages 522_523, 538_541. For example, for polypropylene, in-line polypropylene system Described in, for example, U.S. Patent No. 5 (column 3, column 2 to line 6, column 3 (and in the references cited in 4 therein)), and polypropene is described in, for example, US patent 5,269,8. 7th column i lines 18-21 and 53-67 (and in the patents cited therein), and the heteropolypropylene is described in, for example, RA. University Press, New York, 1972, pp. 55, 132-141, and 158 (and in the references cited therein) and U.S. Patent 4,557,264. As used herein, the term &quot; polymer &quot; includes all three-dimensional regular forms of the polymer, such as side-by-side, side-by-side, miscellaneous, and random. In a specific embodiment, the polymerization product of the present invention is an in-row, an opposite-row, or a-row. In another specific embodiment, the polymerization products of the present invention are in the same row, meaning that they contain at least 94 mole% of the same three-unit group. In another embodiment with 85552 • 21 · 200426156, the system was originally arranged in the Mingshi, and the system containing Mo di-binary Γ was essentially in the same row, which means that the polymerization product of the present invention is included: Row II Two other: item specific implementation finance, three unit group. In the other example of "... two packs" with less than 94 Mo candle rows, the polymer product of the present invention is another province and contains at least 85 mol% of anti-row three-unit groups. In the spoon; ~, fla: r embodiment, the polymer product of the present invention is a miscellaneous row, that is, the tone contains at least 94 mole% impurity-that is, the polymer of the present invention is produced in another specific embodiment. Row of three units. Miscellaneous row, which means that it contains at least 85 moles or τ. The polymerization product is in the same row, and the opposite row is in the same row. The method is "Shuikou production;" in another specific embodiment. , This

: Product: It is substantially in-line. In another specific embodiment, I Maomingyan Yonghe product is a pair of polypropenes. In another specific embodiment, the 'polymerization product of the present invention is essentially a polypropene polymer. In another case, the polymerized product of the present invention is a heteropoly polypropylene. In another specific implementation example of item I, Tai Pian ^ BE1, &lt; This hair month <The coupling product is substantially heterogeneous polypropylene. In a specific embodiment, the polymerization product of the present invention is in-line, counter-line or travel-line acetoacetam. In another specific embodiment, the polymerization product of the present invention: is an in-line polystyrene. In another specific embodiment, the product of the present invention is negative-negative upper-row phenylethylamidine. In another specific embodiment = the polymerization product of the present invention is p-phenylene. In another specific example, see her example, the polymerized product of the present invention is essentially paraphenylene. 85552 '22-200426156 In another embodiment, the polymerization product of the present invention is a heteropolymer polystyrene. In another embodiment, the polymer product of the present invention is heteropoly polystyrene. Examples of the types of polymers that can be made using the method of the present invention include polyolefins and olefins, which can be conjugated or non-conjugated, poly (ethylene monomers), poly (polar ethylene monomers) ) 'And poly light class. As used herein, &quot; polyolefin &quot; is a polymer or a copolymer comprising an olefin monomer. Exemplary polyalkylene hydrocarbons include polymers and copolymers such as Greek, propylene, butene, pentylene-methyl-4-methylpentane, hexamethylene, heptyl-1, n-ene, and the like. Copolymers can be formed using many methods known to those skilled in the art, for example, by the polymerization of two or more different monomers. This copolymerization can be of the rule-of-law type, alternating type, or somewhere in between. When the end of the polymer chain growing from any monomer unit has approximately the same priority for the addition of any monomer, the copolymer is conventionally referred to as, "regular" or "ideal" However, when the end-stopping species of the polymer chain in the growth earlier added the group to another monomer, it was called &quot; alternative &quot;. See, for example, F.W.BillmeyeUr., Ju々 # # ㈣ 以, 2nd edition,

Wiley-Interscience, New York, 1971, pp. 330-331. In a specific embodiment, the copolymerization product of the present invention is a random copolymer. In another specific embodiment, the 'copolymerization product of the present invention is a regular copolymer of classical quality, and t is a copolymerization reaction by which a copolymerization product is formed.' In terms of characteristics, it is better than an alternating polymerization reaction. Examples of the types of copolymers that can be used in the method of the present invention, such as poly (associated smoke_ 85552 -23- 200426156 co-diene), poly (olefin-co- (acetylene monomer) ), Poly (fluorene_co- (polar ethylenic monomer)), poly (fluorene-co-aldehyde), poly ((polar vinyl monomer) · co-diene), poly ((polar vinyl Monomers) -co- (acetylene monomers)), poly ((polar ethylammonium monomers-co-jun), poly (diene_co_ (decisive monomer)), poly (diasso_ Co-compliance) and poly ((acetylene monomer) -co-aldehyde). It should be understood that, for each of the above-exemplified types of copolymers, of course, each monomer type can, of course, be independently and in a variety of specific monomer forms Exist. Only used as an example is the copolymer type, poly (associated hydrocarbon_co-diene)) f ', this copolymer type may include poly (acetylene_co-butadiene), polypinene_copolymer -1,4-hexadiene), poly (butene-co-butadiene), poly (butene-co-], hexadecadiene), poly (acetamidine-co-butadiene-co-butadiene ）), Ju (Yi_Gong_ 丁 _ 卜#_Hexadiene), poly (acetamidine-co-butadiene-copolymer from hexamethylene dioxin, polyisobutadiene-butadiene · co-1,4-hexadiene), and poly (acetamidine-co- Butadiene-co-butadiene-co], pre-hexadiene), only a few are mentioned. σ Exemplary polymers made using the Benmemin method include polyethylene, polypropylene, kimu (butane 1), poly (pentene)), poly (4-methylpentamidine), poly (hexene) ”): Poly (heptane, · 1), poly (xin association)), polybutadiene, polyisoprene, polychloroprene-ene, Yong (1,3-pentafluorene), polycyclopentadiene Women, poly (M-hexane), poly (sub: 4) polyethylene block, poly (methylacetylene), poly (ethylacetylene), polyethylene (*) ), Poly (p-methyl styrene), poly (Nakasuka) ▲ (Ethyl Acetate), poly (Ethyl Acrylate), poly (Ethyl Methyl Propionate), Poly (Chloroacetylene), poly (fluoroethylen), poly (f-ethylenyl ether), poly (methyl acrylate), ye, yong (methyl acrylic acid), polytetrafluoroethylene, poly Propylene such as, polyoxymethylene, and polyacetaldehyde. In a specific embodiment, the polymer product made using the method of the present invention is 85552 -24- 1 ^ 0 is polyethylene. Tool &quot; Performance Example towels' made using the method of the present invention can be used by the present invention, + Examples of copolymers are m species of other hydrocarbon-associated monomers, including ethylene and at least one methyl group, such monomers such as propylene and butyl.缔 定 ^ ¥ Phenylethylbenzene, p-methylbenzylethylbenzene_Buxindi, Buphenylethylene, "The basic cloth and n-berene of base furnace sheet r; Propylene and at least one other kind of pentylbenzene -1, hexamethylene-i, heptylamine, methyl, 料 田 苴 #. Octyl ethylene 'methyl styrene terylene ethyl ether and n-diethylbenzene; butylene-1 and at least one other olefin mono-K copolymer 'The alkane monomers are, for example, pentamidine, 4-f-methylpentene, -1, anisocyanate-1, octyl-benzophenone, α-methylacetophenone, p-f-phenylethylethene, and The old woman; the second woman, the proprietor and at least one other polymer of the tobacco-associating monomers, such as the tobacco-associating monomers such as Ding Yixin 4_methylpentane Styrene, α-methylstyrene, p-methylstyrene, and n-stilene; copolymers of ethylene, butene, and at least one other olefin monomer, such as alkene monomers such as 4 · Methylpentamidine] m, heptene_, octyl ^, styrene, ... methylphenylethylidene, p-methyl Acetylene and n-Suzu; copolymers of propylene, butene-1, and at least one other olefin monomer, such as 4-methylpentamidine-1, hexene-1, heptene-1, octene _ 丨, styrene, chloromethylstyrene, p-methylstyrene, and n-formazan; co-ice of ethylene and at least one diene '# 海》 —Women can be shared or non-shared vehicles, such as Ding Diphenyl, pentadiene, chloroprene, 1,3-pentadiene, cyclopentadiene, hexadecadiene, and ethylene n-saccharine; copolymers of propylene and at least one diene The diene may be conjugated or non-conjugated, such as butadiene, isoprene, gas butadiene, 3-penta 85552 -25- 200426156 :, cyclopentadiene, hexamethylenediamine, and Ethylene n-cyclopentadiene; a copolymer of butene and at least one species of Greek, the difluorene may be common or non-fluorene, such as butadiene: isoprene, chloroprene, u_pentene Diene, cyclopentadiene, I'hexadiene, and ethylene are -enes; copolymers of ethene, propylene, and at least one diene, and the diene can be conjugated or non-common, such as butadiene Ene, isoprene, chloroprene, 1,3-pentadiene , 5 袤 pentadiene, M • hexamethylene diene and ethylene: n-saccharene; copolymer of ethylene, butene 4 and at least one difluorene; the di-association; conjugated or non-conjugated, such as butadiene , Isoprene, chloroprene, D. pentadiene,% pentadiene, 丨 hexadiene and ethylene n-sulphonate; propylene, butene-1 and at least one di-copolymer The di-association may be conjugated or non-conjugated, such as butadiene, xylprene, chloroprene, 3-pentadiene, cyclopentadiene, hexamethylene, and ethylene A copolymer of acetylene and at least one acetylene monomer, such as acetylene, methylacetylene, and ethylacetylene; a copolymer of propane and at least one acetylene monomer, such as acetylene monomer Acetylene, methylacetylene, and ethylacetylene; copolymers of butene 4 and at least one ethylenic monomer, such as acetylene, methylacetylene, and ethylacetylene; ethylene, propylene, and at least one acetylene Copolymers of acetylene monomers such as acetylene, methyl ethyl block, and ethyl ethyl acetate: ethylene, butylene, and at least one of ethyl monomer Polymer, the acetylene monomer such as acetylene, methylacetylene, and ethylacetylene; copolymer of propane, butene 4 and at least one acetylene monomer 'the acetylene monomer such as acetylene, methylacetylene And ethyl acetylene; a copolymer of ethylene and at least one polar acetamidine monomer, such as vinyl acetate, acetamyl acrylate, acetamyl methacrylate, chloroacetamidine, vinyl fluoride, Methyl ethyl ether, methyl acrylate, methyl methacrylate / 85552 -26- 200426156, tetrafluoroethylene and propionitrile; copolymers of propylene and at least one polar ethyl acetate monomer, such as vinyl acetate , Vinyl propionate, vinyl methyl propionate, vinyl chloride, vinyl fluoride, methyl vinyl ether, methyl acrylate, methyl methacrylate, tetrafluoroethylene and acrylonitrile; butene-1 and at least A copolymer of a polar vinyl monomer such as ethyl acetate, vinyl acrylate, vinyl methacrylate, vinyl chloride, vinyl fluoride, methyl vinyl ether, methyl acrylate, methacrylic acid Methyl Ester, Tetrafluoroethylene and Propylene A copolymer of ethylene, propylene, and at least one polar vinyl-based monomer, such as ethyl acetate, such as vinyl acetate, vinyl acrylate, methacrylic acid, ethyl acetate, ethyl acetate, fluoroethylene, methyl ethylene Copolymers of methyl ether, methyl acrylate, methyl methacrylate, tetrafluoroethylene and propionitrile; copolymers of ethylene, butene, and at least one polar vinyl monomer, such as ethyl acetate , Vinyl acrylate, methyl ethyl propionate, ethyl chloroacetate, vinyl fluoride, methyl ethyl ether, methyl propionate, methyl methyl propionate, tetrafluoroacetic acid and propionitrile ; Copolymer of propylene, butylene 4 and at least one polar ethylenic monomer, such as vinyl acetate, vinyl propionate, vinyl methacrylate, vinyl chloride, ethyl acetate, methyl Acetyl ether, methyl malonate, methyl methylpropionate, tetramethylene, and acrylonitrile; copolymers of acetam and at least one aldehyde monomer such as formaldehyde and acetaldehyde Copolymer of at least one aldehyde monomer, such as formaldehyde and acetaldehyde butyrate 1 and ) A copolymer of aldehyde monomers such as copolymers of formaldehyde and acetaldehyde 'ethylene, propylene and at least one aldehyde monomer, #aldehyde monomers such as formaldehyde and acetaldehyde; ethylene ^ butene-1 and at least A copolymer of aldehyde monomers, such as formic acid, acetic acid, acetic acid, and allyl, butan-1 and at least one aldehyde monomer 85552 -27- 200426156 copolymer 'the aldehyde monomer Such as formaldehyde and acetaldehyde. In the specific embodiment, the copolymer is made of poly (ethylene-co-propaneamidine). In ,, water. House property, the above specific embodiment, using the ugly manpower made by Taiyiming Wanfa "quotation of this hair into" </, Hehe products are clustered and struggling, A ,,,丄 々 ~ -1). In the other--,-, examples, the copolymerization product made using the present poly (ethylene ugly ..., Fayue Wanfa is Yong W / Greek-co-hexene. In the other and touch, ^ 女In the case of 丄 / 、, and other examples, the copolymerization product A made by using the method of the present invention is A, taking A as yong (ethylene-co-heptyl-υ. In another example of Qiba Qiguan, Using the method of the present invention, the method of preparing the copolymerization product is poly (ethylene, co-octene). In another example, the present invention is used. The copolymerized product obtained by the method is poly (propylene-co-butadiene-1). In another embodiment, the copolymerized product made by the method of the present invention is poly (called co-hexanone). -丨). In another specific embodiment, the copolymerization product using the method of the present invention is poly (propyl-co-heptane.) In another specific embodiment, the copolymerization product is made using the method of the present invention. The copolymerization product is poly (propyl hydrazine-co-synthesis-1). In a specific embodiment, the polymer or copolymerization product of the present invention made of a conventional Ziegler-Natta catalyst is used. by ASTM Method D1238 Revised B_90 'The standard test method for the flow rate of thermoplastics by extruding a plastic meter' at 190 C 'using condition E and a weight of 2.16 kg (&quot; ASTM D1238 ,,) Melt index ("MΓ") is about 0.1 g / 10 minutes to about 150 g / 10 minutes, preferably about 0.3 g / 10 minutes to about 75 g / 10 minutes, and more preferably about 0.5 g / 10 minutes to About 60 g / 10 minutes. In a specific embodiment, the polymer or copolymer product of the present invention, when subjected to ASTM method D4883-99, is entitled "Polyethylene Density by Ultrasound Technology 85552 -28- 200426156 standard test method, when measured using a TECRAD ultrasonic device ("ASTM D4883"), has a density of about 0.900 g / cm3 to about 1.100 g / cm3, preferably about 0.905 g / cm3 to about 1.000 grams / cubic centimeter, more preferably about 0.910 grams / cubic centimeter to about 0.980 grams / cubic centimeter. In a specific embodiment, the polymer or copolymerization product is selected from the group having a MI by ASTMD 1238 of about 5.0 to About 10.0 g / 10 minutes, and density by ASTM D4883 About 0.950 to about 0.975 grams per cubic centimeter of resin. In another embodiment, the polymer or copolymerization product is selected from the group having a MI by ASTM D1238 of about 4.0 to about 9.0 grams per 10 minutes, and borrowed from A resin having a density of about 0.935 to about 0.965 grams per cubic centimeter from ASTM D4883. In another embodiment, the polymer or copolymerization product is selected from those having a MI of about 1.5 to about 5.0 grams by ASTM D1238. / 10 minutes, and resin having a density of about 0.900 to about 0.935 g / cm3 by ASTM D4883. In another embodiment, the polymer or copolymerization product is selected from the group having a MI by ASTM D1238 of about 0.1 to about 1.5 grams / 10 minutes, and a density of about 0.900 to about 0.935 grams by ASTM D4883. / Cubic centimeter of resin. In another specific embodiment, the polymer or copolymerization product is selected from the group having a MI by ASTM D1238 of about 0.5 to about 2.0 grams / 10 minutes, and a density of about 0.900 to about 0.935 grams by ASTM D4883. / Cubic centimeter of resin. In another embodiment, the polymer or copolymerization product is selected from having a MI of about 1.0 to about 3.5 g / 10 minutes by ASTM D1238 and a density of about 0.900 to about 0.935 g by ASTM D4883 / Cubic centimeter of resin. In another embodiment, the polymer or copolymerization product is selected from the group having a MI of about 10.0 to about 35.0 g / 10 minutes by ASTM D1238 and a density of about 85552 -29- 200426156 ASTM D4883. 0.910 to about 0.945 g / cm3 of resin. In another specific embodiment, the polymer or copolymerization product is selected from the group having a MI of about 30.0 to about 70.0 g / 10 minutes by ASTM D1238 and a density of about 0.910 to about 0.945 g by ASTM D4883 / Cubic centimeter of resin. In another specific embodiment, the polymer or copolymerization product is selected from the group having a MI by ASTM D1238 of about 0.5 to about 2.0 grams / 10 minutes, and a density of about 0.900 to about 0.935 grams by ASTM D4883. / Cubic centimeter of resin. In another specific embodiment, the polymer or copolymerization product is selected from so-called film grade `` resins, having a MI by ASTM D1238 of about 0.01 to about 5.0 g / 10 minutes, and a density by ASTM D4883 About 0.900 to about 0.930 g / cm3, so-called π-molded grade "resin, having a MI of about 0.1 to about 150 g / 10 minutes, and a density of about 0.920 to about 0.939 g / cm3, and so-called" high density " The π resin has a MI of about 0.01 to about 70 g / 10 minutes and a density of about 0.940 to about 0.970 g / cm3. In another specific embodiment, the polymer or copolymerization product is selected from a film-grade resin having a MI of ASTM D1238 of about 0.5 to about 5.0 g / 10 minutes, and a density of about 0.900 by ASTM D4883. To about 0.930 g / cm3, a mold-grade resin having an MI of 4.0 to about 150 g / 10 min, and a density of about 0.920 to about 0.939 g / cm3, and a high-density resin having a MI of about 2.0 to about 70 g / 10 minutes and a density of about 0.940 to about 0.970 g / cm3. At start-up, the conventional system is used to load the existing polymer particles into the reactor before the circulating stream begins to flow. These existing polymer particles may advantageously be similar to the new microparticle polymerization product to be made. However, and especially if the existing poly -30- 85552

The composite particles are different and the newly formed micro-particles: The combined particles usually do not pollute the latter. To increase cooling capacity,

And by increasing the production rate of the polymerization reactor, a dew point temperature of the mixture is circulated to allow a larger amount of heat 2. The dew point of the circulating stream can be increased by increasing the percentage of the circulating mixture 吆, and at the same time reducing the non-condensable gas by 100%. For example, the methods disclosed in US Pat. Nos. 4,543,399 and 4,588,790 are used to introduce condensing agents into the recirculation mix, For example, in FIG. 1, after the compressor 26 and before the condenser 28, the source 44 passes through the line 16. Therefore, in Figure w, the condensing agent enters the melonization bed through line 8. However, as is known in the art, the condensing agent can be introduced into the reactor / recycling system by any method and at any suitable location in the system. For example, U.S. Patent No. 6,001,93 issued to Chinh et al., Yang Shi first separated a part of the liquid from the recirculated gas, and then directly fed the mud through the individual, for example, as shown in Figure 1 by line 8A This liquid is introduced to a specific location in the fluidized bed. In a specific embodiment, the condensing agent may be consistently inert with respect to the catalyst, monomer, and polymerization products. In an alternative embodiment, the condensing agent may include monomers and / or comonomers. As used herein, the term "condensing agent" includes burners and olefins. Condensants that can be used are selected from burners and olefins containing 3 to 8 carbon atoms. Alkanes that can be used as condensants include Propane, n-butane, butane, n-pentane, isopentane, neopentane, n-hexane, isohexane and 85552 • 31- 200426156 Other saturated C: 6 hydrocarbons, n-heptane and Other saturated C: 7 蛵, n-octane and other saturated cs hydrocarbons, and mixtures of these alkanes. Alkenes which can be used as condensing agents, including butene-2, pentene-2, pentamidine-3 And other unsaturated c5 hydrocarbons, hexene, ene-2, hexene-3 and other unsaturated Q hydrocarbons, heptene-2, heptene, heptene-4 and other unsaturated C7 hydrocarbons, octane_2, _3, Xin_4, and others: Saturated Q hydrocarbons, and mixtures of these women. Contains at least one mixture of at least one ene and at least one olefin, and can also be used as a condensing agent. The condensing agent may include polymerizable rhenium Hydrocarbon monomers, such as fumes, especially fumes :: enes, especially those containing at least one ridge carbon double bond, and mixtures thereof, including some of the aforementioned monomers, combined In Example 1, when polypropylene is produced, Γ, or a polymerization agent and a monomer are completely incorporated. In another example, when Γ is used as condensation, in the case of d r κ, when poly (propylene-co-butyl) is produced,晞 寺 丁 少 ▼ ―1 monomer can be used as a condensing agent. ^ M ^ ^ ^ ^ ^ ^ c3 ^ ^ One application two Φ '", the condensing agent contains at least-one kind of Q alkane. In the other-and moon beans In the example, the condensing agent includes at least one embodiment. In another embodiment, the condensing agent includes at least one kind of :: In another specific embodiment, the condensing agent is “at least one kind of C 6 yuan. In another embodiment, the condensing agent includes At least one kind of 7; °. In another embodiment, the agent contains at least 8: #In another embodiment, the condensation sword contains at least one kind of C4 burn or tincture contains at least one kind of 05 burn or tin The agent contains at least one C6 alkane or olefin. The agent contains at least one alkane or 埽 C3 虼 or ene. In another specific embodiment, it is condensed in another specific embodiment and cooled in another specific embodiment. , Colder than another specific embodiment, colder than another specific embodiment, cold 85552 -32- 200426156, the condensing agent contains at least one alkane Orene

The agent comprises at least one alkane or amidine, and the agent comprises at least one C: 8 alkane or hydrogen. In a specific embodiment,, has about 114 g / mo jp. a TS-Guandou is another concrete, a kind of alkane, and has a molecular weight of about 42 P. In another embodiment, the condensation has a molecular weight of about 42 g / mole to about 86 g / mole. As is known in the art, a variety of condensing agents can be used. For example, isopentane may be present in an amount such that it does not cause the substantial particulate polymer product to be sticky, and propane may also be present to increase the achievable condensation and increase the thermal capacity of the recycled mixture. In another specific embodiment, the condensing agent comprises a mixture of at least one species of rhenium and at least one C4 alkane. In another embodiment, the condensing agent comprises a mixture of at least one C4 alkane and at least one c5 alkane. In another embodiment, the condensing agent comprises a mixture of at least one C5 alkane and at least one C6 alkane. In another specific embodiment, the condensing agent comprises a mixture of at least one C; 4-carbon, at least one C: 5 alkane, and at least one c6 alkane. In another embodiment, the condensing agent comprises a mixture of at least one C6 alkane and at least one C: 7 alkane. In another embodiment, the condensing agent comprises a mixture of at least one q-alkane and at least one Q-alkane. In another specific embodiment, the condensing agent comprises a mixture of at least one C3 gram and at least one c5 burn. In another embodiment, the condensing agent comprises a mixture of at least one C4 alkane and at least about 96 mole% of at least one c5 alkane. In another embodiment, the condensing agent comprises a mixture of at least about 96 mole% of at least a C5 alkane and at least 85552 -33-200426156-a c6 alkane. In another specific embodiment, the condensing agent contains at least one species of pinane and at least about 96 mole%. Alkane and at least: species &lt;: 6 burnt mixture I in another-specific embodiment, the condensing agent contains at least-a kind of Q burn and at least about 99 mol% at least, the burnt mixture is two more than another-specific In the embodiment, the 'condensing agent contains at least about 99 mol% of at least-a mixture with at least-red scorch. In another embodiment, the' condensing agent contains at least one. 4. A mixture of at least -species and at least about -6 moles of at least about 99 mole%. In another embodiment, the condensing agent comprises a mixture of at least one C: 4 alkane and at least about 997 mole% of at least one C5 alkane. In another embodiment, the condensing agent comprises at least about 99.7 mole% of a mixture of at least one C5 fired and at least one C6 垸. In another embodiment, the condensing agent comprises a mixture of at least one pinane, at least about 99.7 mole% of at least one Q-alkane, and at least one Q-alkane. In another specific embodiment, the condensing agent comprises a mixture of at least one trioxane and at least about 99 mole% of isopentane, neopentane, n-pentane and mixtures thereof in another specific embodiment Medium 'condensing agent comprises a mixture of at least one c6 垸 and at least about 99 mole% isopentane, neopentane, n-pentane, and mixtures thereof. In another embodiment, the condensing agent comprises a mixture of at least one C4 stage, at least one C6 alkane, and at least about 99 mole% isopentane, neopentane, n-pentamidine, and mixtures thereof. In another embodiment, the condensing agent comprises a mixture of at least one c4 alkane and at least about 99.7 mol% isopentane, neopentane, n-pentane, and mixtures thereof. In another embodiment, the condensing agent comprises a mixture of at least one C6 alkane and at least about 99.7 mole% isopentane, neopentane, n-pentane, and a mixture thereof 85552 -34- 200426156. In another embodiment, the condensing agent comprises a mixture of at least one C4 alkane, at least one C6 alkane, and at least about 99.7 mol% isopentane, neopentyl, n-pentamidine, and mixtures thereof. In another specific embodiment, when the monomer comprises ethylene, the condensing agent is selected from the group consisting of n-butane, isobutane, n-pentane, isoamyl, n-hexane, n-heptane, and Its mixture. In another specific embodiment, when the monomer comprises propylene, the condensing agent is propylene. Conventionally, the dew point or dew point temperature of a gas is the temperature at which the gas is saturated with the condensable components. Therefore, when the gas is cooled, the dew point temperature of the gas is the temperature at which the liquid condensate begins to form in the gaseous part. Similarly, after cooling the circulating flow, for example, using the condenser 28 in FIG. 1 and passing through the line 8 to enter the fluidized bed reactor 2 in FIG. 1, the dew point temperature is the gaseous part of the liquid condensate starting in the circulating flow. Formation temperature. It is generally known that the temperature of the circulating stream, i.e. the reactor inlet temperature of the recycled mixture, can be reduced below the dew point temperature of the mixture. For example, it has been proven that V-, such as disclosed by Jenkins et al. In U.S. Patent Nos. 4,543,399 and 4,588,790, that the circulating stream can be cooled to a temperature lower than the dew point temperature of the fluidized bed polymerization process, thereby generating Condensation. The resulting liquid stream containing the liquid condensate can then be returned to the reactor without adverse effects on the fluidized bed, such as caused by the viscosity of the polymer product of the microparticles and / or the polymer particles cohesing by adhesion. The method of deliberately introducing a liquid condensing agent into the recycle mixture entering the reactor is a "condensation mode π" operation known in the art as a gas-phase fluidized-bed polymerization method. In a specific embodiment, the The difference between the controlled reactor bed temperature and the circulation of the mixture 85552 -35- 200426156 The dew point temperature is greater than or equal to about 5 ° C. In another specific embodiment, the controlled reactor bed temperature and the circulation of the mixture The difference between the dew point temperature is greater than or equal to about 10 ° C. In another specific embodiment, the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is greater than or equal to about 15 ° C. One or more condensing agents are present at a content that helps condense and form a liquid-containing recirculating mixture, and then introduces the mixture into the reaction zone of the reactor. Therefore, the fluidized bed reactor polymerization method of the present invention can "Condensation mode π operation. There may be an upper limit on the amount of liquid in the liquid-containing recirculating mixture, depending on the combination of the particular polymerization product and the condensing agent chosen. For example, when the polymerization product is less crystalline, such as poly (propyl-co-butane-1), a lower content of c5 alkane and / or ene condensing agent must be used compared to c4 burning and / or ene condensing agent. Compared with c3 alkanes and / or olefin condensing agents, lower levels of c4 alkanes and / or olefin condensing agents must be used. Therefore, for example, isopentane tends to become soluble and soften in a polymer product having less crystallinity, and therefore, less isoprene condensing agent must be used. On the other hand, even if propylene is present in a relatively high content, it does not specifically fall into poly (propylene-co- ·· tin-1). Because of this, propane does not significantly soften the copolymer, so it can be used at high concentrations in liquid-containing recycled mixtures and is introduced into fluidized bed reactors for the manufacture of poly (propylene-co-butyl Condensing agent for ene-1). In a specific embodiment, the liquid-containing mixture introduced or recycled into the reaction zone comprises from about 17.5% to about 70% by weight of liquid, based on the total weight of the circulating stream. In another specific embodiment, the liquid-containing mixture that is introduced or recirculated into the reaction zone 85552 -36- 200426156 contains about 20% to about 70% liquid by weight, based on the total weight of the circulating stream . In another embodiment, the liquid-containing mixture that is introduced or recycled into the reaction zone contains 21.8% to about 70% liquid by weight, based on the total weight of the circulating stream. In a specific embodiment of polyethylene made by Otome, the liquid-containing mixture that is introduced or recirculated into the reaction zone contains at least about 21.8% liquid by weight based on the total weight of the circulating stream. In another specific embodiment of the production of polyethylene glycol from ethyl acetate, the liquid-containing mixture introduced or recycled into the reaction zone contains 30% to about 70% liquid-to-weight ratio, based on the total weight of the circulating stream As a benchmark. In a specific embodiment of the production of poly (acetamidine-co-butene-1) from ethylene and butene-1, the liquid-containing mixture introduced or recycled into the reaction zone comprises 17.5% to about 40% liquid weight ratio, based on the total weight of the circulating flow. In a specific embodiment of the production of poly (ethylene-co-hexene-1) from ethylene and hexane-1, the liquid-containing mixture introduced or recycled into the reaction zone contains at least about 17.5% liquid The weight ratio is based on the total weight of the circulating flow. In another embodiment of the production of poly (ethylene-co-hexene-1) from ethylene and hexene-1, the liquid-containing mixture introduced or recycled into the reaction zone comprises at least about 20% The liquid weight ratio is based on the total weight of the circulating flow. The reactor inlet temperature, that is, the temperature of the gas flow that is introduced or recycled into the reaction zone, is measured conventionally in a gas collection chamber inside the bottom of the reaction tower, as shown below the distribution plate 32 shown in Fig. 2a. The reactor inlet temperature can be measured in any conventional way, for example using at least one thermometer, thermocouple, thermo-37- 85552 200426156 varistor or platinum resistance thermometer. In a specific embodiment, the reactor inlet temperature of the gas flow introduced or recycled into the reaction zone is about 10 ° C to about 60 ° C. In another embodiment, the reactor inlet temperature of the gas stream introduced or recycled into the reaction zone is about 20 ° C to about 55 ° C. In another specific embodiment, the reactor inlet temperature of the gas stream that is introduced or recycled into the reaction zone is about 25t to about 50 ° C. In another embodiment, the temperature of the reactor inlet containing the liquid mixture introduced or recirculated to the reaction zone is about 10 ° C to about 60 ° C. In another embodiment, the temperature of the reactor inlet containing the liquid mixture introduced or recirculated into the reaction zone is about 20 ° C to about 55 ° C. In another embodiment, the temperature of the reactor inlet containing the liquid mixture introduced or recycled into the reaction zone is about 25 ° C to about 50 ° C. Even in the stable operating state polymerization conditions, there will be a π temperature gradient region in a gas fluidized bed reactor, close to the bottom of the fluidized bed, in an area or layer extending upward from the distribution plate, for example, from the direction of fluidization The surface of the distribution plate of the bed enters the bed at a distance of about 102 mm to about 203 mm above the surface. This is due to the inlet temperature of the mixture that is introduced or recycled to the reactor, meaning the reactor inlet temperature and The temperature difference between the temperature of the controlled reactor bed. In the rest of the fluidized bed above the non-isothermal area below, the temperature of the fluidized bed is basically constant at the controlled reactor bed temperature. A plurality of temperature measurement devices, that is, a π measurement position nfl device, are located in the above-mentioned temperature gradient region of the reactor reaction zone 2. For example, FIG. 2 illustrates four such measurement position n devices, each located inside the reactor. At about 0.0091Q above the surface of the distribution plate facing the fluidized bed at 85552 -38- 200426156 (approximately 152 mm for Q = 16,64 mm) means that at measurement position 1, measurement position 2, measurement position 3 and There are 4 measuring positions. In order to provide uniformity in each temperature measuring position, and in a fluidized bed, to provide a flow "disturbance" near each device in each position (if included), each measuring position n device is located at The surface of the distribution plate facing the fluidized bed is substantially the same distance above and protrudes into the reactor at substantially the same size. In a specific embodiment, each measuring position η device is located in the reaction zone 2 of the reaction tower, and above the surface of the distribution plate facing the fluidized bed is greater than or equal to about 〇_〇〇66q and lower than or equal to about 0.022 Q. In another specific embodiment, each measuring position ^ means is located in the reaction zone 2 of the reaction tower, and above the surface of the distribution plate facing the fluidized bed is greater than or equal to about 0.0075Q and lower than or equal to about 0 · 〇 ι5ρ. In another specific embodiment, each measuring position η device is located above the surface of the distribution plate facing the fluidized bed in the reaction zone 2 of the reaction tower, which is greater than or equal to about 0.0088q and lower than or equal to about 0.013. Q. In a specific embodiment, q is about · 13.6 meters. In another embodiment, Q is about 16.64 meters. In another embodiment, Q is about 21.0 meters. In another specific embodiment, each measuring position η device is located in the reaction zone 2 of the reactor, and is about 52 mm above the surface of the distribution plate facing the fluidized bed, and has a length of about 13.6 meters. In another specific embodiment, each measuring position η device is located in the reaction zone 2 of the reactor, about 152 mm above the surface of the distribution plate facing the fluidized bed, and about 16.64 meters in length. In another specific embodiment, each measuring position η device is located in the reaction zone 2 of the reactor, about 152 mm above the surface of the split plate facing the fluidized bed, and about 21.0 meters in length 85552 -39- 200426156 . In another specific embodiment, each measuring position η device is located in the reaction zone 2 of the reactor, at a position about 102 mm above the surface of the distribution plate facing the fluidized bed, and a length of about 13.6 meters. In another specific embodiment, each measuring position η device is located in the reaction zone 2 of the reactor, at a position about 102 mm above the surface of the distribution plate facing the fluidized bed, and about 16.64 meters in length. In another specific embodiment, the devices at each measurement position 11 are located in the reaction zone 2 of the reactor, approximately 102 mm above the surface of the distribution plate facing the fluidized bed, and approximately 21.0 meters in length. In another specific embodiment, as shown in FIG. 2a, when Q is about 16.64 meters, each measurement position n device is located at a height of about 152 mm above the surface of the distribution plate 32 facing the fluidized bed, and each The measurement position ^ temperature is measured at this point. In a specific embodiment, each measuring position n device protrudes from the inner wall of the reactor by about 0.048D to about 0.18D and enters the reactor, where D is the smallest dimension from one wall to the opposite wall, perpendicular to each The wall measure, with respect to the minimum internal cross-sectional area of the reaction zone 2, is present at a distance from the surface of the distribution plate facing the fluidized bed to approximately 203 mm above the surface in the bed. In another specific embodiment, each measuring position n device protrudes from the inner wall of the reactor by about 0.062D to about 0.14D and enters the reactor. In another specific embodiment, each measuring position n device protrudes from the inner wall of the reactor by about 0.070D to about 0.10D and enters the reactor. In a specific embodiment, for a cylindrical reaction zone, that is, a person having a circular cross-sectional area, each measuring position 11 device protrudes from the inner wall of the reactor by about 0.048 ID to about 0.18 ID and enters the reactor. Where ID is the internal reactor diameter. In another specific embodiment, each measuring position 11 device protrudes from the inner wall of the reactor by about 0.062 ID to about 0.14 ID and enters the reactor. In another item, 85552 • 40- 200426156 7. The Jiuliang measuring position 11 device protrudes from the inner wall of the reactor. In the specific embodiment, each z-A Π 1 ΠΤΉ 9 enters the reaction benefit.

0.070ID 彡 about 0.10ID In a specific embodiment, the ‘devices at each measurement position n protrude from the inner wall of the reactor by about 300 mm and enter the reactor’ with an ID of about 4.42 meters. In another embodiment of the nasal body, the 'devices at each measurement position n protrude from the inner wall of the reactor by about 350 mm and enter the reactor' with an ID of about 4.42 meters. In another specific embodiment, each measuring position n device protrudes from the inner wall of the reactor by about 300 mm'into the reactor 'and has an ID of about 5.5 meters. In another specific embodiment, the 'devices at each measurement position η protrude from the inner wall of the reactor by about 350 mm and enter the reactor' with an ID of about 5.5 meters. In another specific embodiment, each measuring position n device protrudes from the inner wall of the reactor by about 400 mm, enters the reactor, and has an ID of about 5.5 meters. Any number of measurement position n devices can exist, of course, provided that multiple measurement position devices exist. In a specific embodiment, there are four measuring position n devices. In another embodiment, there is a device for measuring position n. In another embodiment, there are twelve measuring positions. In another specific embodiment, there are sixteen measuring position n devices. In the specific embodiment shown in the figure, the four measuring positions are substantially equally radiated in a radial manner. Tian Guang, Yue, and Wu respond to the circumference of the circle, which means that at the position I and i Measure position 2

At measurement position 3 and measurement position, at degree! Between position 2 and measurement position 3, there is about 901. In the other two rooms, and at the measurement position 4 and the measurement position 1, the devices are substantially equal to = in the specific embodiment, the person measurement position η. In another specific embodiment &quot; spaced around the circumference of the reactor in a directional manner, the 'twelve measurement positions' in 1 is essentially 85552 '41. 200426156 spaced equally around the circumference of the reactor in a radial manner. . In another embodiment of the stomach, the sixteen measuring position n devices are substantially equally spaced around the circumference of the reactor in a ballast manner. The temperature at each measurement position η, that is, the measurement position η temperature, can be measured by any conventional method, such as using a thermometer, a thermocouple, a thermistor, or a platinum resistance thermometer. For the purpose of this application, the quantity Aη is defined from the viewpoint of the controlled reactor bed temperature, the reactor inlet temperature, and the temperature of each measurement position η, and is defined as the following equation (1): (Controlled reactor bed temperature)- (Measuring position η temperature) ----- (1) (Controlled reactor bed temperature)-(Reactor inlet temperature) where each temperature is expressed in the same temperature measurement unit, for example,. c means. Therefore, 'Αη is the ratio of the two temperature differences, which is a dimensionless parameter. Each a is about the temperature of a specific measurement location. For example, ^ temperature 'measured at measurement position 1 is used to calculate A!' 'S temperature measured at measurement position 2 is used to measure A2, and so on. Therefore, in a specific embodiment, there are sixteen degrees f-position n temperature, which means the temperature from the measurement position i to the temperature at the measurement position M, and there are sixteen Aη values, that is, Al to Al 6 individually. It has been surprisingly discovered that certain ranges of An values can be used to find and define the desired operating conditions for the polymerization process of a gas fluidized bed reactor, as discussed below. Inevitably, since there may be fluctuations in the temperatures involved in measuring An, it is particularly important to identify the trend of \. This can be achieved by observing multiple An values, such as at least about 18, over a relatively short period of time, such as about 3 minutes, to determine whether a noteworthy An value is an instantaneous I motion, or an indicator of changing operating conditions. The instantaneous fluctuations on An will not be long-lasting 85552 -42- 200426156, even after a relatively short period of time; the eighth "straight" state of the display during the change will be maintained through this relatively short period of time. During gas fluidization The fluidized bed density ("FBD") in a bed polymerization reactor is conventionally defined as going up a part of the reactor, meaning the measured pressure drop in the direction of the gas flow, divided by the measured pressure Falling distance. Therefore, those skilled in this art know that FBD is the average. Conventionally, a typical fluidized bed polymerization reactor has pressure measurement points or interfaces at three heights within the reaction zone. Therefore, the fluidized bed in the reactor has been divided into two zones or sections, called the lower fluidized bed and the upper fluidized bed. The bottom or starting point of the lower fluidized bed starts at or near the surface of the distribution plate, such as 32 in Figure 1, facing the fluidized bed and extending upwards, which means that in the direction of the air flow, the top or uppermost degree ends. At the bottom or starting point of the fluidized bed above. The bottom of the upper fluidized bed starts at the top surface of the lower fluidized bed and extends upward, meaning that in the direction of the air flow, the top of the fluidized bed ends at or near the top of the fluidized bed. · In a specific embodiment, the pressure drop of the lower fluidized bed is the first position at a height of about 0.005Q to about 0.028Q above the surface of the distribution plate facing the fluidized bed, and the distribution plate faces the distribution plate facing the fluidized bed. Measured between the second position at a height of about 0.15Q to about 0.49Q above the surface. In another embodiment, the pressure drop of the lower fluidized bed is measured between a first position at about 0.006Q to about 0.021Q and a second position at about 0.18Q to about 0.45Q. In another specific embodiment, the pressure drop of the lower fluidized bed is measured between a first position at about 0.008Q to about 0.014Q and a second position at about 0.19Q to about 0.42Q. In a specific embodiment, the pressure drop of the upper fluidized bed is at a third position at a height of about 0.15Q to about a49Q above the surface of the distribution plate at 85552-43-200426156 facing the fluidized bed, and at the third position facing the fluidized bed. Measured between the fourth position above the surface of the distribution plate at a height of about 0.555Q to about 0.80Q. In another specific embodiment, the pressure drop of the upper fluidized bed is at a third position at about 0.18Q to about 0.45Q, and at a fourth position at about 0.60q to about 0.78Q Metric. In another specific embodiment, the pressure drop of the upper fluidized bed is measured between a third position at about 0J9Q to about 0.42Q and a fourth position at about 0.615Q to about 0.75Q. In the specific embodiment, with respect to q, the second position is the same as the third position. In another embodiment, with respect to Q, the second position is different from the third position. The density of a fluidized bed is observed using a measure of the pressure difference between the area below the bed and the area above the bed. As shown in the figure, the density of the lower fluidized bed (&quot; LBD &quot;) can be called from the pressure gauge interface? 1. Interface P2, 0.37q above the distribution plate (for example, Q = 16,64 mm, ㈣50 mm), the pressure difference between the two, divided by the distance separating _p2, which means about 0 view, for example, Q = 16 , 64 mm, about 6, mm). The density of the upper fluidized bed (&quot; excitation &quot;) can be connected to the pressure gauge P2, the surface of the distribution plate facing the fluidized bed (for example, Q = 16'640 mm 'is about 6,150 mm), and the pressure gauge interface P3 ㈣Q above the distribution plate (for example, q = Liao millimeter, which is about 12,15 ohms), the pressure difference between the two is divided by the distance separating P2 and P3, which means about a36Q (for example, ㈣, 64. Mm 'is about 6, mm). : Can be about 190 to about 400 kg / m3. In the other implementation of 歹 |, the excitation is about 200 to about 37 kg / m3. In another specific embodiment 85552 200426156, the UBD is about 210 to about 340 kg / m3. In another embodiment, the UBD is from about 220 to about 350 kg / m3. In another specific embodiment, the UBD is from about 220 to about 300 kg / m3. Conventionally, the weight or bed weight of a fluidized bed is approximately equal to the pressure drop across the bed times the internal cross-sectional area of the reactor. The height of the fluidized bed or bed is often kept higher than the position where the measure P3 is measured, for example, for the reaction tower in Fig. 2a, it is higher than 0.73Q. As is known in the art, the calculation of specific values can be determined from the pressure readings and UBD at P3 and P5, and depends on the type of each specific reaction tower. The amount referred to as "neck ΔP" in this technique is an indicator that gives the fluidized bed a degree (if any) of the expansion zone (for example, 4 in Figure 1). For example, for a reaction tower with Q = 16,640 mm and configured as shown in Figure 2a, the neck ΔP can be faced by a pressure gauge interface P4 of 16,967 mm above the surface of the distribution plate facing the fluidized bed and a pressure of 26,310 mm above the distribution plate. Measured by the pressure difference between the meter interface P5. Pressure can be measured using any conventional means, such as using a barometer, pressure gauge, or pressure transmitter. Differential pressure or pressure drop can be measured using any conventional means, such as using a differential barometer, differential pressure gauge, or electronically comparing signals obtained from two pressure transmitters. For the purpose of this application, the amount of Δρ is based on the views of LBD and UBD, and is defined as the following equation (2): △ p = LBD-UBD (2) where each density is of course expressed in the same unit of density measurement, such as Expressed in kilograms per cubic meter. Inevitably, because there may be fluctuations in the pressures involved in measuring Δρ, it is particularly important to identify the trend of Δρ. This can be achieved by observing the value of 85552 -45- 200426156 evening weight Δρ, for example, at least about 18, and after a relatively well-known time production, such as about 3 minutes, to determine whether the value of note ~ is instantaneous: two: or change Medium operation status <indicator. The instantaneous fluctuations on ~ will not occur, even after this relatively short period of time; the value of the operating state energy in the display change will be maintained through this relatively short period of time. It has been surprisingly #found that ~ and can be used to monitor changes in the fluidized bed conditions in the reaction zone, and in some ranges, in some cases combined with Αη values in some ranges, can be used to Find and define the pure operating states required for a gas fluidized bed reactor polymerization process, as discussed below. For the purposes of this application, the following seven "pure" continuity states are defined here: &quot; steady state &quot;, &quot; warning state, &quot;, &quot; corrective action state &quot;, &quot; continuous damage state &quot;, &quot; &quot; Loss of continuity 丨 ,, "△ 々Alarm state" and "Continuity loss 2". Certain ranges, and in some cases, combined with certain ranges of Aη values, can be used to find and define the desired operating state with respect to the polymerization method of a gas fluidized bed reactor, which means "steady state", "warning state" , "Corrective action state", "continuous damage state" and / or "alarm-like complaints" as discussed below. Table 1 below is an excerpt from the seven "pure" consecutive performance states defined here. 85552 46- 200426156 Table 1 · Loss of continuity in pure continuity state 170 kg / m3 0.8 ^ η &lt; 1.0 Continuity damage state 50 kg / m3 70 kg / m3 0.7 ^ An &lt; 0.8 Corrective action state 40 kg / m3 $ ~ 50 kg / m3 0.6 ^ An &lt; 0.7 Warning state 30 kg / m3 40 kg / m3 0.55 ^ An &lt; 0.6 Steady state 10 kg / m3 30 kg / m3 0.25 SAn &lt; 0.55 △ ρ alarm status 0 kg / m3 $ &lt; 10 kg / m3 loss of continuity status 2 ”Δρ” &lt; 0 kg / m3 ~ An value used in this article that satisfies a status condition "Critical number ,, and very few, but the number of the position measurement means 11 by the presence of a temperature dependent. In a specific embodiment, when there are four temperature measurement position n devices, that is, as shown in FIG. 2b, the critical number of An values is two. In another specific embodiment, when sixteen temperature measurement position n devices exist, the critical number of ^ values is three. In another specific embodiment, when there are n temperature units 85552 -47- 200426156, the critical number of An values is ⑻m. If ⑻M is not an integer, the nearest integer is adopted. For example, if n is 2, the critical number is 1, if η is 3, the critical number is 1; if n is 4, the critical number is 2; when square η is 8, the critical number is 2; if n is 12 , The critical number is 2; if n is 15, the critical number is 2; if η is 16, the critical number is 3; and so on. It has been found that in fluidized bed polymerization reactions that cover a wide range of conditions, for example, the 彳 &lt; dry mode method reaches a method characterized by a relatively high degree of condensation, and it can be confirmed that the point is reachable and that the method is in danger of failure, For example, if the critical number of ΔP and / or Aη values increases further, continuity is lost. This point can be confirmed by monitoring LBD, UBD, and in some cases, for controlled reactor bed temperature, measurement position η temperature, and reactor inlet temperature; it can be applied to a wide range of conditions, from dry mode methods to achieve It is characterized by a relatively high degree of cold &amp; Monitoring can be achieved by customary methods, such as by a computer-controlled system that periodically samples and displays these parameters, calculates or Δη, and compares Αρ or Αη individually with limits and values. In the desired operating state called "stable state", at least the critical number of An satisfies the condition 0.25 s An &lt; 0.55, and Δρ satisfies the condition 10 kg / m3 S Δρ &lt; 30 kg / m3. In the steady state, the low value of the car parent compared with and is 0 · 25, the higher value compared with Αη is 0.55, and there are two limits of 10 kg / m3 and 30 compared with the comparison. Kg / m3. In order to reduce Αη and / or Δρ while keeping each within its "steady state" operating range, 'no specific action is necessary. However, even in "steady state", it is recommended to closely monitor Αη Value, LBD and UBD, especially when the degree of condensation is relatively high, for example below 17.5% by weight and higher. 85552 -48- 200426156 continuous gas fluidized bed method for manufacturing the polymer of the present invention can continue to &quot; Stable state &quot; operation. At least the critical number of Αη satisfies the condition α55 $ An &lt; Q 6 and △ is sufficient to cater / cubic meter S △ 々 &lt; 40 kg / cubic meter, then the &quot; warning state is reached, at Warning, sad, middle, compared with Αη The low value is 055, and the higher value compared to &amp; is 0.6, and there are two limits compared to 30 kg / m3 and 40 kg / m #. For any further on the value of Aη and / or ~ The increase must be alert, because such a step-up increase may indicate that the corrective action state: is being approached 'or has been reached. Although to reduce ~ and, or ~, or to reduce Αη and / or to advance- Increased possibility, no specific action is necessary ', but the following actions are recommended ... Mass flow rate of J bed with same bed weight, LBD, UBD, and airflow through the fluidized bed. • Keep the bed weight at a substantially constant level. 4 疋The PDS system is not completely or partially clogged, and if so, remedy the situation. • The foot pressure measurement interface is not completely or partially clogged, and if so, remedy the situation. • Reduce the catalyst feed by 50%. The continuous gas slurry bed method of Yuehe compound can continue to operate with &quot; Warning ^. However, the polymer manufacturing efficiency of this method may decrease during the reduction of catalyst feed. Right to / An critical number Satisfies the condition 0 · 6 $ Α〆〇 · 7 and satisfies the condition 40 kg / million ^ ΑΡ &lt; 50 kg / m3, &quot; corrective action state &quot;. In the "corrective action state", the lower value compared to Αη is 0.6, and the higher value of human Aη to 軚 is 0.7, and compared with △ / 〇, there are two limits. 4055285552 -49- 200426156, 50, 50 meters per square meter. In order to reduce the possibility of An and / or, or to / minus) An &amp; / or ~, it is recommended to take the following actions: • Stop catalyst feed. • Monitor bed height, bed weight, LBD, Na and the mass flow rate of airflow through the fluidized bed. The bed weight is constant at a constant load; the fluid bed weight set point should not be changed in an attempt to change the bed height. By keeping the compressor operating, the recirculated gas is kept in circulation. • Check that the pressure measurement interface is closest to the distribution plate to confirm that the bed is fluidized, and if not, remedy the situation. The use of these actions by silk is to reduce or even exclude the continuity damage states described in the following paragraph (the possibility of being achieved. However, even in the absence of any constructive action, the continuous gas for the polymer of the present invention is produced The fluidized bed method can also continue to operate in the "corrected action state". Of course, the polymer manufacturing efficiency of this method may be reduced during the period when the catalyst feed is stopped. At least the critical number of Αη satisfies the conditions 〇7 ^ & 〇8 and ~ meet the conditions of 50 kg / million ^ ^ ρ &lt; 70 kg / m3, then reach, the state of continuity damage ". In the" state of continuity damage ", it is lower than Αη The value is 0j ', the higher value compared to An is 0.8, and compared with ~, there are two limits of 50kg / m3 and 70kg / m3. To reduce A, / or ~, or soil / Reduce the possibility that Αη and / or Δρ will further increase, it is recommended to take the following actions: • Stop the catalyst feed, if it has not been stopped, and perform the so-called catalyst &quot; 85552 -50- 200426156 Type I all-static Treatment ". Keep the bed solid Change the height of the bed in an attempt to change the bed constant. • The operation of the compressor is maintained to maintain the recirculated gas circulation. This type of "know-how" is known as "Type 1 All Quiet" ^ involves adding an effective amount of catalyst poison: It is typically-carbon oxide, into the reactor, and at the same time the compressor is in operation, so the -carbon oxide is circulated, and the catalyst stock inside the reactor is deactivated. Type I The static treatment can be reversed by adding other catalysts after washing the poisons of the catalyst from the system and charging the I. In the case of continuous shooting complaints, there may be polymer blocks in the Anti-backup (possibility, so it is generally desirable to check the interfaces near the distribution plate, such as for pressure and / or measurement locations, for temperature measurement devices to obtain interfaces, to ensure that no polymer blocks have contributed to the complete or partial connection of these interfaces. If the blocker is found to be totally or partially blocked, the affected interface should be removed, for example by drilling. Furthermore, if polymer blocks are formed in the reactor, this method may have to be interrupted. Remove the lumps at the same time. The above is about ^ days-months. § However, the polymer manufacturing efficiency of this method is reduced during this period. However, due to the "continuity damage state," the interruption of the period is more than the loss of even one state The interruption of a period is typically a short period, so the foregoing state is advantageous when compared with the latter.

The fluid bed weight set point should not be reported until the critical number of ^ An meets the condition 0.8 A &lt; and the condition of 70 kg / m3 S Λρ is reached, and the loss of continuity state is &quot;. In the loss of consecutive performance traits 1,1, the lower value compared with Αη is 0.8, the value of I direction compared with Αη is 丨 · 0, and compared with Δρ, there is a limit of 70 kg / 85552 -51 -200426156 Cubic in, loss of continuity state 丨 ,, and, because the polymer block can be formed in Anti-Secondary II, causing it to be blocked or completely blocked, this method may have to be interrupted and removed at the same time Lumps, typically for a period of about 7-15 days. It has also been found that in a fluidized bed polymerization reaction performed over a wide range of conditions, the method such as the dry text method reaches a relatively high degree of condensation. If the method is lower than a certain level, the point can be confirmed. To the extent that the party is in danger of failure, such as loss of continuity. If it falls below the stable state of '', the Ap range satisfies the condition of 0 kg / m3 △ kg / m3, then it reaches the "alarm state". In the "alarm state", there are two limits of 0 kg / m3 and 10 kg / m3 compared with Δρ. To increase Αρ or at least reduce the possibility of further reduction, the following actions are recommended: • Monitoring bed Height, bed weight, LBD, UBD, and mass flow rate of gas flow through the fluidized bed. • Keep the bed weight at a substantially constant level; the fluid bed weight set point should not be changed in an attempt to change the bed height. • By maintaining The compressor operates to maintain recirculated gas circulation. • Check the pressure gauge interface closest to the distribution plate to confirm that the bed is fluidized, and if not, remedy the situation. Also 'if Δρ continues to display π Δρ alarm status π over a long period of time For example, at least 10 to 15 minutes, you must take the following actions: • Then change the catalyst batch to the new catalyst batch during use. • Reduce the new catalyst input when compared with the feed content of the previous batch. It is believed that the use of this action is intended to reduce or even exclude the possibility of reaching the "loss of continuity 2" described in paragraph 85552-52-200426156 below. However, the continuous gas fluidized bed method for manufacturing the hydrate of the present invention can continue to operate in a warning state. Of course, the polymer manufacturing efficiency of this method may decrease during the reduction of catalyst feed. The square Δρ satisfies the condition "" &lt; 0 kg / m3, and then reaches, the loss of continuity state 2 '. In the "loss of continuity state 2", there is a limit of 0 kg / m3 compared to "". As discussed above, because there may be fluctuations in the pressures involved in measuring Δρ, it is important to identify trends, especially regarding "loss of continuity 2". This can be achieved by observing multiple Δρ values, such as at least about 18, over a relatively short period of time, such as about 3 minutes, to determine whether the value of note is an instantaneous fluctuation or an indicator of changing operating conditions. Therefore, regarding the loss of continuity state 2, the system is shown as, Λρ "to indicate that the instantaneous fluctuation on △ 々 is not enough to trigger the loss of continuous state 2". Instead, it is required (lbd—Yeshang's performance change 'means, △ 〆, to show that the loss of continuity state 2 ,,. In order to increase "Δρ" or at least decrease ", it will be further To reduce the possibility, the following actions are recommended: Stop the catalyst feed 'if it has not been stopped, and perform the so-called catalyst, type I fully static treatment.' By keeping the compressor operating, keep the recirculated gas circulating • Stop the feeding of monomer and co-monomer. In the loss of continuity 2 &quot;, because the polymer block may be said / formed in the reactor to make it partially or completely blocked, so this method may be Blocks must be interrupted and removed simultaneously, typically over a period of about 7-15 days. 85552 -53- 200426156 During the process of the continuous gas fluidized bed process of the present invention for the manufacture of polymers, in addition to the seven discussed in detail above, In addition to the pure “continuity” state, you may encounter a “transition” continuity state. As used in this paper, the transition “continuity state” exists when the Δρ value is lost in relation to the state that is not continuous Within a range specified by Aρ for a purely continuous character, but the critical number of An values is within the range of &lt; An with respect to a different purely continuous state that is not lost for a continuous state. For example, transition to continuous The sexual status exists in the range of 35 kg / m3, which means that it is within the "warning state," and two of the total-and four Aη values meet the condition of 0.25 $ Αη &lt; 0.55, meaning Now, when the stability is within the range of ΑηΚ. Take the following as another example, the transformation of continuous traits exists when it is 5 kg / m3, which means that it is within the range of Δρ of the warning state ~, and a total of four Two of these An values meet the condition of 0, 55, and 6 when they are in the `` warning state, and within the range of An. When you encounter a transition continuity state during the operation, you are generally expected to consider the article about the return The "steady state" constitutes a state of pure continuity, and if Δρ is &lt; 10 kg /, / 乂 10,000 meters, it is about, 'Δρ alarm state, and, the proposed action is provided. A, loan J such as' for the above transition states, where Display, warning warning! "," Three of the four An values indicate "steady state", and generally expect to take the suggested actions provided by "^, closing hair warning state". Take the following as another. × For example, for the above transition status, △ / 〇 displays "Δρ alarm status", and two of the four Δη values of γ display, "warning status". It is generally expected to consider the above S3 to recognize "you The recommended actions provided by the company in the "state of announcement" and / or "Δ /? Alarm state" are used to perform the continuous gas fluidization of a polymer of the present invention in a specific embodiment 85552 -54- 200426156 bed method, Operate in a steady state. In another embodiment, the continuous gas fluidized bed method of manufacturing a polymer of the present invention operates in a warning state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a corrective action state. In another embodiment, the continuous gas fluidized bed method for manufacturing a polymer of the present invention operates in a state of continuity damage. In another embodiment, the continuous gas fluidized bed method of manufacturing a polymer of the present invention operates in a Δρ alarm state. In another embodiment, the continuous gas fluidized bed method of manufacturing the polymer of the present invention operates in a steady state and a warning state. In another embodiment, the continuous gas fluidized bed method of manufacturing the polymer of the present invention operates in a steady state and a Δρ alarm state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a warning state and a corrective action state. -In another specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates by correcting the operating state and the state of continuity damage. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a Δρ alarm state, a steady state, and a warning state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a steady state, a warning state, and a corrective action state. In another specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a warning state, a corrective action state, and a state of continuity damage. 85552 -55- 200426156 In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a Δρ alarm state, steady state, warning state, and corrective action state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a steady state, a warning state, a corrective action state, and a continuous damage state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a Δρ alarm state, steady state, warning state, corrective action state, and continuity-damaged state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a steady state or a warning state. In another specific embodiment, the continuous gas fluidized bed method of manufacturing a polymer of the present invention operates in a steady state or a Δρ alarm state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a warning state or a corrective action state. -In another specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a state of corrective action or state of continuity damage. In another embodiment, the continuous gas fluidized bed method for manufacturing a polymer of the present invention operates in a Δ / 0 alarm state, steady state, or warning state. In another embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a steady state, a warning state, or a corrective action state. In another specific embodiment, the continuous gas fluidized bed method for manufacturing a polymer of the present invention operates in a warning state, a corrective action state, or a state of continuity damage. 85552 -56- 200426156 In another embodiment, a continuous gas flow for the production of a polymer of the invention

The bed method is operated in the state of ~ alarm state, warning state, or calibration. In another specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention operates in a steady state, a warning state, a corrective action state, or a continuous damage state. In another specific embodiment, the method for manufacturing a continuous gas fluidized bed of a polymer of the present invention operates in a Δρ alarm state, steady state, warning state, corrective action state, or continuity damage state. In another specific embodiment, a continuous gas fluidized bed method for manufacturing a polymer of the present invention is operated so that the condition of 10 kg / m3 $ Δρ &lt; 30 kg / m3 is simultaneously satisfied, and at least Αη The critical number satisfies the condition 0.25 $ Αη &lt; 0.55. In another specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention is operated so that the condition 30 kg / m 3 40 kg / m 3 is simultaneously satisfied, and at least the critical number satisfies Condition 0.55 $ Αη &lt; 0.6. In another specific embodiment, a continuous gas fluidized bed method for manufacturing a polymer of the present invention is operated so that at the same time Aρ satisfies the condition 40 kg / m3 S Δρ &lt; 50 kg / m3, and at least The critical number of Aη satisfies the condition 0.6 $ Aη &lt; 0.7. In another specific embodiment, a continuous gas fluidized bed method for manufacturing a polymer of the present invention is operated so that the condition of 50 kg / m3 $ Δρ &lt; 70 kg / m3 is simultaneously satisfied, and at least The critical number satisfies 85552 -57- 200426156 pieces 0.7 $ Aη &lt; 0.8. In another specific embodiment, the continuous gas fluidized bed method for manufacturing the aggregates of the present invention is operated so that ΔP satisfies the condition of 0 kg ;: square meter S △ / 〇 &lt; 10 kg / cubic meter . In another specific embodiment, the method is used to produce a continuous gas fluidized bed method, in order to achieve the condition that the simultaneous Δρ satisfies the condition of 10 kg / m3 at the same time $ Δρ &lt; 40 kg / s, soil η ^ , Α, &gt; / 乂 Wanwei, and at least the critical number of Αηfoot meets the condition 0.25 gAn &lt; 0.6. In another specific embodiment, it is a continuous gas fluidized bed operation for manufacturing the polymer of the present invention. Method, so that at the same time the condition ι〇kg / cubic meter ^ △ ρ &lt; 50 kg / cubic meter is met, and at least the critical number of Aη satisfies the condition 0.25 $ Αη &lt; 0.7 in another specific embodiment, Is a continuous gas fluidized bed method for manufacturing the polymer of the present invention such that Δρ satisfies the condition 10 kg / m3 at the same time $ Δρ &lt; 70 kg / m3 and at least A. The critical number satisfies the condition 0.25 SAn & lt 0.8. In another specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention is operated so that at the same time Δ p satisfies the condition 30 kg / m 3 S Δ P &lt; 50 Kg / m3 and at least &amp; critical number The conditions are 0.55 $ Αη &lt; 0. 7. In another embodiment, a continuous gas fluidized bed method for manufacturing a polymer of the present invention is operated so that at the same time Λρ satisfies the condition of 30 kg / m3 &lt; 70 kg / m3, and at least the critical number of Αη satisfies the condition 0.55 $ Αη &lt; 0 · 8 〇85552 -58-200426156 In another specific embodiment, it is a continuous gas operated for manufacturing the polymer of the present invention Fluidized bed method, so that at the same time ΛP satisfies the condition of 40 kg / cubic meter $ Δρ &lt; 70 kg / cubic meter * above twenty thousand yuan, and at least a critical number of Αη 〇6 $ Αη &lt; 0 · 8. In a specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention is operated so that the condition 0 kg / m3 ^ &lt; 30 kg / m3 is satisfied, and when kg / m3 At the same time, the critical number of at least Aη satisfies the condition 025 $ A / 055. In another specific embodiment, the continuous gas fluidized bed method for manufacturing the polymer of the present invention is operated so that the condition 0 kg / M3_ &lt; 40kg / m3, And when 0 kg and cubic meters, the critical number of at least Aη simultaneously satisfies the condition of 0.25 $ 0.6. In another specific embodiment, a continuous gas fluidized bed method for manufacturing a polymer of the present invention is operated , So that the condition of 0 kg / m3 ^ △ ρ &lt; 50 kg / m3 is satisfied, and when ~ ^ 10 kg / m3, at least Ani 5¾ bounds satisfy the condition of 0.25 $ Αη &lt; 0.7. In another specific embodiment, a continuous gas fluidized bed method for manufacturing a polymer of the present invention is operated so that the condition 0 kg / m3 S Δρ &lt; 70 kg / m3 is satisfied, and when ^ 1〇 At kg / m3, the critical number of at least An simultaneously satisfies the condition 0.25 $ An &lt; 0.8. In addition, the present invention relates to a method for monitoring and providing continuity in a gas fluidized bed method characterized by a condensing agent in a circulating stream in the manufacture of a polymer, comprising: monitoring a fluidized bed reaction zone ν 'wherein the reaction zone The belt has a controlled reactor bed temperature of 85552-59-200426156, a lower fluidized bed density, an upper fluidized bed density, and a plurality of measurement position temperatures; monitoring of the circulating flow into the reaction zone, wherein the gas flow has a reactor inlet temperature; Measure Δρ, and compare Δρ with at least one limit; and when Δρ-10 kg / m3, measure multiple Aη, and compare each Aη with lower and higher values, where each \ and Δρ are as above definition. In a specific embodiment, there are four measurement positions η temperature. In another specific embodiment, there are 16 measurement locations ^ temperature. In another specific embodiment, the present invention relates to a method for monitoring and providing continuity in a gas fluidized bed method characterized in that a condensing agent is in a circulating stream in the manufacture of a polymer, which includes: monitoring a fluidized bed The reaction zone, wherein the reaction zone has a controlled reactor bed temperature, a lower fluidized bed density, an upper fluidized bed density and a plurality of measurement positions η temperature; monitoring of the circulating flow into the reaction zone, wherein the gas stream has a reactor Inlet temperature;-measuring Δρ, and comparing Δρ with at least one limit; and measuring multiple Δη, and comparing each Δη with a lower value and a higher value, wherein each of 811 and 8/0 are as defined above. In another specific embodiment, the present invention relates to a method for monitoring and providing continuity in a gas fluidized bed method characterized in that a condensing agent is in a circulating stream in the manufacture of a polymer, which includes: monitoring a fluidized bed A reaction zone, wherein the reaction zone has a lower fluidized bed density and an upper fluidized bed density; compared with determining Δρ, and comparing Δρ with at least one limit, wherein Δρ is as defined in the foregoing 85552 -60- 200426156 text. [Embodiment] Examples, as described above, 'characterized by a condensing agent in a circulating gas fluidized bed method' and monitoring in a method characterized by a condensing agent in a circulating fluidized bed method It also provides a method of continuity that produces superior performance in the manufacture of polymers. The following examples are provided to further illustrate some specific embodiments of the present invention. These examples are provided for illustrative purposes only, and are not intended to limit the scope of the present invention in any way. 6.1 Epidemic ^ continuous state loss 1 &gt; _ This example is used to illustrate that the Δρ and An parameters indicate changes in the fluidized bed and their disintegration, which ultimately leads to "loss of continuous state Γ, which requires the reactor to be closed Manufactured in a gas slurry bed from about 44.2 mol% ethylene monomer, about 7.6 mol% butene-1 monomer, about 8.0 mol% hydrogen, and about 105 mol During the copolymerization of a mixture of a condensing agent called ic5 and about 19.7 mole% inert gas (meaning about 148 mole% nitrogen and about 4.9 mole% ethane), certain factors may cause the production to stop, And the process continuity is lost. IC5 contains a mixture of about 97-98% by weight isopentane and about 2-3% by weight neopentane and n-pentane, and is considered to further contain 4 carbon atoms below about 10 ppm by weight. Alkanes and alkanes with 6 carbon atoms in a weight ratio of less than about 10 PPm. The liquid-containing mixture introduced into the reaction zone contains about 12% to about 13% by weight of liquid in a circulating flow. The total weight is the basis. The catalyst used is Ziegler-Natta type catalyst, including titanium trichloride and aluminum alkyl. The fluidized bed reactor device used has a reaction tower having a reaction zone with a generally circular 85552-61, 200426156 columnar shape, and an expansion zone with a substantially conical shape in the lower half and a substantially hemispherical shape in the upper half, such as Shown in the picture. In this device, Q is about 16 64 meters. The reaction tower is equipped with a pressure interface and four measuring position η thermocouple devices, which are located as shown in Figures 2a and 2b. Approximately controlled reaction The reactor bed temperature set point is 86 ° C, which will result in an average controlled reactor bed temperature of about 87; rc, after 15 hours, ends at about 15: 00 hours, which means immediately following the discussion below Before 16:00 hours before the event. During the 15-hour period, other method parameters have the following averages and ranges: · Response pressure · Average is about 2L3 kg / cm² (from about 20.9 kg / cm² to about 21.6 Kg / cm2); reactor inlet temperature: on average about 55.2 ° C (from about 53.0 ° C to about 59.3.); Dew point temperature: on average 64.2 ° C (from about 63.2. (: To about 65.5.) ; Recirculated gas density: average 28.7 kg / litre Meters (from about 28.2 kg / m3 to about 29.3 kg / m3). The recirculated gas density is calculated based on the recirculated gas composition, which in turn is measured at the compressor outlet. The following table 2 gives other important manufacturing parameters The time before and during the shutdown. Table 2: Data excerpts about the loss of continuity indicated in Example 6.1 i time hours: minutes reactor bed temperature ° C distribution plate ΔP mm η2ο bed height meter bed weight ton SGV meter / Sec UBD kg / cubic meter LBD kg / cubic meter 厶 P kg / cubic meter A3 a4 8:09 86.6 8506 15.4 56.3 0.82 243 290 47 0.54 0.47 8:33 U ----- _, 86.8 8939 _J5.3 55.6 0.80 241 249 8 0.61 0.48 ί 8:52 87.3 8887 ^! 5.4 56.0 0.81 239 247 8 0.64 0.43: 9:11 87.6 8864 _J5.3 55.5 0.80 241 244 3 0.63 0.43! 9:30 87.4 8802 _J5.〇55.3 0.80 246 245 • 1 0.66 0.43 9:50 87.0 8788 15.3 56.6 0.80 239 250 10 0.62 0.43 j 10:09 86.6 8800 1 56.9 0.80 243 252 9 0.49 0.38 I 10:28 t 87.0 9020 LIL5.6 57.7 0.80 244 250 6 0.51 0.33- 62-

85552 200426156 Hours: minutes reactor bed temperature ° C distribution plate ΔΡ mm h2o bed height I meter I bed weight | tons ί SGV ~ T UBD meters / I kg / second 丨 cubic meters L 巳 D kg / cubic meters △ P 「 a3] kg / I! m3 丨 a4 Ί 10:47 87.0 8868 15.4 57.8 丨 0.81 | 247 248 0 0.43 ί 0.31; 11:06 87.0 8686 15.2 57.9 丨 0.79 252 252 0_J 0.57 0.3 ~ 6 1 11:26 86.9 8978 15.4 58.1 0.79 249 249 0 _ Ί 0.55! &Quot; a35 ~ 11:45 87.4 8941 15.4 57.7! 0.79 251 246 -5 0.55 0.41 12:04 87.9 8819 15.5 58.0 0.79 244 249 5 0.59 0.41 12:23 87.9 8691 15.3 57.1 0.79 246 250 4 0.77 0.51 12:42 87.3 8588 15.7 58.2 0.80 239 254 15 0.72 0.46 13:02 87.6 8745 15.3 58.2 0.78 251 251 0 0.72 0.53 13:21 87.2 8721 15.3 57.2 0.80 248 250 2 0.81 0.56 13:40 86.9 8916 15.6 57.8 0.79 242 248 6 0.68 0.52 13:59 86.7 9028 15.4 57.0 0.81 247 243 • 4 0.73 0.49 14:18 86.9-15.4 57.3 0.81 244 249 4 0.58 0.51 14:38 86.5-15.2 56.9 0.81 245 250 5 0.70 0.48 | 14: 57 86.8 8853 15.3 58.0 0.81 251 250 -2 0.71 0.50 i 15:16 8 6.7 9062 15.3 57.5 0.80 247 252 5 0.57 0.47 15:33 86.7 8855 15.5 57.0 0.81 237 248 11 0.62 0. ~ 45 15:35 87.1 9056 15.4 57.0 0.82 237 251 14 0.62 0.46 15:38 87.3 8913 15.4 56.5 0.81 239 248 9 0.68 0.44 15:40 87.2 8925! 15.5 56.2 0.81 236 248 12 0.62 0.46 15:42 86.8 9155 15.3 55.6 0.80 237 249 12; [0.61 0.47 15:45 86.3 9269 15.5 55.6 ί! 0.81 228 251 23! I 0.66 0.43 15: 47 87.0 9272 15.5 54.9 0.81 229 246 16 0.60 0.44 15:50 87.2 9127 15.4 54.5 0.81 228 244 16 0.65 0.48 15:52 86.8 8981 15.7 55.6 0.80 231 240 9!! 0.66 0.45 15:54 87.1 9229 15.3 54.6 0.80 232 242 11 0.65 0.44 15:57 86.8 9140 15.7 54.2 0.81 221 244 23 ji 0.58 0.44 | 15:59 86.8 9023 15.8 55.3 0.81 225 246 21 丨 0.60 0.41 16:02 87.8 9072 15.6 54.9 0.79 229 242 13 0.52 0.49 16:04 87.2 8821 15.6 55.0 0.80 227 248 20 0.61 0.49 16:06 86.8 9136 15.6 55.0 0.80 228 249 21 0.60 0.46 16:09 86.8 9018 16.0 54.8 0.81 221 237 16 0.53 0.47 16:11 87.5 9150 15.7 55.1 0.81 226 243 17 0.62 0.44 16:14 87.4 9084 15.6 54.2 0.79 222 244 22 0.61 0.48 16:16 86.6 8985 15.9 54,3 0.80 221 237 16 0.60 0.52 16:18 86.8 9152 16.1 55.6 0.79 224 240 16 0.55 0.46 16:21 87.6 9068 15.7 54.6 0.79 223 244 22 0.57 0.47 16:23 87.1 9049 16.0 54.3 0.79 217 241 24 0.60 0.48 16:26 86.7 9021 15.9 80.5 0.79 221 256 35 0.54 0.47 16:28 86.9 9200 16.4 54.1 0.79 220 235 15 0.56 0.39 16:30 87.4 8858 14.9 54.7 0.80 219 236 17 0.59 0.45 16 : 33 87.4 9037 16.2 55.0 0.79 221 240 19 0.55 0.48 16:35 87.0 8842 16.2 54.7 0.79 220 237 17 0.58 0.45 16:38 86.7 9192 16.1 54.8 0.79 225 233 8 0.58 0.45 16:40 87.3 8929 16.3 54.7 0.79 213 241 29 0.59 0.46 16:42 87.5 8841 16.2 55.7 0.79 223 241 17 0.56 0.45 16:45 87.3 9014 16.1 54.7 0.78 223 235 12 0.56-0.46 16:47 86.6 8986 16.3 54.0 0,79 214 235 22 0.60 0.49

85552 -63- 200426156 Hours: minutes reactor bed temperature ° C distribution plate ΔΡ mm H20 bed i height meter i bed weight ton 丨 SGV m / 丨 second UBD kg / m3 LBO kg / m3 Δρ kg / m3 a3 ~ I! 16:50 86.8 9215 16.3 53.8 0.80 214 233 20 0.60 0.44 16:52 87.2 9223 16.2 52.8!! 0.80 210 230 20 0.52 0.44 16:54 86.9 8892 16.2 52.3 0.79 202 238 36 0.58 0.46 16:57 86.8 9185 16.5 52.2 0.78 203 227 24 0.60 0.48 16:59 86.6 9368 16.7 51.0 0.79 195 222 28 0.60 0.45 17:02 87.4 9011 16.5 51.9 0.79 201 226 25 0.51 0.40 17:04 87.8 9003 16.3 51.5 0.77 200 230 29 0.59 0.45 17:06 86.6 9076 16.4 50.8 0.77 197 225 28 0.60 0.45 17:09 85.7 9398 16.5 49.6 ί 0.79 187 226 40 0.54 0.40 17:11 87.0 9096 16.8 49.2! 0.80 185 214 29 0.51 0.36 17:14 87.9 8842 16.6 50.8 0.77 193 222 29 0.63 0.44 17:16 86.8 9072 16.4 49.9 0.77 189 228 39 0.55 0.45 17:18 85.3 9353 16.7 48.9 0.78 185 212 28 0.49 0.44 17:21 86.7 9222 16.7 47.8 0.79 178 212 33 0.47 0.40 17:23 87.3 9085 16.5 46.8 0.77 177 215 38 0.57 0.43 17:26 85.4 9285 16.6 46.5 0.77 175 208 33 0.53 0.39 17:28 86.2 9427 16.8 45.1 0.79 168 201 33 0.45 0.41 17:30 87.5 8937 16.7 44.7 0.78 167 199 32 0.57 0.45 17:33 86.3 9301 16.5 45.2 0.78 172 202 30 0.49 0.46 | 17:35 86.1 9466 17.0 44.3 0.78 165 191 26 0.44 0.40 17:38 87.3 9115 16.8 44.3 ''! 0.79 163 199 36 0.51 0.40 | 17:40 87.3 9025 16.7 45.4 | j 0.78 164 210 46 0.96 0.46! 17:42 85.9 9440 16.5 44.4 0.78 158 222 64 0.71 &quot; 〇45 ~ | 17:45 86.2 9303 16.4 43.9 0.79 146 241 i 95 0 68 0.57: | 17:47 87.3 9211 15.9 43.2 0.78 136 261 125 0.52 0.73 17:50 85.1 9433 15.5 47.3 0.78 145 300 155 0.87 0.48 17:52 85.7 9560 15.9 47.9 0.78 124 327 202 0.81 0.82 17:54 86.0 9437 14.5 47.9 0.80 125 367 242 0.81 0.82 17:57 87.0 9237 14.5 48.2 0.79 121 368 247 0.90 0 service 17:59 86.1 9277 14.0 51.0 0.80 128 391 264 0.85 0.86 18:02 85.3 9332 14.3 49.9 0.79 128 384 256 0.86 0.87 18:04 85.4 9341 14.2 51.0 0.80 124 403 278 0.83 0.84 18:06 86.0 9287 14.1 51.6 0.80 124 41 1 287 0.86 0.86 18:09 85.1 9335 14.1 52.6 0.80 123 425 302 0.81 0.81 18:11 85.3 9354 13.8 53.8 0.80 133 430 297 0.77 0.77 18:14 86.1 9296 14.0 53.7 0.79 120 436 316 0.79 0.80 At about 16:00 hours, several conditions existed before adjustments were made to the operating parameters. To be clear, the analysis found frequent blockages of the catalyst feed tube. In addition, S3BD, which means that the combined mass of the microparticle products divided by the volume occupied by the particles is very low. Moreover, the pressure drop across the distribution plate ("Distribution plate ΔΠ") is high. Furthermore, a low value of Δρ was found. In particular, non-negative Δ! 〇 values below 10 kg / m3 are shown in Table 2 H-64- 85552 ZUU4ZOO ()

5 At different days, PS-IT, from about 8:33 hours to about 15:16 hours, sometimes for several connected addictions, "^ Inverse ,, continued number, alarm status" is displayed at different time series. ^} 〇 One, 33 hours until about 15.16 hours. However, the production of this example of JJL Polymerization 7, soil ... &lt; Continuous gas fluidized bed method is continuous operation, even in the "alarm state". At 1,600 hours, adjustments are implemented to reduce fluidization The weight of the bed ranges from about 55 meters to ㈣mi drink to reduce the height of the bed, because it is found to be too high. Then the bed length is increased by ~ 2, from about 15.6 meters at 17:35 hours to about 17.0 meters Figure 3 shows the graphs of LBD, _, bed height, bed weight, and ΔΔP, after a period of time, from hours before 18: Q2 to hours after. Kk &quot; IU bed's mass flow rate remains substantial No change in the above, and at the same time reducing the bed weight 'will lead to differences in the properties of the fluidized bed below and above. LBD] At the beginning, the final increase to more than about 400 kg / m3, such as at 18: 04 hours, at the same time advise Began to lower, and finally dropped below about 125 kg / meter above for example at 18: 04 hours. These changes from the above can be seen from the data in Table 2 and Figure 4, which is the left vertical axis The upper LBD 14 UBD 'and the vertical axis on the right, for from about 8: ⑽ hours to about 18 · A graph of 21 hours' time. For example, Figure 4 shows, for example, about 15 to 45 hours from about ^ ⑽ I to .45 on average. It is consistently lower than about kg / m3. Figure 5 is the weight of Figure 4. The marginal version, showing ㈣, delete and △ P, from about 16:50 hours to about 18:21 hours. It can be found from Figure 5 that, for example, △ P reaches a value of about milk kg / cubic meter in about Π: 40 hours, And at about 17:45 hours, the value is about 95 kg / m3. Figure 6 shows the number 8 and 4 on the left vertical axis and the number on the right vertical axis ~ 85552 -65- 200426156 'for from about 8 19 Hours to about 18: 21 hours. No corresponding values. Al and 8-2 values can be used for retrospective analysis. Figure 6 shows that, for example, from about 8:09 hours to about 17:42 hours, A4 is maintained on average— It is below about 0055. The transition state is displayed, for example, from about 17:21 to about 17:33 hours. During this period, the Δρ value indicates &quot; warning state &quot;, however, the value indication &quot; steady state; each The value and most of the value of 8.3 are 055 or lower. Of course, even in this transition state, the continuous gas fluidized bed method of this example is continuously operated. Fig. 7 is a redrawn version of Fig. 6, showing,, ~, and △, from about 6:% hours to about 18: 21 hours. It can be found from Fig. 7 that, for example, a3 reaches a value of about 0.87 at about ^ 50 hours, and remains above 0.8 at least until about 18:09 hours. It can also be found from FIG. 7 that, for example, ~ reaches a value of about 0.82 in about 17:52 hours, and remains at or south of about 0.8 at least until about 18:09 hours. Therefore, at about 17:52 hours, and then until at least about 18 ·· 09 hours, each of A and A * has a value of at least 0.8, and a value of at least 70 kg / m3, thinking This indicates the "loss of continuity I", starting at about P • 52 hours and then at least about 18:09 hours. At this time, the collapse of the fluidized bed was irreversible. Obtaining the "loss of continuity 1" indicates that excessive polymer mass formation occurred in the reactor, blocking it, and the production had to be stopped. The catalyst was implemented within 8 hours and 18 hours. Type 丨 all-static treatment ", and then closing the reactor and disassembling it. A large amount of polymerization products were lost due to the shutdown of the furnace. 6 · 2 Photo explanation, such as stabilizing Zhuangnengping This example illustrates how the Αη parameter indicates fluidization The stable state of the bed, 85552 -66- 200426156 operation, in a long continuous production period, after three days, the empty window period ,. The copolymer made from ethylene and butene-1 monomer was continuously produced in a gas fluidized bed reaction reactor as described in Example 61. IC5 was used as the condensing agent. The use of IC5 will increase the dew point temperature of the recycled mixture and allow a larger amount of heat to be removed from the fluidized bed; however, the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is used throughout this example. , Is kept at a temperature of about 15 ° C or more. The reactor bed temperature, which was approximately controlled throughout the three days, was about 87_2. (: To about 89. (TC. Tables 3 to 5 provide hourly averages of <△ / 〇, A !, A :, As, A *, and other important manufacturing parameters during three consecutive days of operation. Table 3¼ For the data of the first day, Table 4 provides the data for the second day, and Table $ provides the data for the third day. 85552 • 67 · 200426156 &gt; 'i J 5 &quot; Jie 1 22:00 21 «1 2000 1 19Λ0 ι 17:00 s 15.00 £ Lh ^ l ϋ! «ο &lt; 〇eft? Ok 8 ί • V i • ♦ Μ ^ Η: 锾 FT u 1 • J 5 fc utb Τ • ο & · 〇» τ b Γ t (Λ b AA Ιλ Γ Γ Γ \ o T «Τ U» agricultural rate ton / Ι · Η 1 II ii * 〇S is i 8 i F δ i P p ρ F ρ o \? pppo ρ ρ! : 5 0.01 «0.» 20 〇Λ1β po: 0.91 «0.010 0,919 0.910 0 Λ1β Ο 〇 〇.« 0 0.9ΐβ ο.βιβ o «&gt; 0.918 • o • 〇.β1β ρ ο ρ φ 1 o Vo A ο. βιβ P 0.β1 «po 0.010 〇 S Ρ I r ^ KJ i 21.02 .¾! ϋΐ 5 &quot; s 120.00 丨 20.96, 20.90 21.00 20.W One buckle ° 9 2, · 00 • s hi '8 if s 21.02 21.00 J0.W o 21.00 2101 ww i, 8 S Μ 8 F e • O ψ 3 0 F Μ SI u T ο 'ί 9 s 8 8 • ο ·· TF 3 5 e S ο 8 · 〇 [V ai Γ • o F fl Τ (Λ 〇F ▲ rb «&quot;! 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S 3J« S 3.2 «3.27 f 1 W 1 X 1 sew s.ree sw 1 5.§7β y1 8 57ββ s.wo »βα &lt; * 8 SK7 5.974 1 S.WJ0, &lt; 1 0.600 B | 0.51« 1 &lt; Μ · 1 0.522 0.SM osse 0351 1β ^! 0S «1 o.eoo ι |» I NI I ii 0.312 〇05 * 5 I1 0.521 〇-5'2 0.512 0.520 il · 05! Β ο S 0.514 0.517 0.5 ι 0.517 ®% 1 | a ρ l ~ □ 3 r 1— 0! A iT 5 〇a 3 t ο 8 1 o 2 I oip I 丨ΓΓ i &gt; 3: 芩 芩 芩 令 I ε 铖 丨 &gt; Ma Hong eggplant stir-fry 嬅 嬅 嬅 85 4 85552 • 68- 200426156 5 '•• r 85552 s · *:-* 5--5 ss 205 2050 2010 27 · 2 s * sw / t &gt; &gt; &gt; / iLit &lt; J «AW ^ T» »T)

Is &gt; &gt; &gt; &gt;, &gt; 55 ®% -69- 200426156 85552 -70- 200426156

It should be noted that the continuous operation of the operating room is only carried out before the day of collecting the data in Table 3, and on the day of collecting the data in Table 5 . It should be noted that the gas viscosity species is usually not measured. 彳 口 ## 你 你 | 4 ， Rarr Taili 1 Lane is used for example to calculate the X and Y values of Wu Guo Patent 5,436,304. The parameters are measured in a retrospective way by the Zuon computer software program, and are used for this purpose by those skilled in the art. As shown in Table 3, each of the 盥 a &gt; μμ 丄 合 is equal to 314 ~ ~ value, during the first day, never exceeded 0.45. Moreover, during the first day of the first month, A never exceeded 0.51, and during the first day, A? Never exceeded 0.55. Furthermore, it is possible for Yugong * to ^^ Λ, during the period of one day, when it is 30 kg / m3 or larger, at some time, it means 14: ㈨, 15: 00, and 16: 〇 〇Hours, each 丨 to ~ not more than 〇45. Except for 14: 00, 15, 00, and 16: 00 hours, when changing to the stable state 丨 丨 and 丨, and the warning state π, the bismuth system in the Kotoda field will be the first to be changed. ； # 士 # Τ, Spear Tendon at all other times, the operation is π stable state. "As shown by Tables 4 and 5, during the second and third days, the values of" each, to ~ ", Never exceeded G.55. During the second and third days, ^ has never equaled or exceeded 30 kg / m3, and on the second day of 6: QM, the maximum value obtained today is only 27 kg / m3 (See Table 4). Therefore, the operation is "stable" at all times of the first and second days.

Therefore, this example confirms the operation of the fluidized bed throughout the second and third days of the three-day period, and most of the "steady-state" operations during the first day of the period. Furthermore, during this three-day period, Provides continuous operation, even if the liquid-containing mixture introduced into the reaction zone contains a relatively high content by weight of liquid (based on the total weight of the circulating stream). For example, the liquid content in the circulating stream is One day, during the entire period from 10:00 to 24 · 00 hours, the system kept 85552-71- 200426156 higher than 20% by weight. During this period, it has a high value at 10: 00 hours. 23.8% by weight f% (see Table 3). Furthermore, the liquid content in the circulating stream is maintained at or above 20.8% by weight on the first day, and has a high value of 22.7 at π: 00 hours. Therefore, this example further provides fluidization, "stable state" operation, even when the liquid content in the circulating stream is relatively high, such as at least about 175% by weight, at least about 20% by weight or at least about 21.8% by weight. Moreover, with for example Recitations Patent 5,352,749 the contrary, in this example a positive penetration of FBD S SBD ratio (ratio ,, ") need not be maintained above 6.59 square fluidized bed in order to ensure the continuity of the polymerization process. For example, on the third day of continuous operation (see Table 5), the fluidized bed polymerization method of the present invention is continuously operated, especially from 2 • 00 to (and including) 20: 00 hours; in a continuous “steady state” Throughout the operation, the ratio was below 0.59. In fact, the ratio never exceeds 0.55 during the 18-hour period (see the 18: 00-hour line in Table 5). Furthermore, 'as opposed to, for example, US patent 5,436,304, this example proves that Z, meaning the so-called "bulk density function", need not be maintained at or above the calculated limit of the so-called body bifurcation function "(" Limit B " , Using Table B of US Patent 5,436,304, from the values of the parameters, χ ”and“ γ ”, to avoid destabilizing the fluidized bed. For example, on the third day of continuous operation (see Table 5), The fluidized bed polymerization method of the present invention is continuously operated during its entire day and in a continuous "steady state", and during operation, especially from 2: 00 to 20: 00 hours, ζ is below the limit B. 6 · 3 shows the continuous performance state #loss 2 This example is used to illustrate that the Δρ parameter indicates the change in the fluidized bed and its disintegration, / 85552 -72- 200426156 finally leads to "loss of continuity state 2", The reactor needs to be shut down. Manufactured in a gas slurry bed from a mixture containing about 395 mol% ethylene monomer, about 136 mol% butene-1 monomer, about 5.8 mol% hydrogen, and about 411 mol% nitrogen &lt;; During the copolymer period, certain factors may cause production stoppage and loss of process success. The mixture introduced into the reaction zone is essentially free of liquids, based on the total weight of the mounting &gt; tile, which means this method operates in dry mode. The catalyst used is a Ziegler-Natta type catalyst, including titanium trichloride and aluminum alkyl. The catalyst productivity was approximately 6,693 grams of polymer per gram of catalyst. A fluidized bed reactor apparatus similar to that described in Example 6.1 was used, and the following were developed. In this example, q is about 13.6 meters. The reaction tower is equipped with two measuring position η thermocouple devices, which are opposite to each other; each is positioned at about 001Q, which means about 152 mm above the surface of the distribution plate facing the fluidized bed. The reaction tower is also equipped with pressure ports Pi, P2 and p3, and the approximate positions are as follows: individually above the surface of the distribution plate facing the fluidized bed, 0.0HQ (about 151 mm), 0.20Q (about 2,74 mm) and 0.627 (^ (Approximately 8,530 Φm). The set point of the reactor bed temperature for approximately control is 88 ° C, which will cause the average controlled reactor bed temperature to be approximately 87.0 ° C to approximately 88.8 C. After a period of 12 hours, it ends at approximately 2 〇: 13 hours, which means immediately before the event starting at 20: 13 hours as discussed below. During this 12 hour period, the polymer production rate was about 24.5 metric tons / hour. Review of the data The analysis showed that several conditions existed before the operating parameter adjustment was performed at about 20 ... 15 hours. To be clear, the analysis found that during the period of about 24 hours immediately before 20:13 hours, the copolymer M] [top Causes several kinds of changes, meaning 2.0 to 1.0 · 2.0, and finally returns to ι · 〇. Furthermore, there are indications that the hydrogen-sensing SS4 sensor reading is incorrect. T 85552 -73- 200426156 Application area ^ middle ° This electrostatic agent control system may have water added to the reaction chamber unintentionally. In about 20: 30 hours At present, LBD is approaching UBD. Figure 8 shows LBD, UBD, and &lt; graphs, which have gone from about 20 ·· 13 to about 21 ·· 13 hours. 82, As and A * No corresponding values are available for review. Analysis. It can also be seen from Figure 8 that the Δ / 〇 value is non-negative and is less than about 10 kg / m3, from about 20 • 31 to about 20: 35 hours, and from about 20 ·· 42 to about 20: 44 Hours. During at least the interval, meaning from about 20 ·· 31 to about 20 ·· 35 hours, the value shows a π Δρ alarm state. In addition, it can be found from Figure 8 that, for example, at about 20.0 hours It reaches a value of about 0 kg / m3, and remains substantially lower than 0 kg / m3, until at least about 21:13 hours, which means that the loss of continuity is 2 ,. At 20: 50 In the next hour, due to the implementation of the π type I total static treatment of the catalyst, the enemy stopped the polymerization reaction. Then, the reactor system was purged to remove the carbon monoxide catalyst poison and restore the flow of ethylene and butylene-1. Then, the catalyst was introduced again. Then, the SGV dropped from about 0.7 to about 0 68 m / s, and the distribution plate Aρ increased from about 2,500 to about 3, 100 millimeters of water. This results in a difference in the properties of the fluidized bed below and above. At about 28 kg / m3, for example at 20:53 hours. These changes in LBD, UBE) and above can be seen from the data plotted in Figure 8.

At about 20: 15 W, 卩 ~ ττ _ J, because the static charge is accumulated in the reaction tower, the electrostatic agent control system is started, and the… This system is customary, so it is not shown in Figure 1. For 4, the content of the system is connected to the pipeline 8 and enters the "Alarm state" at approximately 21: 02 hours. . However, this 85552 -74- 200426156 state of sorrow did not reach 'because' Δρ 'remained negative until about 2i: 13 hours. Therefore, at about 20: 49 hours, and then until at least about 21: 13 hours As of now, ΔP has a value below 0 kg / m3, which means from about 20:49 hours, and then until at least about 21:13 hours, indicating "loss of continuity state 2". At this time, fluidization The disintegration of the bed was irreversible. The loss of "continuous state 2" showed that excessive polymer lumps had formed in the reactor, blocking it, and production had to be stopped. The compressor was shut down at 53 hours, then the reactor was shut down and disassembled. A large amount of polymerization products were lost due to the shutdown. All publications and patent applications are incorporated herein by reference to the same extent as if each individual publication or patent application was explicitly and individually shown and incorporated herein by reference. All concentrations herein are by weight unless otherwise indicated. That is, although the present invention has been described with reference to specific embodiments, it should be understood that various changes and modifications can be made without departing from the spirit or scope of the invention. [Brief description of the formula] Figure 1 shows a non-limiting schematic group of a typical commercial fluidized-bed reactor polymerization unit. "A non-limiting simplified schematic diagram of the typical temperature and pressure measurement location of a polymerization unit. Figure 2b shows the fluidization of the polymerization unit." Sectional view of a thermocouple (position) plane 3 made in the bed area 'Explanation — a specific embodiment in which the four-good 1-position device is only qualitatively spaced around its circumference in a radial manner. 85552 -75- 200426156 Figure 3 shows the graphs of LBD, UBD, fluidized bed height, bed weight, and neck ΔP for example 6.1 over a period of time from '18 .τ + • w hours to hours after. Figure 4 shows a graph of LBD, ubd, and Λ vs. time for Example 6.1 from about 8:09 hours to about 18:21 hours. Figure 5 shows LBD, UBD, and pairing of 6.1 for Example 6.1 The graph is from about 16.50 hours to about 18: 21 hours. Figure 6 shows the As, A # and Δρ versus time, and J &lt; patterns for Example 6.1, from about 8 • 09 hours to about is: 21 hours. 7 shows that A3, A4, and Δρ for time, Shape, from • 50 hours to about 18: 21 hours., 'Scoop 6 Figure 8 shows the LBD and UBD of Example 6.3 and the time period from about 20: 13 hours to about 21: 13 hours. Explanation of the symbols of the formula 2 Reaction zone 4 Expansion zone 6 Fluidized bed 8 Pipe 8A Pipe 10A Source 10B Source 12 Pipe 13 Pipe 14 Source 85552 -76- 200426156 16 Pipe 18A Source 18B Source 20 Source 21 Source 22A Source 22B Source 24 Line 26 Compressor 28 Condenser / heat exchanger 30 Turning plate 32 Distribution plate 34 Line 36 Drain tank 38 Valve 40 Tank 42 Valve 44 Source 85552 -77-

Claims (1)

200426156 Scope of patent application: 1. A continuous gas fluidized bed method for producing polymers characterized by a condensing agent in a circulating flow, comprising: a controlled bed temperature, a fluidized bed density below, Upper fluidized bed density and multiple measurement positions: In the reaction zone of ^ temperature, in the presence of a catalyst, a gas stream containing monomer and condensing agent is continuously passed through the fluidized bed; the polymerization product is taken out from the reaction zone, and contains A gas stream of unreacted gas; recirculate this gas stream and a sufficient amount of additional monomers to the reaction zone to replace the monomers polymerized and separated by the polymerization product; cool the circulating stream to condense one of them And formed a liquid-containing mixture having a circulating flow dew point temperature, a reactor inlet temperature, and a weight ratio of about 17.5% to about 70% liquid, based on the total weight of the cooled circulating flow, in which the controlled reaction The difference between the bed temperature of the device and the circulating dew point temperature of the mixture is greater than or equal to about 5 ° C; and the introduction of the mixture into the reaction zone, where the liquid in the mixture is vaporized; △) 〇 meets the condition of 0 kg / m3 $ △! 〇 &lt; 70 kg / m3, and when Δρ ^ 10 kg / m3, at least one critical number of An simultaneously meets 0.25 S An &lt; 0.8 Conditions; and where Δρ is equal to (lower fluidized bed density) minus (upper fluidized bed density), and (controlled reactor bed temperature)-(measured position η temperature) Αη = (controlled reactor bed temperature) -(Reactor inlet temperature). 2. The continuous gas fluidized bed method according to item 1 of the scope of patent application, wherein the poly 85552 200426156 compound is a poly hydrocarbon. 3. The continuous gas fluidized bed method according to item 2 of the patent application scope, wherein the liquid-containing mixture contains at least about 20% by weight of liquid, based on the total weight of the cooled circulating flow. 4. The continuous gas fluidized bed method according to item 2 of the patent application, wherein the liquid-containing mixture contains at least about 21.8% by weight of liquid, based on the total weight of the cooled circulating flow. 5. The continuous gas fluidized bed method according to item 2 of the scope of patent application, wherein the monomer is ethylene, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the liquid-containing mixture contains at least about 21.8 % Liquid weight ratio, based on the total weight of the cooled circulating stream. 6. The continuous gas fluidized bed method according to item 5 of the patent application scope, wherein the controlled reactor bed temperature is about 105 ° C to about 110 ° C. 7. The continuous gas fluidized bed method according to item 2 of the patent application, wherein the monomers are ethylene and butene-1, the controlled reactor bed temperature is about 80 ° C to about 95eC, and the liquid-containing mixture contains A liquid weight ratio of about 17.5% to about 40% based on the total weight of the cooled circulating stream. 8. The continuous gas fluidized bed method according to item 7 of the patent application scope, wherein the controlled reactor bed temperature is about 80 ° C to about 90 ° C. 9. Continuous gas fluidized bed method according to item 2 of the patent application, wherein the monomers are ethylene and hexene-1, the temperature of the controlled reactor bed is about 78 ° C to about 90 ° C, and the mixture contains a liquid Contains at least about 17.5% liquid to weight ratio based on the total weight of the cooled circulating stream. 10. The continuous gas fluidized bed method according to item 2 of the patent application, in which the single 85552 200426156 body is ethylene and hexene-1, the controlled reactor bed temperature is about 100 ° C to about 110 ° c, and it contains liquid The mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 11. The continuous gas fluidized bed method according to item 2 of the patent application, wherein the monomer is propidium. 12. The continuous gas fluidized bed method according to item 2 of the patent application, wherein the monomers are propylene and butene-1. 13. The continuous gas fluidized bed method according to item 2 of the scope of the patent application, wherein the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is greater than or equal to about 1 (TC. 14. According to the patent application The continuous gas fluidized bed method of the scope item 13, wherein the liquid-containing mixture contains at least about 20% by weight of the liquid, based on the total weight of the cooled circulating stream. 15. The continuous gas flow according to the scope of claim 13 of the patent application A fluidized bed method in which the liquid-containing mixture contains at least about 21.8% by weight of liquid, based on the total weight of the recycled stream. 16. The continuous gas fluidized bed method according to item 13 of the patent application scope, wherein The body is ethylene, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the liquid-containing mixture contains at least about 21.8% by weight of liquid, based on the total weight of the cooled circulating stream. 17. According to the application The continuous gas fluidized bed method according to item 16 of the patent, wherein the controlled reactor bed temperature is about 105 ° C to about 110 ° C. 18. The continuous gas fluidized bed method according to item 13 of the application, The monomers are ethylene and butene-1, the controlled reactor bed temperature is about 80 ° C to about 95 ° C / 85552 200426156, and the liquid-containing mixture contains about 17.5% to about 40% liquid by weight, with cooling The total weight of the circulating stream is the basis. 19. The continuous gas fluidized bed method according to item 18 of the scope of the patent application, wherein the controlled reactor bed temperature is about 80 ° C to about 90 ° C. The continuous gas fluidized bed method of item 13, wherein the monomers are ethylene and hexene-1, the controlled reactor bed temperature is about 78 ° C to about 90 ° C, and the liquid-containing mixture contains at least about Π.5% The weight ratio of liquid is based on the total weight of the cooled circulating stream. 21. The continuous gas fluidized bed method according to item 13 of the patent application scope, wherein the monomers are ethylene and hexene-1, and the controlled reactor bed temperature is About 100 ° C to about 110 ° C, and the liquid-containing mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 22. Continuous gas flow according to item 13 of the scope of the patent application Chemical bed method in which the monomer is propylene. According to item 13 of the scope of patent application Continuous gas fluidized bed method, the monomers in the ash are propylene and butene-1. 24. The continuous gas fluidized bed method according to item 2 of the patent application scope, wherein the controlled reactor bed temperature and the circulating flow dew point of the mixture The difference between the temperatures is greater than or equal to about 15 ° C. 25. The continuous gas fluidized bed method according to item 24 of the scope of the patent application, wherein the liquid-containing mixture contains at least about 20% liquid by weight in a cooled circulating stream The total weight is the basis. 26. The continuous gas fluidized bed method according to item 24 of the application, wherein the liquid-containing mixture contains at least about 21.8% by weight of the liquid, based on the total weight of the cooled / 85552 200426156 circulating flow. . 27. The continuous gas fluidized bed method according to item 24 of the application, wherein the monomer is ethylene, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the liquid-containing mixture contains at least about 21.8% The liquid weight ratio is based on the total weight of the cooled circulating stream. 28. The continuous gas fluidized bed method according to item 27 of the patent application, wherein the controlled reactor bed temperature is about 105 ° C to about 110 ° C. 29. The continuous gas fluidized bed method according to item 24 of the patent application, wherein the monomers are acetamidine and butene-1, the controlled reactor bed temperature is about 80 ° C to about 95 ° C, and The mixture contains from about 17.5% to about 40% by weight of liquid, based on the total weight of the cooled circulating stream. 30. The continuous gas fluidized bed method according to item 29 of the application, wherein the controlled reactor bed temperature is about 80 ° C to about 90 ° C. 31. The continuous gas fluidized bed method according to item 24 of the patent application, wherein the monomers are acetamidine and hexene-1, the temperature of the controlled reactor bed is about 78 ° C to about% ° C, and The mixture contains at least about 17.5% by weight of liquid based on the total weight of the cooled circulating stream. 32. The continuous gas fluidized bed method according to item 24 of the patent application, wherein the monomers are ethylene and hexene-1, and the controlled reactor bed temperature is about 100 ° C to about 110 ° C. (: And the liquid-containing mixture contains at least about 20% by weight of liquid, based on the total weight of the cooled circulating stream. 33. The continuous gas fluidized bed method according to item 24 of the patent application, wherein the monomer is propylene 34. The continuous gas fluidized bed method according to item 24 of the scope of patent application, in which 85552 200426156 monomers are propylene and butene-1. 35.-a kind of manufacturing polymer characterized by a condensing agent in the circulating stream Continuous gas fluidized bed method, comprising: in a reaction zone having a controlled reactor bed temperature, a lower fluidized bed density, an upper fluidized bed density, and a plurality of measurement positions 11 temperatures, in the presence of a catalyst, The gas stream containing monomer and condensing agent continuously passes through the fluidized bed; the polymerization product is taken out from the reaction zone, and the gas stream containing unreacted gas is recycled; this gas stream and a sufficient amount of other monomers are recycled to the reaction zone to replace Monomers that have been polymerized and are separated by the polymerization product; this circulating stream is cooled to condense a portion of it and form a liquid-containing mixture with a circulating stream dew point temperature, a reactor inlet And the weight ratio of liquid containing about 17.5% to about 70%, based on the total weight of the cooled circulating stream, where the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is greater than or equal to 5 ° C; and. Introducing the mixture into the reaction zone, where the k-body in the mixture is vaporized; wherein Δρ satisfies the condition of 10 kg / m3 &lt; 30 kg / m3, and at least one threshold of η The number satisfies the condition of 0.25 $ Αη &lt;0.55; and Δρ is equal to (lower fluidized bed density) minus (upper fluidized bed density), and (controlled reactor bed temperature)-(measured position η temperature) Αη = (Controlled reactor bed temperature, M reactor inlet temperature). 36. The continuous gas fluidized bed method according to item 35 of the patent application, in which 85552 200426156 polymer is polyolefin. Item of the continuous gas fluidized bed method, wherein the liquid-containing mixture contains at least about 20% liquid by weight, based on the total weight of the cooled circulating stream. 38. Continuous according to item 36 of the scope of patent application Bulk fluidized bed method, wherein the liquid-containing mixture contains at least about 21.8% by weight of liquid, based on the total weight of the cooled circulating stream. 39. The continuous gas fluidized bed method according to item 36 of the patent application, wherein The body is ethylene, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the liquid-containing mixture contains at least about 21.8% by weight of liquid, based on the total weight of the cooled circulating stream. 40. According to the application The continuous gas fluidized bed method of item 36 of the patent, wherein the monomers are ethylene and butene-1, the controlled reactor bed temperature is about 80 ° C to about 95 ° C, and the liquid-containing mixture contains about 17.5% To about 40% liquid by weight, based on the total weight of the cooled circulating stream. ~ 41. The continuous gas fluidized bed method according to item 36 of the patent application, wherein the monomers are ethylene and hexane-1, the temperature of the controlled reactor bed is about 78 ° C to about 90 ° C, and The mixture contains at least about 17.5% by weight of liquid based on the total weight of the cooled circulating stream. 42. The continuous gas fluidized bed method according to item 36 of the application, wherein the monomers are ethylene and hexene-1, the temperature of the controlled reactor bed is about 100 ° C to about 110 ° C, and the liquid The mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 43. The continuous gas fluidized bed method according to item 36 of the patent application, wherein / 85552 200426156 monomer is propylene. 44. The continuous gas fluidized bed method according to item 36 of the patent application, wherein the monomers are propane and butan τ -1. 45. The continuous gas fluidized bed method according to item 36 of the application, wherein the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is greater than or equal to about 10 ° C. 46. The continuous gas fluidized bed method according to item 45 of the patent application, wherein the liquid-containing mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 47. The continuous gas fluidized bed method according to item 45 of the patent application, wherein the liquid-containing mixture contains at least about 21.8% by weight of liquid, based on the total weight of the cooled circulating stream. 48. The continuous gas fluidized bed method according to item 45 of the application, wherein the monomer is ethylene, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the liquid-containing thirst compound contains at least about 21.8% liquid weight ratio, based on the total weight of the cooled circulating stream. 49. The continuous gas fluidized bed method according to item 45 of the patent application, wherein the monomers are ethylene and butylene-1, the temperature of the controlled reactor bed is about 80 ° C to about 95 ° C, and the mixture contains a liquid Contains about 17.5% to about 40% liquid by weight based on the total weight of the cooled circulating stream. 50. The continuous gas fluidized bed method according to item 45 of the patent application, wherein the monomers are acetamidine and hexene-1, the controlled reactor bed temperature is about 78 ° C to about 90 ° C, and The mixture contains at least about 17.5% by weight of liquid based on the total weight of the cooled circulating stream. r 85552 200426156 51. The continuous gas fluidized bed method according to item 45 of the scope of patent application, wherein the monomers are ethene and hexene-1, and the controlled reactor bed temperature is about 100 ° C to about 110 ° C, and The liquid-containing mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 52. The continuous gas fluidized bed method according to item 45 of the application, wherein the monomer is propylene. 53. The continuous gas fluidized bed method according to item 45 of the application, wherein the monomers are propylene and butene-1. 54. The continuous gas fluidized bed method according to item 36 of the application, wherein the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is greater than or equal to about 15 ° C. 55. The continuous gas fluidized bed method according to item 54 of the application, wherein the liquid-containing mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 56. According to the continuous gas fluidized bed method of item 54 of the scope of the patent application, the mixture of Mozambique-containing liquid contains at least about 21.8% by weight of liquid, based on the total weight of the cooled circulating stream. 57. The continuous gas fluidized bed method according to item 54 of the application, wherein the monomer is ethylene, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the liquid-containing mixture contains at least about 21.8% liquid weight ratio, based on the total weight of the cooled circulating stream. 58. The continuous gas fluidized bed method according to item 54 of the patent application, wherein the monomers are acetamidine and butene-1, the controlled reactor bed temperature is about 80 ° C to about 95 ° C, and The mixture contains about 17.5% to about 40% liquid by weight, 85552 200426156 based on the total weight of the cooled circulating stream. 59. The continuous gas fluidized bed method according to item 54 of the application, wherein the monomers are ethylene and hexene-1, the controlled reactor bed temperature is about 78 ° C to about 90t, and the liquid-containing mixture contains at least About 17.5% weight ratio of liquid, based on the total weight of the cooled circulating stream. 60. The continuous gas fluidized bed method according to item 54 of the application, wherein the monomers are ethylene and hexene-1, and the temperature of the controlled reactor bed is about 10 (TC to about 110 ° C, and the mixture contains a liquid Contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 61. The continuous gas fluidized bed method according to item 54 of the patent application, wherein the monomer is propylene. 62. According to the patent application The continuous gas fluidized bed method of item 54, wherein the monomers are propylene and butene-1. 63. A continuous gas fluidized bed method for manufacturing a polymer and characterized by a condensing agent in a circulating flow, comprising: In a reaction zone with a controlled reactor bed temperature, a lower fluidized bed density, an upper fluidized bed density, and a plurality of measurement positions n temperatures, a gas stream containing monomers and condensing agents is continuously passed in the presence of a catalyst Fluidized bed; take out the polymerization product from the reaction zone, and a gas stream containing unreacted gas; recycle this gas stream and a sufficient amount of additional monomers into the reaction zone to replace the polymerized and polymerized product being withdrawn Monomer; make this Circulating cooling to condense a portion of it and forming a liquid-containing mixture, which has a circulating flow dew point temperature, a reactor inlet temperature, and a weight ratio of liquid containing about Π.5% to about 70%, based on the cooled circulating flow. Total -10-85552 200426156 weight as the basis, where the difference between the controlled reactor bed temperature and the circulating dew point temperature of the mixture is greater than or equal to about 5 ° C; and the mixture is introduced into the reaction zone, where the The vaporization of the liquid in the mixture; wherein Δ / 〇 satisfies the condition of 30 kg / m 3 $ Δρ &lt; 40 kg / m3, and at least one critical number of Δη satisfies the condition of 0.55 $ Αη &lt;0.6; Is equal to (lower fluidized bed density) minus (upper fluidized bed density), and (controlled reactor bed temperature)-(measured position 11 temperature) An =-(controlled reactor bed temperature)-(reactor Inlet temperature) 64. The continuous gas fluidized bed method according to item 63 of the patent application, wherein the monomer is acetam, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the mixture contains a liquid Contains at least about 21.8% The weight ratio of liquid is based on the total weight of the cooled circulating stream. 65. The continuous gas fluidized bed method according to item 63 of the patent application, wherein the monomers are acetamidine and butene-1, and the temperature of the reactor bed is controlled. It is about 80 ° C to about 95 ° C, and the liquid-containing mixture contains about 17.5% to about 40% by weight of liquid, based on the total weight of the cooled circulating flow. 66. Continuous according to item 63 of the scope of patent application Gas fluidized bed method, wherein the monomers are acetamidine and hexene-1, the controlled reactor bed temperature is about 78 ° C to about 90 ° C, and the liquid-containing mixture contains at least about 17.5% liquid to weight ratio, The total weight of the cooled circulating stream is the basis. ㈤ 67. The continuous gas fluidized bed method according to item 63 of the patent application, wherein the monomers of 85552-11-200426156 are ethylene and hexene-1, and the controlled reactor bed temperature is about 100 ° C to about lio ° C And the liquid-containing mixture contains at least about 20% liquid by weight, based on the total weight of the cooled circulating stream. 68. The continuous gas fluidized bed method according to item 63 of the application, wherein the monomer is propidium. 69. The continuous gas fluidized bed method according to item 63 of the application, wherein the monomers are propylene and butene-1. 70. A continuous gas fluidized bed method for manufacturing a polymer characterized by a condensing agent in a circulating stream, comprising: a controlled bed temperature, a lower fluidized bed density, an upper fluidized bed density and In a plurality of reaction zone measuring temperature, in the presence of a catalyst, a gas stream containing monomer and condensing agent is continuously passed through a fluidized bed; a polymerization product is taken out from the reaction zone and a gas stream containing unreacted gas; The gas stream and a sufficient amount of additional monomers are recycled to the reaction zone to replace the monomers that have been polymerized and removed as polymerized products; 'Cool this circulating stream to condense a portion of it and form a liquid containing A mixture having a circulating flow dew point temperature, a reactor inlet temperature, and a weight ratio of about 17.5% to about 70% liquid, based on the total weight of the cooled circulating flow, wherein the controlled reactor bed temperature and the circulation of the mixture The difference between the dew point temperature is greater than or equal to about 5 ° C; and the mixture is introduced into the reaction zone, where the liquid in the mixture is vaporized; and at the same time, Δρ is 40 kg / m3 $ Δρ &lt; 50 kg / m3 condition, and at least one critical number of Αη satisfies 0.6 $ t 85552 -12- 200426156 Αη &lt; 0 · 7 condition; and Δρ is equal to (lower fluidized bed density) minus Go to (upper fluidized bed density), and (controlled reactor bed temperature)-(measured position η temperature) Αη =-(controlled reactor bed temperature M reactor inlet temperature). 71. The continuous gas fluidized bed method according to item 70 of the application, wherein the monomer is acetam, the controlled reactor bed temperature is about 100 ° C to about 115 ° C, and the liquid-containing mixture contains at least about 21.8 % Liquid weight ratio, based on the total weight of the cooled circulating stream. 72. The continuous gas fluidized bed method according to item 70 of the application, wherein the monomers are ethylene and butene-1, the controlled reactor bed temperature is about 80 ° C to about 95 ° C, and the liquid-containing mixture contains A liquid weight ratio of about 17.5% to about 40% based on the total weight of the cooled circulating stream. 73. The continuous gas fluidized bed method according to item 70 of the application, wherein the monomers are ethylene and hexene-1, the temperature of the controlled reactor bed is about 78 ° C to about 90 ° C, and the mixture contains a liquid Contains at least about 17.5% liquid to weight ratio based on the total weight of the cooled circulating stream. 74. The continuous gas fluidized bed method according to item 70 of the patent application, wherein the monomers are ethylene and hexene-1, the temperature of the controlled reactor bed is about 100 ° C to about 110 ° C, and contains liquid The mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. 75. The continuous gas fluidized bed method according to claim 70, wherein the monomer is propylene. m. 76. The continuous gas fluidized bed method according to item 70 of the application, wherein 85552 -13- 200426156 monomers are propylene and butene-1. 77. A continuous gas fluidized bed method for manufacturing a polymer and characterized by a condensing agent in a circulating flow, comprising: a controlled reactor bed temperature, a lower fluidized bed density, an upper fluidized bed density and In a plurality of reaction zone measuring temperature, in the presence of a catalyst, a gas stream containing monomer and condensing agent is continuously passed through a fluidized bed; a polymerization product is taken out from the reaction zone and a gas stream containing unreacted gas; The gas stream and a sufficient amount of additional monomers are recycled to the reaction zone to replace the monomers polymerized and separated by the polymerization product; the circulating stream is cooled to condense a portion thereof and form a liquid-containing mixture , Which has a circulating flow dew point temperature, a reactor inlet temperature, and a weight ratio of liquid containing about 17.5% to about 70%, based on the total weight of the cooled circulating flow, wherein the controlled reactor bed temperature and the circulating flow of the mixture The difference between the dew point temperature is greater than or equal to about 5 ° C; and. The mixture is introduced into the reaction zone, where the vaporization of the mixture in the mixture is vaporized; and at the same time Δρ satisfies 50 kg / m3 Δρ &lt; 70 kg / m3, and at least one critical number of Aη satisfies the condition of 0.7 $ Αη &lt;0.8; and Δρ is equal to (lower fluidized bed density) minus (upper fluidized bed density), And (controlled reactor bed temperature)-(measured location temperature) Αη = (controlled reactor bed temperature)-(reactor inlet temperature). 78. The continuous gas fluidized bed method according to item 77 of the patent application, wherein -14- 85552 200426156 monomer is ethylene, the temperature of the controlled reactor bed is about 100 ° C to about 115 ° c, and the mixture contains a liquid Contains at least about 21.8% liquid by weight based on the total weight of the cooled circulating stream. 79. The continuous gas fluidized bed method according to item 77 of the application, wherein the monomers are ethylene and butene-1, the temperature of the controlled reactor bed is about 80 ° C to about 95 ° C, and the mixture contains a liquid Contains about 17.5% to about 40% liquid by weight based on the total weight of the cooled circulating stream. 80. The continuous gas fluidized bed method according to item 77 of the application, wherein the monomers are ethylene and hexene-1, the temperature of the controlled reactor bed is about 78 ° C to about 90 ° C, and the mixture contains a liquid Contains at least about 17.5% liquid to weight ratio based on the total weight of the cooled circulating stream. 81. The continuous gas fluidized bed method according to item 77 of the application, wherein the monomers are ethylene and hexene-1, the controlled reactor bed temperature is about 100 ° C to about 110 ° C, and the liquid The mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. ~ 82. The continuous gas fluidized bed method according to item 77 of the application, wherein the monomer is propylene. 83. The continuous gas fluidized bed method according to item 77 of the application, wherein the monomers are propylene and butylene-1. 84. A continuous gas fluidized bed method for manufacturing a polymer characterized by a condensing agent in a circulating flow, comprising: a controlled reactor bed temperature, a lower fluidized bed density, an upper fluidized bed density and In the reaction zone measuring temperature at multiple locations, in the presence of a catalyst, a gas stream containing monomers and a condensing agent is continuously passed through the fluidized bed; t 85552 -15-200426156 Polymerization products are taken out from the reaction zone, and unreacted A gas stream; recycling this stream and a sufficient amount of additional monomers to the reaction zone to replace the polymerized monomers that have been polymerized and withdrawn as polymerization products; cooling the circulating stream to condense a portion of it, A liquid-containing mixture is formed, which has a circulating flow dew point temperature, a reactor inlet temperature, and a weight ratio of about 17.5% to about 70% liquid, based on the total weight of the cooled circulating flow, which is controlled in the reactor bed. The difference between the temperature and the circulating dew point temperature of the mixture is greater than or equal to about 5 ° C; and the mixture is introduced into the reaction zone, where the liquid in the mixture is vaporized; where Δρ satisfies 0 Kg / m3 $ Δρ &lt; 10 kg / m3, and where it is equal to (lower fluidized bed density) minus (upper fluidized bed density). 85. The continuous gas fluidized bed method according to item 84 of the application, wherein the monomer is olefin, the temperature of the controlled reactor bed is about 100 ° C to about 115 ° C, and 1 the liquid-containing mixture contains at least about 21.8 % Liquid weight ratio, based on the total weight of the cooled circulating stream. 86. The continuous gas fluidized bed method according to item 84 of the application, wherein the monomers are ethylene and butene-1, the temperature of the controlled reactor bed is about 80 ° C to about 95 ° C, and the mixture contains a liquid Contains about 17.5% to about 40% liquid by weight based on the total weight of the cooled circulating stream. 87. The continuous gas fluidized bed method according to item 84 of the application, wherein the monomers are ethylene and hexene-1, the temperature of the controlled reactor bed is about 78 ° C to about 90 ° C, and the mixture contains a liquid Contains at least about 17.5% by weight of liquid, based on the total weight of the cooling cycle of -16- 85552 200426156. 88. The continuous gas fluidized bed method according to item 84 of the application, wherein the monomers are ethylene and hexene-1, the temperature of the controlled reactor bed is about 100 Ό to about 110 ° C, and the liquid-containing mixture contains at least About 20% liquid weight ratio, based on the total weight of the cooled circulating flow. 89. The continuous gas fluidized bed method according to claim 84, wherein the monomer is propylene. 90. The continuous gas fluidized bed method according to item 84 of the application, wherein the monomers are propidium and Ding Jin τ -1. 91. A continuous gas fluidized bed method for manufacturing a polymer characterized by a condensing agent in a circulating stream, comprising: having a controlled reactor bed temperature, a lower fluidized bed density, an upper fluidized bed density and more In the reaction zone measuring the temperature of the position, in the presence of the catalyst, the gas stream containing the monomer and the condensing agent is continuously passed through the fluidized bed; the polymerization product is taken out from the reaction zone and the gas containing unreacted gas is charged; Recirculate this gas stream and a sufficient amount of additional monomers to the reaction zone to replace the monomers that have been polymerized and separated as polymerized products; cool the recycle stream to condense a portion of it and form a liquid-containing A mixture having a circulating flow dew point temperature, a reactor inlet temperature, and a weight ratio of about 17.5% to about 70% liquid, based on the total weight of the cooled circulating flow, wherein the controlled reactor bed temperature and the circulation of the mixture The difference between the dew point temperature is greater than or equal to about, and the mixture is introduced into the reaction zone, where the liquid in the mixture is vaporized; -17- 85552 200426156, where Δρ satisfies l Kg / m3 &lt; 70 kg / m3, and at least one critical number of An satisfies the condition of 0.25 $ Αη &lt; 0 · 8; and Δρ is equal to (lower fluidized bed density) minus ( Upper fluidized bed density), and (controlled reactor bed temperature)-(measured location temperature) Αη = -------- (controlled reactor bed temperature)-(reactor inlet temperature). 92. The continuous gas fluidized bed method according to item 91 of the application, wherein the monomer is ethylene, the controlled reactor bed temperature is about 1000C to about nyc, and the liquid-containing mixture contains at least about 21.8% liquid The weight ratio is based on the total weight of the cooled circulating stream. 93. The continuous gas fluidized bed method according to item 91 of the scope of the patent application, in which the monomers are acetamidine and diamidine-1, and the temperature of the controlled reactor bed is about 80 ° C to about 95 ° C. The mixture contains from about 17.5% to about 40% by weight of liquid, based on the total weight of the cooled circulating stream. 94. The continuous gas fluidized bed method according to item 91 of the application, wherein the monomers are ethylene and hexene, and the controlled reactor bed temperature is about 78. 0 to about 900 c / 'and the liquid-containing mixture contains at least about 17.5% liquid by weight based on the total weight of the cooled circulating stream. 95. The continuous gas fluidized bed method according to item 91 of the patent scope of the patent, wherein the monomers are ethylene and ethyl, and the temperature of the controlled reactor bed is from about 100 to about 1100. And the liquid-containing mixture contains at least about 20% liquid by weight based on the total weight of the cooled circulating stream. Go to 96. The continuous gas fluidized bed method according to item 91 of the patent application, wherein 85552 200426156 monomer is propylene. 97. The continuous gas fluidized bed method according to item 91 of the application, wherein the monomers are propidium and butene-1. 98. A method for monitoring and providing continuity in a continuous gas fluidized bed method in which polymers are characterized by a condensing agent in a circulating stream, comprising: monitoring a fluidized bed reaction zone, wherein the reaction zone With controlled reactor bed temperature, lower fluidized bed density, upper fluidized bed density and temperature at multiple measurement positions, monitor the circulating flow into the reaction zone, where the gas flow has the reactor inlet temperature; determine Δρ, and Compared with at least one limit, where Δρ is equal to (lower fluidized bed density) minus (upper fluidized bed density); and when Δρ-10 kg / m3, multiple Αη is measured, and each Αη is lower than Comparison of several numbers and higher values, where ~ (controlled reactor bed temperature)-(measured position temperature) Αη =-(controlled reactor bed temperature)-(reactor inlet temperature). 99. The method according to item 98 of the scope of patent application, in which there are four measurement positions η temperature. 100. The method according to item 98 of the patent application scope, in which there are 16 measurement positions η temperature. -19- 85552