[go: up one dir, main page]

WO2005061554A1 - Procede et dispositif de fabrication de polyolefines - Google Patents

Procede et dispositif de fabrication de polyolefines Download PDF

Info

Publication number
WO2005061554A1
WO2005061554A1 PCT/JP2004/019166 JP2004019166W WO2005061554A1 WO 2005061554 A1 WO2005061554 A1 WO 2005061554A1 JP 2004019166 W JP2004019166 W JP 2004019166W WO 2005061554 A1 WO2005061554 A1 WO 2005061554A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
phase polymerization
pressure
monomer
polymerization vessel
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2004/019166
Other languages
English (en)
Japanese (ja)
Inventor
Yasunobu Kaneko
Takamichi Matsumura
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Idemitsu Kosan Co Ltd
Original Assignee
Idemitsu Kosan Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Idemitsu Kosan Co Ltd filed Critical Idemitsu Kosan Co Ltd
Publication of WO2005061554A1 publication Critical patent/WO2005061554A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/0007—Pressure measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours

Definitions

  • the present invention relates to a method for producing polyolefin and an apparatus for producing the same, and more particularly, to producing polyolefin using a gas-phase polymerization reactor, the polyolefin is supplied to a heat exchanger according to the pressure in the vapor-phase polymerization reactor. And an apparatus for producing a polyolefin that can stably and effectively control the pressure and temperature in a gas-phase polymerization vessel by changing the inflow of cooling water, thereby enabling stable production of polyolefin. .
  • a polyolefin gas-phase polymerization reactor (appropriately abbreviated as a gas-phase polymerization reactor) are adjusted so that each of the pressure and the temperature becomes a constant value suitable for the polymerization reaction.
  • a stable operation of the gas phase polymerization reactor can be achieved, and a stable quality polyolefin can be produced.
  • a raw material monomer gas is extracted from the gas-phase polymerization reactor, and the monomer gas is cooled or cooled by heat exchange and then returned to the gas-phase polymerization reactor again. By doing so, the heat of polymerization is removed.
  • the pressure may fluctuate largely due to a strong state change in a gas phase polymerization vessel, and the stability of temperature control is not always good.
  • a large temperature change in the gas-phase polymerization reactor is required.
  • a sufficient temperature control function could not be exhibited.
  • Patent Document 1 discloses the following technology. That is, in producing polyolefin using a gas phase polymerization vessel, the temperature in the gas phase polymerization vessel is supplied to the gas phase polymerization vessel by vaporizing a part or the entire amount of the raw material monomer, and is supplied from the inside of the gas phase polymerization vessel. The monomer gas is withdrawn, cooled, liquefied, returned to the gas phase polymerization vessel, and controlled by adjusting the flow rate of the liquefied monomer returned to the gas phase polymerization vessel.
  • the polyolefin is characterized in that the pressure in the gas phase polymerization vessel is controlled by adjusting the gas flow rate of the raw material monomer supplied to the gas phase polymerization vessel and the flow rate of the monomer gas extracted from the gas phase polymerization vessel.
  • the technology of the manufacturing method is disclosed.
  • the temperature controllability in the gas phase polymerization reactor was significantly improved.
  • Patent Document 1 Japanese Patent Application Laid-Open No. 11 209415 (Claims 1, 2, 3, 4, Figure 1)
  • the pressure in the gas phase polymerization reactor is mainly controlled by increasing or decreasing the supply amount of the raw material monomer, increasing or decreasing the supply amount of the catalyst, and extracting the monomer gas to the outside of the system.
  • the temperature in the gas phase polymerization vessel is heated by the polymerization heat of the polypropylene, and is cooled by the heat of vaporization of the liquid monomer refluxed to the gas phase polymerization vessel. It takes a long time to respond! /
  • Patent Document 1 the method for producing polyolefin described in Patent Document 1 has room for improvement from the viewpoint of controlling the temperature more stably.
  • the present invention solves the above-mentioned problems by producing a polyolefin using a gas-phase polymerization reactor, and by changing the inflow of cooling water for heat exchange, the pressure in the gas-phase polymerization reactor is changed.
  • An object of the present invention is to provide a method for producing polyolefin and an apparatus for producing the same, whereby force and temperature are controlled stably and effectively to enable stable production of polyolefin.
  • the present inventors have conducted intensive studies and found that the vaporization rate of the liquid monomer refluxed into the gas phase polymerization vessel was reduced while the flow rate of the refluxed liquid monomer was kept substantially constant.
  • the inventors of the present invention have conceived that the adjustment may be performed and that the vaporization rate of the liquefied monomer depends on the pressure in the gas phase polymerization vessel.
  • a monomer gas is extracted from a gas-phase polymerization reactor, and a part or all of the monomer gas is cooled by heat exchange and cooled.
  • Change in the amount of monomer gas to be extracted By controlling the pressure in the gas phase polymerization vessel, the vaporization rate of the liquid monomer in the gas phase polymerization vessel is changed by the controlled pressure in the gas phase polymerization vessel.
  • the temperature change having a slower response speed than the pressure change can be effectively controlled, and the vaporization rate of the liquid monomer in the gas phase polymerization vessel changes.
  • the temperature in the gas phase polymerization reactor can be controlled very stably.
  • a monomer gas is extracted from a gas phase polymerization reactor, and a part or all of the monomer gas is cooled by heat exchange, and the cooling gas and Z or liquid
  • a method for producing polyolefin wherein the pressure in the gas-phase polymerization vessel is higher than a target pressure range, wherein the refrigerant is introduced into the heat exchanger.
  • the heat exchange capacity of the refrigerant flowing into the heat exchanger is reduced to reduce the gas exchange capacity. This is a method for controlling the temperature in the polymerization vessel.
  • the temperature in the gas phase polymerization reactor can be easily controlled by comparing the pressure in the gas phase polymerization reactor with the target pressure range.
  • the method for producing polyolefin of the present invention is a method for controlling the cooling capacity of the heat exchanger based on the inflow amount and Z of the refrigerant or the temperature of the refrigerant.
  • the cooling capacity of heat exchange can be easily and accurately controlled.
  • the control power S becomes even easier.
  • the method for producing polyolefin of the present invention is a method in which the inflow amount of the refrigerant is set according to a differential pressure between a pressure value in the gas phase polymerization reactor and a target pressure value.
  • the cooling capacity of the heat exchange can be adjusted to the optimum capacity in a short time, so that the pressure and the temperature can be stabilized in a short time.
  • the method for producing polyolefin of the present invention is a method for setting the inflow amount of the refrigerant based on the ambient temperature and z of the gas phase polymerization reactor or the temperature of the refrigerant. By doing so, the cooling capacity of the heat exchange can be adjusted to a more optimal capacity, so that the pressure and temperature can be stabilized more accurately.
  • the flow rate (kgZh) of at least a part of the monomer refluxed from the heat exchanger to the gas-phase polymerization vessel may be adjusted to a target value of 10%.
  • a polyolefin production apparatus of the present invention extracts a monomer gas from a gas phase polymerization reactor, cools part or all of the monomer gas by heat exchange, and cools the monomer gas.
  • a polyolefin production apparatus for refluxing a gas and Z or a liquefied monomer to a gas-phase polymerization reactor comprising: a pressure gauge for measuring a pressure in the gas-phase polymerization reactor; and a refrigerant for flowing to the heat exchanger.
  • Flow rate adjusting means for adjusting the inflow amount, and a flow rate adjustment signal for determining the inflow amount of the refrigerant in accordance with the differential pressure between the pressure value detected by the pressure gauge and the target pressure value, and realizing the inflow amount.
  • a control means for outputting the flow rate to the flow rate adjusting means.
  • the present invention is also effective as a polyolefin manufacturing apparatus, and it is possible to control the pressure and temperature of the gas-phase polymerization reactor in a stable state by controlling the flow rate of the refrigerant to the heat exchanger. it can.
  • the pressure and temperature in the gas phase polymerization vessel can be controlled well, and the generation of polymer lumps that easily occur in the gas phase polymerization vessel is prevented. be able to.
  • FIG. 1 is a schematic block diagram illustrating a method for producing polyolefin according to the present invention.
  • FIG. 2 is a schematic flowchart for explaining a method for producing polyolefin according to the present invention.
  • FIG. 3 is a schematic block diagram illustrating a polyolefin manufacturing apparatus according to the present invention. are doing.
  • FIG. 1 is a schematic block diagram for explaining a method for producing polyolefin according to the present invention.
  • a polyolefin production apparatus 1 is a basic apparatus for producing polyolefin by a gas phase polymerization reaction, and is a gas phase polymerization vessel 2, a heat exchanger 3, a flow control valve 4, a flow meter 5, It consists of a pressure gauge 6 and control means 8.
  • the gas phase polymerization vessel 2 is a pressure vessel that can withstand the temperature and pressure in the gas phase polymerization reaction, and has a pressure gauge 6 provided at an upper portion thereof.
  • the gas-phase polymerization device 2 is a continuous stirring type gas-phase polymerization device, in which a monomer gas according to a production amount is supplied from a monomer supply line 20a, and a catalyst is supplied from a catalyst supply line 20b.
  • the monomer gas is extracted from the upper force of the gas-phase polymerization reactor 2 and cooled in the heat exchange 3, and then returned to the lower part of the gas-phase polymerization reactor 2 in the state of the cooling gas and the Z or liquid monomer. It is.
  • a closed system that is, a system that does not discharge the refluxed monomer to the outside of the system.
  • the present invention is not limited to this.
  • a part of the monomer gas is discharged to the outside of the system.
  • the pressure gauge 6 detects the internal pressure of the gas-phase polymerization reactor 2 and outputs a pressure signal to the control means 8. Then, when the internal pressure is higher than a predetermined pressure range (a pressure range suitable for a polymerization reaction), the control means 8 outputs a control signal to the flow control valve 4.
  • the flow control valve 4 that has received the control signal increases the flow rate of the refrigerant supplied to the heat exchanger 3 and increases the cooling capacity of the heat exchanger 3.
  • control means 8 outputs a control signal to the flow control valve 4 when the internal pressure of the gas phase polymerization vessel 2 is lower than a predetermined pressure range.
  • the flow control valve 4 to which the control signal is input reduces the flow rate of the refrigerant supplied to the heat exchanger 3 and lowers the cooling capacity of the heat exchanger 3.
  • the heat exchange 3 is a type of heat exchange in which a refrigerant flows into the heat exchange main body, and the heat exchange main body cooled by the refrigerant cools the monomer gas and liquefies.
  • a tubular heat exchanger 3 is used, but the present invention is not limited to this type.
  • a plate-type heat exchanger may be used.
  • the power of using normal-temperature water (cooling water as appropriate; generally about 23-30 ° C in summer and about 5-20 ° C in winter) as a refrigerant. This is because they can satisfy the heat exchange capacity, and are excellent in terms of dust, safety and cost.
  • a method of controlling the cooling capacity of the heat exchanger 3 is a method of adjusting the cooling capacity according to the inflow amount of the cooling water. It can be controlled easily and accurately.
  • the refrigerant is not limited to normal-temperature water.
  • forced cooling water that has been cooled to more than 0 ° C and lower than normal temperature by a chiller may be used.
  • the cooling capacity of the heat exchanger 3 may be changed. Further, the cooling capacity of the heat exchanger 3 may be changed depending on the amount of cooling water and the temperature.
  • the method for producing polyolefin of the present embodiment includes a catalyst and an optional Supplying a molecular weight modifier (hydrogen gas or the like) or the like, homopolymerization or copolymerization of olefins such as ethylene, propylene, butene 1, pentene-1, hexene 1, otaten-1, 4-methylpentene 1, or This is a method for producing polyolefin by copolymerizing olefin and other various monomers.
  • a molecular weight modifier such as ethylene, propylene, butene 1, pentene-1, hexene 1, otaten-1, 4-methylpentene 1, or This is a method for producing polyolefin by copolymerizing olefin and other various monomers.
  • any general catalyst type solid catalyst can be used as long as it is a catalyst used for the polymerization of olefins.
  • a general Ziegler-based solid catalyst is prepared by adjusting a titanium compound, an organoaluminum, and an electron donor.
  • a titanium conjugate for example, titanium tetrachloride, titanium tetrabromide, titanium tetraiodide, or the like is used.
  • the organic aluminum include alkyl aluminum such as trimethyl aluminum and triethyl aluminum.
  • examples of the electron donor include organosilane conjugates such as tetraethoxysilane, diphenyldimethoxysilane, and dicyclopentyldimethoxysilane in order to effectively improve stereoregularity and the like.
  • the catalyst is not limited to the Ziegler-based solid catalyst, but may be, for example, a meta-open catalyst capable of producing a plastic having excellent transparency and impact resistance.
  • FIG. 2 is a schematic flowchart illustrating the method for producing polyolefin according to the present invention.
  • the raw material monomer is supplied to the gas-phase polymerization reactor 2 through the monomer supply line 20a in the form of liquid or Z or gas, and the catalyst is supplied from the catalyst supply line 20b ( Step Sl).
  • the polymerization reaction usually proceeds at a temperature of about 40 to 90 ° C and a pressure of about 14 MPa, and a powder, which is a polymer, is formed in the middle and lower parts of the gas phase polymerization vessel 2. I do. Since the above polymerization reaction is an exothermic reaction, the temperature in the gas phase polymerization vessel 2 rises, and the pressure rises due to the temperature rise.
  • Step S 2 the pressure in the gas phase polymerization reactor 2 is measured by the pressure gauge 6 (Step S 2), and the control means 8 determines whether the measured pressure value is higher or lower than a predetermined pressure range. Alternatively, it is determined whether the pressure is within a predetermined pressure range (step S3).
  • the flow control valve 4 When the pressure value is higher than the predetermined pressure range, the flow control valve 4 is further opened to The flow rate of the refrigerant supplied to the exchanger 3 is increased, and the cooling capacity of the heat exchanger 3 is increased (step S4).
  • the cooling capacity of the heat exchange ⁇ 3 when the cooling capacity of the heat exchange ⁇ 3 is increased, the amount of the monomer gas liquefied increases, that is, the liquefaction speed increases, and accordingly, the heat exchanger 3 and the gas-phase polymerization reactor are correspondingly increased. 2, the pressure difference becomes large, and more monomer gas in the gas phase polymerization vessel 2 can be extracted. As a result, the pressure force in the gas phase polymerization vessel 2 is sensitively reduced.
  • the vaporization rate of the refluxed liquefied monomer is sensitively increased due to the decrease in the pressure in the gas phase polymerization vessel 2, and the cooling rate in the gas phase polymerization vessel 2 is increased. Therefore, in the inside of the gas phase polymerization vessel 2, when the pressure becomes higher than a predetermined pressure range, the pressure can be reduced first, and then the temperature can be lowered.
  • Step S5 the flow rate of the refrigerant supplied to the heat exchanger 3 is reduced by narrowing the flow control valve 4 to lower the cooling capacity of the heat exchanger 3 ( Step S5)
  • Step S5 the cooling capacity of the heat exchanger is reduced, a phenomenon opposite to that when the cooling capacity of the heat exchanger 3 is increased occurs. That is, when the cooling capacity of the heat exchanger 3 is reduced, the amount of the monomer gas liquefied decreases, and the speed of the liquefaction decreases, so that the pressure difference between the heat exchange 3 and the gas-phase polymerization unit 2 is reduced accordingly. As a result, the amount of the monomer gas extracted from the gas phase polymerization vessel 2 is reduced.
  • the pressure in the gas phase polymerization vessel 2 rises sensitively. Then, the vaporization rate of the refluxed liquefied monomer is reduced sensitively to the extent that the pressure in the gas-phase polymerizer 2 is increased, and the cooling rate in the gas-phase polymerizer 2 is reduced. Therefore, in the inside of the gas phase polymerization vessel 2, when the pressure becomes lower than the predetermined pressure range, the pressure can be increased first, and then the temperature can be increased.
  • step S6 when the pressure value is within the predetermined pressure range, the opening of the flow control valve 4 is maintained, and the current cooling capacity of the heat exchanger 3 is maintained.
  • steps S3, S4, S5, S6 [koo!] By adjusting the cooling capacity of the heat exchanger ⁇ 3 in response to the pressure in the gaseous polymerizer 2, the gas phase
  • the vaporization rate of the liquid monomer in the polymerization vessel 2 changes, and the change in the vaporization rate makes use of the characteristic that the cooling rate in the gas phase polymerization vessel 2 is adjusted. It also controls the temperature.
  • the pressure in the gas phase polymerization vessel 2 is desirably a constant pressure p. However, if the pressure can be controlled at about 0.1 MPa, it is possible to sufficiently prevent inconvenience such as generation of grade-off products. it can.
  • the temperature in the gas phase polymerization vessel 2 is desirably a constant temperature t. However, if the temperature can be controlled at about 4 ° C., inconvenience such as generation of a grade-off product can be sufficiently prevented.
  • a constant temperature t is set between about 60-100 ° C, and a constant pressure p is set between about 11 and 3.5 MPa.
  • step S7 it is determined whether or not the power to terminate the polymerization reaction is present. Again, returning to step S2, the pressure in the gas phase polymerization vessel 2 is measured, and the cooling capacity of the heat exchanger 3 is adjusted. When the polymerization reaction is terminated, the adjustment of the cooling capacity of the heat exchange 3 is terminated.
  • the cooling capacity of the heat exchanger 3 is changed according to the pressure change in the gas-phase polymerization vessel 2, Pressure and temperature can be controlled.
  • the pressure in the gas phase polymerization vessel 2 is controlled by changing the cooling capacity of the heat exchange 3 and adjusting the amount of the monomer gas withdrawn from the gas phase polymerization vessel 2.
  • the temperature in the gas phase polymerization vessel 2 can be controlled. By controlling the temperature in this way, it is possible to control the temperature at which the response speed is slow and stable control is easy, to an extremely stable state.
  • the method for producing polyolefin of the present invention includes various application examples that are not limited to the method of the above embodiment.
  • the flow rate of the cooling water was increased or decreased based on the predetermined pressure range.However, the flow rate of the cooling water was set according to the differential pressure between the pressure value in the gas-phase polymerization vessel 2 and the target pressure value. It is a good way to do it.
  • the increase / decrease flow rate of the cooling water can be reduced in a short time. Since it can be increased or decreased, the cooling capacity of the heat exchanger 3 can be adjusted to the optimum capacity in a short time, and the pressure and temperature can be stabilized in a short time.
  • the accuracy of the simulation can be improved by periodically comparing the simulation with the actual situation.
  • the cooling capacity of the heat exchange 3 can be reduced. Since it can be adjusted to more optimal capacity, pressure and temperature can be stabilized more accurately.
  • the flow rate of the cooling water flowing into the heat exchanger 3 depends on the amount of production and the capacity of the heat exchanger 3, so it cannot be said unconditionally. For a device that produces in volume, it is about 200-1500 m 3 Zhr.
  • a method may be used in which the flow rate (kgZh) of the monomer refluxed from the heat exchange 3 to the gas-phase polymerization vessel 2 and at least partially immersed is set to the target value ⁇ 10%.
  • the flow rate of the liquified monomer is kept constant by refluxing the liquored monomer that has been liquified by the heat exchange 3 to the gas phase polymerization reactor 2 using a metering pump. can do.
  • a polypropylene was manufactured using the manufacturing method and the manufacturing apparatus shown in FIGS.
  • the gas-phase polymerization reactor 2 had a capacity of about 200 liters, and was polymerized for 12 hours at a target polymerization temperature of 80 ° C, a target polymerization pressure of 3 MPa, and a target production volume of 50 kgZhr.
  • Raw material propylene was supplied from the monomer supply line 20a. From the catalyst supply line 20b, a prepolymerized product of the Cidara-based catalyst (0.44 mmol / g-cat in terms of T source, prepolymerized amount 0.43 g—PPZg—cat) was supplied in 4.OgZ hours (based on the raw material propylene). 0.0044 weight 0/0), causes polymerized at the target temperature 'pressure from the top of the polymerization vessel 2, unreacted monomer gas extraction, cooling and Ekyi ⁇ Shi in the heat exchanger 3, the lower portion of the polymerization vessel 2 Refluxed.
  • Example 1 polyolefin was produced in a state where the flow rate of the cooling water of the heat exchanger 3 was kept constant (5 m 3 Zhr) without being adjusted.
  • the polymerization temperature was 80 ⁇ 5 ° C. and the polymerization pressure was 3 ⁇ 0.2 MPa, and fluctuated at almost the same fluctuation cycle as in Example 1.
  • Example 1 Comparative Example 1, according to the method for producing polyolefin according to the present invention, the polymerization temperature and the polymerization pressure could be accurately controlled to predetermined constant values.
  • FIG. 3 is a schematic block diagram for explaining a polyolefin production apparatus according to the present invention.
  • a polyolefin manufacturing apparatus la is an apparatus for manufacturing a polyolefin by a gas phase polymerization reaction, and is a gas phase polymerization apparatus 2, a heat exchanger 3, a flow control valve 4, a flow meter 5, and a pressure gauge 6. , Consisting of a thermometer 7 and control means 8.
  • the gas phase polymerization vessel 2 is a pressure vessel that can withstand the temperature and pressure in the gas phase polymerization reaction, A pressure gauge 6, a thermometer 7 and a pipe 21 are provided at an upper part, and a pipe 22 is provided at a lower part. Further, the gas-phase polymerization reactor 2 is supplied with a monomer gas corresponding to the production amount from a monomer supply line 20a, and is supplied with a catalyst from a catalyst supply line 20b.
  • the pressure gauge 6 detects the internal pressure of the gas-phase polymerization reactor 2, and the thermometer 7 detects the temperature of a monomer gas (not shown) in the gas-phase polymerization reactor 2.
  • the thermometer 7 is provided at the upper part of the gas phase polymerization vessel 2, the present invention is not limited to this configuration.
  • a pipe 21 supplies the monomer gas in the gas phase polymerization vessel 2 to the heat exchanger 3, and a pipe 22 supplies a monomer (liquid monomer) cooled and liquefied by the heat exchange 3. To supply.
  • the control means 8 receives a pressure signal from the pressure gauge 6 and flows into the heat exchanger main body 31 of the heat exchanger 3 according to the pressure difference between the pressure value of the pressure gauge 6 and the target pressure value.
  • the flow rate of the cooling water is determined, and a flow control signal for realizing the flow rate is output to the flow control valve 4 as flow control means.
  • the flow rate of the cooling water is set based on a simulation in which actual operating conditions are input, and the accuracy of the simulation can be improved by periodically correcting the actual control data with actual control data.
  • the control means 8 receives a temperature signal from the thermometer 7 and records the temperature signal together with the flow rate of the cooling water and the pressure value in the gas-phase polymerization reactor 2.This data is used, for example, to periodically correct the above simulation. It becomes valuable data at the time.
  • the present invention is also effective as a polyolefin production apparatus la, and stabilizes the pressure and temperature in the gas-phase polymerization vessel 2 by controlling the flow rate of the cooling water to the heat exchanger 2. It can be controlled to the state where it was done.
  • the gas-phase polymerization apparatus la can effectively control a temperature change having a slower response speed than a pressure change, and also changes the vaporization rate of the liquid monomer in the gas-phase polymerization vessel 2, and this vaporization rate
  • the temperature in the gas phase polymerization vessel 2 can be extremely stably controlled.
  • the method for producing polyolefin and the apparatus for producing the same according to the present invention are preferably described with reference to the embodiments. The method for producing polyolefin and the apparatus for producing the same according to the present invention are described in the above embodiment. It goes without saying that various modifications can be made without departing from the scope of the present invention.
  • the flow rate control of the cooling water is not limited to the method using the flow rate control valve 4.
  • the flow rate control of the pump for supplying the cooling water using an inverter can also be realized.
  • a flow meter and a pump are provided in the pipe 22, and the flow rate (kgZh) of the monomer which is refluxed from the heat exchanger 3 to the gas phase ) Can be controlled to the target value of ⁇ 10%, so that the disadvantage that the stability of the temperature control in the gas-phase polymerization vessel 2 is degraded can be avoided.
  • the method and apparatus for producing polyolefin of the present invention are used as a production method and apparatus used for a polymerization reaction in producing polyolefin, and the raw material gas is cooled, liquefied and refluxed in a container.
  • the present invention can also be applied as a pressure and temperature control method for removing the reaction heat in the vessel and controlling the pressure and temperature in the vessel.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Polymerisation Methods In General (AREA)

Abstract

Cette invention concerne un procédé de fabrication de polyoléfines consistant à refroidir et/ou à liquéfier un gaz monomère et à faire recirculer ledit gaz vers un réacteur de polymérisation en phase vapeur (2). La capacité de refroidissement de l'échangeur de chaleur (3) est régulée en fonction de la pression régnant dans le réacteur de polymérisation en phase vapeur (2), ce qui permet de réguler la pression dans ce dernier. On fait varier la vitesse de vaporisation du monomère liquéfié dans le réacteur de polymérisation en phase vapeur (2) en fonction de la pression régulée. Une telle caractéristique, à savoir que la vitesse de refroidissement du monomère dans le réacteur de polymérisation en phase vapeur (2) est régulée en fonction de la variation de la vitesse de vaporisation permet également de réguler la température dans ledit réacteur de polymérisation (2).
PCT/JP2004/019166 2003-12-24 2004-12-22 Procede et dispositif de fabrication de polyolefines Ceased WO2005061554A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2003-427627 2003-12-24
JP2003427627 2003-12-24

Publications (1)

Publication Number Publication Date
WO2005061554A1 true WO2005061554A1 (fr) 2005-07-07

Family

ID=34708903

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2004/019166 Ceased WO2005061554A1 (fr) 2003-12-24 2004-12-22 Procede et dispositif de fabrication de polyolefines

Country Status (1)

Country Link
WO (1) WO2005061554A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2674213A1 (fr) * 2012-06-14 2013-12-18 Basell Polyolefine GmbH Procédé de refroidissement d'un réacteur en phase gazeuse pour la polymérisation d'oléfines
WO2013186299A1 (fr) * 2012-06-14 2013-12-19 Basell Polyolefine Gmbh Procédé de refroidissement d'un réacteur en phase gazeuse pour la polymérisation d'oléfines
US8906864B2 (en) 2005-09-30 2014-12-09 AbbVie Deutschland GmbH & Co. KG Binding domains of proteins of the repulsive guidance molecule (RGM) protein family and functional fragments thereof, and their use
US8962803B2 (en) 2008-02-29 2015-02-24 AbbVie Deutschland GmbH & Co. KG Antibodies against the RGM A protein and uses thereof
CN104684942A (zh) * 2012-08-06 2015-06-03 英尼奥斯欧洲股份公司 聚合方法
US9102722B2 (en) 2012-01-27 2015-08-11 AbbVie Deutschland GmbH & Co. KG Composition and method for the diagnosis and treatment of diseases associated with neurite degeneration
US9175075B2 (en) 2009-12-08 2015-11-03 AbbVie Deutschland GmbH & Co. KG Methods of treating retinal nerve fiber layer degeneration with monoclonal antibodies against a retinal guidance molecule (RGM) protein

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH11209415A (ja) * 1998-01-30 1999-08-03 Idemitsu Petrochem Co Ltd ポリオレフィンの製造方法
JP2002501569A (ja) * 1997-05-30 2002-01-15 ユニオン カーバイド ケミカルズ アンド プラスティックス テクノロジー コーポレイション 流動床温度制御の改良方法
JP2002519446A (ja) * 1998-06-29 2002-07-02 モービル・オイル・コーポレイション 連続重合プロセスの温度制御用の装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002501569A (ja) * 1997-05-30 2002-01-15 ユニオン カーバイド ケミカルズ アンド プラスティックス テクノロジー コーポレイション 流動床温度制御の改良方法
JPH11209415A (ja) * 1998-01-30 1999-08-03 Idemitsu Petrochem Co Ltd ポリオレフィンの製造方法
JP2002519446A (ja) * 1998-06-29 2002-07-02 モービル・オイル・コーポレイション 連続重合プロセスの温度制御用の装置

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8906864B2 (en) 2005-09-30 2014-12-09 AbbVie Deutschland GmbH & Co. KG Binding domains of proteins of the repulsive guidance molecule (RGM) protein family and functional fragments thereof, and their use
US8962803B2 (en) 2008-02-29 2015-02-24 AbbVie Deutschland GmbH & Co. KG Antibodies against the RGM A protein and uses thereof
US9605069B2 (en) 2008-02-29 2017-03-28 AbbVie Deutschland GmbH & Co. KG Antibodies against the RGM a protein and uses thereof
US9175075B2 (en) 2009-12-08 2015-11-03 AbbVie Deutschland GmbH & Co. KG Methods of treating retinal nerve fiber layer degeneration with monoclonal antibodies against a retinal guidance molecule (RGM) protein
US9102722B2 (en) 2012-01-27 2015-08-11 AbbVie Deutschland GmbH & Co. KG Composition and method for the diagnosis and treatment of diseases associated with neurite degeneration
US9365643B2 (en) 2012-01-27 2016-06-14 AbbVie Deutschland GmbH & Co. KG Antibodies that bind to repulsive guidance molecule A (RGMA)
US10106602B2 (en) 2012-01-27 2018-10-23 AbbVie Deutschland GmbH & Co. KG Isolated monoclonal anti-repulsive guidance molecule A antibodies and uses thereof
EP2674213A1 (fr) * 2012-06-14 2013-12-18 Basell Polyolefine GmbH Procédé de refroidissement d'un réacteur en phase gazeuse pour la polymérisation d'oléfines
WO2013186299A1 (fr) * 2012-06-14 2013-12-19 Basell Polyolefine Gmbh Procédé de refroidissement d'un réacteur en phase gazeuse pour la polymérisation d'oléfines
US9694336B2 (en) 2012-06-14 2017-07-04 Basell Polyolefine Gmbh Method for cooling a gas-phase reactor for the polymerization of olefins
CN104684942A (zh) * 2012-08-06 2015-06-03 英尼奥斯欧洲股份公司 聚合方法
CN104684942B (zh) * 2012-08-06 2017-03-08 英尼奥斯欧洲股份公司 聚合方法

Similar Documents

Publication Publication Date Title
KR101093470B1 (ko) 중합 루프 반응기에서 에틸렌 및 하나 이상의 선택적인 공단량체(들)의 중합을 향상시키는 공정
WO2005061554A1 (fr) Procede et dispositif de fabrication de polyolefines
WO2018087209A1 (fr) Procédé de polymérisation d'oléfines dans un réacteur à phase gazeuse présentant trois zones de polymérisation ou plus
US8101692B2 (en) Slurry phase polymerisation process
CN104628904A (zh) 一种利用多温度反应区制备烯烃聚合物的方法
NO155580B (no) Fremgangsmaate ved polymerisering av ethylen og to-trinns reaktorsystem for anvendelse ved denne.
US8349947B2 (en) Slurry phase polymerisation process
JP2007500279A (ja) 気相重合およびその制御方法
EP2861337B1 (fr) Procédé de refroidissement d'un réacteur en phase gazeuse pour la polymérisation d'oléfines
CN114008089B (zh) 回收率提高的聚丙烯制备方法
US9475896B2 (en) Loop reactor providing an advanced production split control
JPS62124107A (ja) 分子量の制御方法
JPH062777B2 (ja) プロピレンの連続気相重合方法
EP4480576B1 (fr) Procédé de régulation du taux de production d'un homo- ou copolymère de propylène dans un réacteur en phase gazeuse
JP2010537021A (ja) 複数のループ反応器を用いるオレフィン重合方法
Vahidi et al. Control of a fluidized bed polyethylene reactor
KR102896455B1 (ko) 중합체 제조장치
JPH11209415A (ja) ポリオレフィンの製造方法
EP2880066B1 (fr) Procédé de polymérisation
CN118475622A (zh) 聚合方法
WO2006052590A2 (fr) Processus de production de polymeres au moyen d'un reacteur a boucle
JP5029157B2 (ja) プロピレン（共）重合体の満液重合法
JPS62153302A (ja) 重合温度の制御方法
JPS6198701A (ja) 重合温度の制御方法
BR112021025518B1 (pt) Processo para a produção de um copolímero de propileno e unidade de polimerização para produzir um copolímero de propileno

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
NENP Non-entry into the national phase

Ref country code: DE

WWW Wipo information: withdrawn in national office

Country of ref document: DE

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP

WWW Wipo information: withdrawn in national office

Country of ref document: JP