CN109422829A - Polypropylene continuous producing apparatus and intermittent bulk polypropylene production equipment remodeling method - Google Patents
Polypropylene continuous producing apparatus and intermittent bulk polypropylene production equipment remodeling method Download PDFInfo
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- CN109422829A CN109422829A CN201710730817.8A CN201710730817A CN109422829A CN 109422829 A CN109422829 A CN 109422829A CN 201710730817 A CN201710730817 A CN 201710730817A CN 109422829 A CN109422829 A CN 109422829A
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- 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
- C08F10/04—Monomers containing three or four carbon atoms
- C08F10/06—Propene
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Abstract
The invention discloses a kind of polypropylene continuous producing apparatus and its operating methods and intermittent bulk polypropylene production equipment remodeling method.The polypropylene continuous producing apparatus includes: continuous reaction apparatus, and continuous reaction apparatus includes the batchwise polymerization kettle of intermittent bulk polypropylene production equipment；By batch can, it is connected by first pipe with the discharge port of continuous reaction apparatus by the feed inlet of batch can, is the batchwise polymerization kettle by batch can, first pipe is equipped with first switch valve；With multiple flash vaporization kettles, it is connected by multiple second pipes with the feed inlet of multiple flash vaporization kettles by the discharge port of batch can, each flash vaporization kettle is the interval flash vaporization kettle of intermittent bulk polypropylene production equipment, and each second pipe is equipped with second switch valve.Polypropylene continuous producing apparatus according to an embodiment of the present invention has many advantages, such as that transformation difficulty is low, improvement cost is low, stable product quality is high, production capacity is big, work load is small, production operation conditional stability is controllable, product grade is abundant, added value is high.
Description
Technical field
The present invention relates to chemical fields, and in particular, to polypropylene continuous producing apparatus and its operating method, between further relating to
It has a rest ontology polypropylene production equipment remodeling method.
Background technique
Intermittent bulk propylene polymerization process is the polypropylene production work expedited the emergence of out by the special national conditions in China referred to as " small scale bulk "
Skill.Its method is after the propylene after refining and supplies are proportionally added into polymeric kettle, to carry out heating polymerization with hot water, react
Reach certain conversion ratio, stops polymerization.Unreacted propylene is sent into high pressure propylene condenser and condenses and send to the confession of Propylene recovery tank
Next kettle reaction uses, and solid polypropylene powder is sent into flash vaporization kettle.
Wherein, it is anti-that the corresponding flash vaporization kettle of each polymeric kettle, a polymeric kettle and a flash vaporization kettle form a set of interval
Answer device.In flash vaporization kettle, by repeatedly vacuumizing, inflated with nitrogen, separate propylene and polypropylene, the powder after separation is sent into packet
Process is filled, gas phase is then sent into low pressure Propylene Recovery System or emptying.Discharging terminates just to complete a production operation, then carries out down
One kettle feeds intake, and so on.
Existing intermittent bulk propylene polymerization process has many advantages, such as that equipment investment is small, process is simple, production is flexible, at present
Still it is widely present at home.But the same kettle of intermittent bulk propylene polymerization process feed intake every time and kettle and kettle between react item
Part has different, and stable product quality is poor, large labor intensity.
Summary of the invention
Inventive concept and invention difficult point of the invention are not lain in continuous to obtain polypropylene by the way that completely new device is arranged simultaneously
Production equipment.Inventive concept and invention difficult point of the invention be only to existing intermittent bulk polypropylene production equipment carry out compared with
Few transformation, the i.e. structure by existing intermittent bulk polypropylene production equipment are limited, it will be able to by existing interval sheet
Body polypropylene production equipment is transformed into polypropylene continuous producing apparatus.
It is of the existing technology the purpose of the invention is to overcome the problems, such as, it provides poly- by the way that existing intermittent bulk is transformed
The polypropylene continuous producing apparatus that production of propylene equipment obtains, the polypropylene continuous producing apparatus is low with transformation difficulty, is transformed
Advantage at low cost.
To achieve the goals above, first aspect present invention provides a kind of polypropylene continuous producing apparatus, the polypropylene
Continuous producing apparatus includes: continuous reaction apparatus, and the continuous reaction apparatus includes between intermittent bulk polypropylene production equipment
It has a rest polymeric kettle；By batch can, the feed inlet by batch can is connected by first pipe with the discharge port of the continuous reaction apparatus,
It is described by batch can be the intermittent bulk polypropylene production equipment batchwise polymerization kettle, wherein the first pipe be equipped with first
Switch valve；With multiple flash vaporization kettles, the discharge port by batch can by multiple second pipes correspondingly with multiple sudden strains of a muscle
The feed inlet for steaming kettle is connected, and each flash vaporization kettle is the interval flash vaporization kettle of the intermittent bulk polypropylene production equipment, wherein
Each second pipe is equipped with second switch valve.
Polypropylene continuous producing apparatus according to an embodiment of the present invention is by by the more of intermittent bulk polypropylene production equipment
A part in a batchwise polymerization kettle is used as a part of continuous reaction apparatus or continuous reaction apparatus, by the intermittent bulk poly- third
Another part in multiple batchwise polymerization kettles of alkene production equipment is used as by batch can, and intermittent bulk polypropylene production is set
Standby multiple interval flash vaporization kettles are used as multiple flash vaporization kettles, so as to adaptation to local conditions largely utilize existing intermittent bulk poly- third
Existing intermittent bulk polypropylene production equipment easily, is easily transformed into and can continuously be given birth to by the device of alkene production equipment
Produce polyacrylic polypropylene continuous producing apparatus.
Since polypropylene continuous producing apparatus can continuously produce the polypropylene powder, not only can greatly mention
The stability of high yield quality, and production capacity can be increased, reduce work load.
Therefore, polypropylene continuous producing apparatus according to an embodiment of the present invention is with transformation difficulty is low, improvement cost is low, produces
The advantage that quality stability is high, production capacity is big, work load is small, production operation conditional stability is controllable.
Preferably, the continuous reaction apparatus includes the prepolymerization reactor being sequentially connected, the gentle gathering of liquid-phase bulk polymerization kettle
Kettle is closed, the liquid-phase bulk polymerization kettle is the batchwise polymerization kettle of the intermittent bulk polypropylene production equipment, wherein the gas phase
The discharge port of polymeric kettle is connected by the first pipe with the feed inlet by batch can.
Preferably, the prepolymerization reactor be it is multiple, the liquid-phase bulk polymerization kettle be it is multiple, the vapor phase polymerizer be one
A horizontal retort, the charging with multiple liquid-phase bulk polymerization kettles correspondingly of the discharge port of the plurality of prepolymerization reactor
Mouth connection, the feed inlet of the vapor phase polymerizer are connected to the discharge port of each liquid-phase bulk polymerization kettle.
Preferably, it is described by batch can be it is multiple, the first pipe be it is multiple, multiple feed inlets by batch can are one by one
Accordingly it is connected by multiple first pipes with the discharge port of the continuous reaction apparatus, it is preferable that described by batch can
Discharge port is connected with the first end of third pipeline, each of the second end of the third pipeline and multiple second pipes
It is connected, wherein the third pipeline is equipped with flow control valve.
Preferably, described by the Charge level measurer for being used for continuously detecting material position is equipped in batch can, the polypropylene is continuous
Production equipment further comprises controller, the controller and each of the Charge level measurer and the flow control valve
It is connected, so that the material-level measure value according to the Charge level measurer controls the aperture of the flow control valve.
Preferably, the Charge level measurer has upper limit material position value and lower limit material position value, wherein the Charge level measurer
When material-level measure value is neighbouring or is higher than the upper limit material position value, the aperture that the controller controls the flow control valve increases,
When the material-level measure value of the Charge level measurer is neighbouring or is lower than the lower limit material position value, the controller controls the flow tune
The aperture for saving valve reduces.
Preferably, it is described by batch can include propylene outlet and feedback outlet, the polypropylene continuous producing apparatus further wrap
Include: blender, the blender are located at described by batch can, and the blender is the intermittent bulk polypropylene production equipment
Blender；And cyclone separator, the feed inlet of the cyclone separator and the propylene outlet by batch can, the whirlwind
The solid outlet of separator is connected to the feedback outlet by batch can, and the cyclone separator is raw for the intermittent bulk polypropylene
Produce the cyclone separator of equipment.
Second aspect of the present invention provides the operating method of the polypropylene continuous producing apparatus, the operating method include with
Lower step: polypropylene powder is continuously produced using the continuous reaction apparatus；Continuously by the polypropylene powder of production
It is transported to described by batch can；Multiple flash vaporization kettles are alternately transported to by the polypropylene powder by batch can
It is interior, to be flashed in the flash vaporization kettle；Preferably, it is described by batch can be it is multiple, by the polypropylene powder of production
It is alternately transported to multiple described by batch can.
Third aspect present invention provides intermittent bulk polypropylene production equipment remodeling method, and the intermittent bulk polypropylene is raw
Scrap build method is produced the following steps are included: by a part in multiple batchwise polymerization kettles of intermittent bulk polypropylene production equipment
As continuous reaction apparatus；By the rest part in multiple batchwise polymerization kettles of the intermittent bulk polypropylene production equipment
As by batch can, wherein the feed inlet by batch can is made to pass through the discharge port phase of first pipe and the continuous reaction apparatus
Even, and in the first pipe first switch valve is set；With by multiple intervals of the intermittent bulk polypropylene production equipment
Flash vaporization kettle is used as multiple flash vaporization kettles, make the discharge port by batch can by multiple second pipes correspondingly with it is multiple described
The feed inlet of flash vaporization kettle is connected, and second switch valve is arranged on each second pipe.
Preferably, described a part of multiple batchwise polymerization kettles of the intermittent bulk polypropylene production equipment is used as liquid
Phase bulk polymerizer increases setting prepolymerization reactor and vapor phase polymerizer, makes the discharge port of the prepolymerization reactor and the liquid phase sheet
The feed inlet of body polymeric kettle is connected to, the discharge port of the liquid-phase bulk polymerization kettle is connected to the feed inlet of the vapor phase polymerizer,
The discharge port of the vapor phase polymerizer is connected to the feed inlet by batch can.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of polypropylene continuous producing apparatus according to an embodiment of the present invention.
Specific embodiment
The embodiment of the present invention is described below in detail, examples of the embodiments are shown in the accompanying drawings.Below with reference to
The embodiment of attached drawing description is exemplary, it is intended to is used to explain the present invention, and is not considered as limiting the invention.
Inventive concept and invention difficult point of the invention are not lain in continuous to obtain polypropylene by the way that completely new device is arranged simultaneously
Production equipment 10.Inventive concept and invention difficult point of the invention is only to carry out existing intermittent bulk polypropylene production equipment
Less transformation, the i.e. structure by existing intermittent bulk polypropylene production equipment are limited, it will be able to by existing interval
Ontology polypropylene production equipment is transformed into polypropylene continuous producing apparatus 10.
Below with reference to the accompanying drawings polypropylene continuous producing apparatus 10 according to an embodiment of the present invention is described.As shown in Figure 1, according to
The polypropylene continuous producing apparatus 10 of the embodiment of the present invention includes continuous reaction apparatus 110, by batch can 120 and multiple flash vaporization kettles
130。
Continuous reaction apparatus 110 includes the batchwise polymerization kettle of intermittent bulk polypropylene production equipment.By the charging of batch can 120
Mouth is connected by first pipe 141 with the discharge port of continuous reaction apparatus 110, is that the intermittent bulk polypropylene is raw by batch can 120
Produce the batchwise polymerization kettle of equipment.
Passed through multiple second pipes 142 feed inlet with multiple flash vaporization kettles 130 correspondingly by the discharge port of batch can 120
It is connected, each flash vaporization kettle 130 is the interval flash vaporization kettle of the intermittent bulk polypropylene production equipment.That is, each second pipe
The first end in road 142 is connected with by the discharge port of batch can 120, the second end of multiple second pipes 142 correspondingly with it is multiple
The feed inlet of flash vaporization kettle 130 is connected.Wherein, each first pipe 141 is equipped with first switch valve (not shown), Mei Ge
Two pipelines 142 are equipped with second switch valve (not shown).
That is, by a part in multiple batchwise polymerization kettles of the existing intermittent bulk polypropylene production equipment
A part of continuous reaction apparatus 110 or continuous reaction apparatus 110 is transform as, by the more of the intermittent bulk polypropylene production equipment
Another part in a batchwise polymerization kettle is transform as by batch can 120.
The course of work of polypropylene continuous producing apparatus 10 according to an embodiment of the present invention is described below with reference to Fig. 1.Poly- third
The continuous reaction apparatus 110 of alkene continuous producing apparatus 10 continuously produces polypropylene powder, and the discharging of continuous reaction apparatus 110
Mouth continuously exports the polypropylene powder.
Since the discharge port of continuous reaction apparatus 110 is connected by first pipe 141 with by the feed inlet of batch can 120, because
This continuous reaction apparatus 110 continuously can convey the polypropylene powder to by batch can 120.When being multiple by batch can 120, even
Continuous reaction unit 110 alternately can be conveyed the polypropylene powder by batch can 120 to multiple.
Specifically, continuous reaction apparatus 110 first continuously can be conveyed the polypropylene powder by batch can 120 to first
Material.After certain polypropylene powder to be conveyed, the polypropylene powder continuously can be conveyed by batch can 120 to second, first
A polypropylene powder by batch can 120 can be alternately transported to and first material feeding by multiple second pipes 142
Tank 120 is connected in multiple flash vaporization kettles 130 of (cooperation).
It, can be continuously to third by batch can 120 after being conveyed certain polypropylene powder by batch can 120 to second
The polypropylene powder is conveyed, second can be transported to by the polypropylene powder in batch can 120 by multiple second pipes 142
It is connected in multiple flash vaporization kettles 130 of (cooperation) with this second by batch can 120.And so on, until continuously to the last one
The polypropylene powder is conveyed by batch can 120.At this point, first at least part by the polypropylene powder in batch can 120 is
It is transported in flash vaporization kettle 130, therefore can be again continuously to first by conveying the polypropylene powder in batch can 120.Week
And renew, polypropylene is continuously produced so as to realize.
Wherein, continuous reaction apparatus 110 continuously to by batch can 120 convey the polypropylene powder be not incessantly to
The polypropylene powder is conveyed by batch can 120.Continuous reaction apparatus 110 continuously to by batch can 120 convey the polypropylene powder be
Refer to: within a time cycle, which opens the first preset time and closes the second preset time, the time cycle
It continuously carries out until no longer conveying the polypropylene powder to by batch can 120.
Preferably, which can be time control valve, i.e., the first switch valve can control journey by the time
Sequence controls.
It is transported in turn and the multiple sudden strains of a muscle of (cooperation) of should being connected by batch can 120 by the polypropylene powder in batch can 120
It steams in kettle 130, mode and continuous reaction apparatus 110 are in turn to multiple mode bases for being conveyed the polypropylene powder by batch can 120
This is identical, therefore no longer describes in detail.
Wherein, when the flash vaporization kettle that is transported to and should be cooperated by batch can 120 by the polypropylene powder in batch can 120
When in 130, which can be conveyed continuously in the flash vaporization kettle 130.The polypropylene powder can be by continuously
It is transported in the flash vaporization kettle 130 and refers to that the polypropylene powder can be transported to incessantly in the flash vaporization kettle 130, i.e., accordingly
The second switch valve is in the open state always until no longer conveying the polypropylene powder to the flash vaporization kettle 130.
Polypropylene continuous producing apparatus 10 according to an embodiment of the present invention is by by intermittent bulk polypropylene production equipment
A part in multiple batchwise polymerization kettles is used as a part of continuous reaction apparatus 110 or continuous reaction apparatus 110, by the interval
Another part in multiple batchwise polymerization kettles of ontology polypropylene production equipment is used as by batch can 120, and by the intermittent bulk
Multiple interval flash vaporization kettles of polypropylene production equipment are used as multiple flash vaporization kettles 130, so as to adaptation to local conditions a large amount of using existing
The device of some intermittent bulk polypropylene production equipments, easily, easily by existing intermittent bulk polypropylene production equipment
Being transformed into can be with the polyacrylic polypropylene continuous producing apparatus 10 of continuous production.
It, not only can be greatly since polypropylene continuous producing apparatus 10 can continuously produce the polypropylene powder
The stability of product quality is improved, and production capacity can be increased, reduces work load.
Therefore, polypropylene continuous producing apparatus 10 according to an embodiment of the present invention have transformation difficulty is low, improvement cost is low,
Stable product quality is high, production capacity is big, work load is small, production operation conditional stability is controllable, product grade is abundant, added value is high
The advantages that.
Continuous reaction apparatus 110 can be known, i.e. continuous reaction apparatus 110 can be that existing any one is continuous
Reaction unit.
In addition, continuous reaction apparatus 110 is also possible to the new continuous reaction apparatus of inventor's offer.As shown in Figure 1,
In some embodiments of the present invention, continuous reaction apparatus 110 may include that the prepolymerization reactor 112 being sequentially connected, liquid-phase bulk are poly-
Close kettle 111 and vapor phase polymerizer 113, liquid-phase bulk polymerization kettle 111 can be the intermittent bulk polypropylene production equipment should between
It has a rest polymeric kettle.Wherein, the discharge port of vapor phase polymerizer 113 can by first pipe 141 with by the feed inlet phase of batch can 120
Even.
In other words, setting prepolymerization reactor 112 can be increased on the basis of existing intermittent bulk polypropylene production equipment
With vapor phase polymerizer 113, so as to form new continuous reaction apparatus 110.
As shown in Figure 1, prepolymerization reactor 112 can be multiple, liquid-phase bulk polymerization kettle 111 can be multiple, gas-phase polymerization
Kettle 113 can be a horizontal retort.Wherein, the discharge port of multiple prepolymerization reactors 112 can correspondingly with multiple liquid phase sheets
The feed inlet of body polymeric kettle 111 is connected to (such as passing through pipeline), the feed inlet of vapor phase polymerizer 113 and each liquid-phase bulk polymerization
The discharge port of kettle 111 is connected to (such as passing through pipeline).The discharge port of vapor phase polymerizer 113 can pass through multiple first pipes 141
It is connected correspondingly with multiple feed inlets by batch can 120.In other words, multiple prepolymerization reactors 112 are in parallel, multiple liquid-phase bulks
Polymeric kettle 111 is in parallel.
Preferably, as shown in Figure 1, prepolymerization reactor 112 can be two, liquid-phase bulk polymerization kettle 111 can be two.
The process of the polypropylene powder is continuously produced using continuous reaction apparatus 110 below with reference to Fig. 1 description.
It is up to the raw material propylene that polymerization requires and is respectively delivered to two with Titanium series catalyst, triethyl aluminum and electron donor
In prepolymerization reactor 112 with stirring, prepolymerization reactor 112 can be vertical retort.Under stirring, material is uniformly mixed simultaneously shape
At catalyst active center, then start prepolymerization.At a temperature of 3MPa-3.5MPa (G) pressure, 40 DEG C -45 DEG C, pre-polymerization
Closing the time is 4-5 minutes.
Wherein, Titanium series catalyst, triethyl aluminum, electron donor three are evenly distributed to two prepolymerization reactors by pipeline
In 112.The heat that prepolymerization is released is removed by the cooling water in collet and inner cool tube.
The mixture of propylene and active catalyst after prepolymerization respectively enters two liquid-phase bulks in parallel
Polymeric kettle 111 continues polymerization reaction.Wherein, the pressure of polymerization reaction be 3MPa (G) -3.4MPa (G), temperature be 65 DEG C -
70 DEG C, for Level control in 35%-45%, residence time of material is -1 hour 0.7 hour.Between the heat that polymerization reaction generates passes through
The original cooling water system of bulk polymerizer of having a rest removes.Fresh hydrogen enters two liquid-phase bulk polymerization kettles by pipeline mean allocation
In 111.
The batchwise polymerization of existing intermittent bulk polypropylene production equipment can be used in two liquid-phase bulk polymerization kettles 111
Kettle does not need to remanufacture.Slurries in two liquid-phase bulk polymerization kettles 111 enter under the control of respective liquid level by pressure difference
Vapor phase polymerizer 113.
The polymerization pressure of vapor phase polymerizer 113 is 2.6MPa (G) -2.8MPa (G).Due to coming from liquid-phase bulk polymerization kettle
The pressure of 111 material is higher, therefore the material from liquid-phase bulk polymerization kettle 111 enters the pressure after vapor phase polymerizer 113
Drop larger, Partial Liquid Phase propylene gasifies rapidly, absorbs the heat that partially polymerized reaction is released.The liquid propylene of gasification starts simultaneously
Gas-phase polymerization is carried out, the residence time is -1.5 hours 1 hour.
Vapor phase polymerizer 113 is the container of Horizontal band stirring.In normal operation, vapor phase polymerizer 113 is by poly- third
Alkene powder is partly full of, and stirring is so that powder bed uniformly mixes, and under the adjusting of hydrogen, realization subregion reacts.Vapor phase polymerizer
113 are equipped with the collet water system for maintaining reaction temperature.Vapor phase polymerizer 113 is set there are two biggish gas phase Disengagement zone, is subtracted
The Dust Capacity of few gaseous phase materials entrainment.113 gas phase of vapor phase polymerizer is provided with circulation cooling system, and circulating air passes through condenser,
Gas-phase condensation pumps boosting through lime set at after liquid phase, powder bed is sprayed onto from the differential responses area of reaction kettle respectively, by gasification
Latent heat controls reaction temperature.Another burst of circulation gas phase is sent into the high pressure Propylene Recovery System of intermittent bulk process units, to remove
The inert in gas-phase propene is removed, accumulation is avoided excessively to influence reactivity.The material clamp band of fully reacting is unreacted
Gas-phase propene enters by batch can 120, to be post-processed.
It is may include propylene outlet and feedback outlet by batch can 120 as shown in Figure 1, in an example of the invention, poly- third
Alkene continuous producing apparatus 10 may further include blender 121 and cyclone separator 150.
Blender 121 can be located at by batch can 120, and blender 121 can be the intermittent bulk polypropylene production equipment
Blender.Preferably, the blade type of blender 121 is changed to helical-ribbon type, and stirring motor is changed to and material processing capacity phase
Matched motor.The feed inlet of cyclone separator 150 can with the propylene outlet by batch can 120, cyclone separator 150
Solid outlet can be connected to by the feedback outlet of batch can 120.
When being multiple by batch can 120, blender 121 is that multiple and cyclone separator 150 is multiple.That is, every
It is a can be equal to the number by batch can 120 equipped with a blender 121, the quantity of cyclone separator 150 by batch can 120
Amount, a cyclone separator 150 with one by batch can 120 cooperation.
By the way that by blender 121 is arranged in batch can 120, so as under the stirring action of blender 121, analysis is released
The propylene gas being adsorbed in polypropylene powder.By be arranged with by batch can 120 cooperate cyclone separator 150, so as to
Remove the dust in the propylene gas.
As shown in Figure 1, can be by batch can 120 it is multiple, first pipe 141 can be it is multiple, it is multiple by batch can 120 into
Material mouth can be connected by multiple first pipes 141 with the discharge port of continuous reaction apparatus 110 correspondingly.That is,
The first end of each first pipe 141 can be connected with the discharge port of continuous reaction apparatus 110, and the of multiple first pipes 141
Two ends can be connected with multiple feed inlets by batch can 120 correspondingly.
Each it can be passed through the feed inlet phase of multiple second pipes 142 and multiple flash vaporization kettles 130 by the discharge port of batch can 120
Even.Wherein, the first end of each second pipe 142 can be connected with by the discharge port of batch can 120, multiple second pipes 142
Second end can be connected with the feed inlet of multiple flash vaporization kettles 130 correspondingly.Thus one (is gathered by the material in batch can 120
Propylene powder) it can be transported in multiple flash vaporization kettles 130.Wherein, different by batch can 120 and different 130 phases of flash vaporization kettle
Even (cooperation).
As shown in Figure 1, the discharge port by batch can 120 can be connected with the first end of third pipeline 143, third pipeline 143
Second end can be connected with each of multiple second pipes 142, flow control valve can be equipped on third pipeline 143
(not shown).
Preferably, as shown in Figure 1, the quantity of flash vaporization kettle 130 can be twice of the quantity by batch can 120, each material feeding
The discharge port of tank 120 can be connected by two second pipes 142 with the feed inlet of two flash vaporization kettles 130.
The process post-processed to the polypropylene powder is described below with reference to Fig. 1.After being carried out to the polypropylene powder
Reason is exactly to carry out gas solid separation to the polypropylene powder.
Vapor phase polymerizer 113 continuously can convey the polypropylene powder while being one (by batch can 120) to by batch can 120
Or alternately to it is multiple by batch can 120 convey the polypropylene powder, so as to vapor phase polymerizer 113 can continuously export this poly- third
Alkene powder.Under the stirring action by the blender 121 of batch can 120, the propylene gas being adsorbed in the polypropylene powder is released in analysis
Body.The propylene gas enters in cyclone separator 150, and tentatively removes dust in cyclone separator 150.It is preliminary to remove powder
The propylene gas of dirt is sent into the Propylene Recovery System of intermittent bulk process units.
It is transported in turn by the polypropylene powder in batch can 120 and is somebody's turn to do the multiple flash vaporization kettles 130 that cooperated by batch can 120
It is interior.
Each flash vaporization kettle 130 experience " vacuumized by 120 blankings of batch can-first time propylene to low pressure recovery system-propylene-
Inflated with nitrogen-nitrogen emptying-nitrogen vacuumizes the discharging of-nitrogen binder to packaging-displacement kettle " process.Wherein, a flash vaporization kettle 130
When material feeding full gate begins to carry out gas solid separation operation, another flash vaporization kettle 130 then just starts material feeding.Multiple flash vaporization kettles 130 are in turn
Ground material feeding, multiple flash vaporization kettles 130 alternately carry out gas solid separation operation.
Preferably, it during being vacuumized after 130 material feeding of flash vaporization kettle, can be passed through into flash vaporization kettle 130 micro
Desalted water or steam, to make remaining triethyl aluminum lose activity, thus guarantee be sent into packaging polypropylene powder more
Safety.The higher gas phase of propylene Gas content for leaving flash vaporization kettle 130 removes vacuum pump, and eventually enters into Propylene Recovery System, containing micro-
The gas phase for measuring propylene is vented after analysis is qualified by vacuum pump.
Operating process and aforesaid operations process of the others by batch can 120 and flash vaporization kettle 130 are essentially identical, therefore no longer retouch
It states.By the way that (alternating) operates in turn in batches, the discharging of multiple flash vaporization kettles 130 can satisfy wanting for reaction system continuous operation
It asks.
In some examples of the invention, by batch can 120 can be equipped with for continuously detect material position material-level measure
Device.Polypropylene continuous producing apparatus 10 may further include controller, which can be with the Charge level measurer and the stream
Each of adjustable valve is connected, to control opening for the flow control valve according to the material-level measure value of the Charge level measurer
Degree.It is possible thereby to the degree of automation of polypropylene continuous producing apparatus 10 be greatlyd improve, so as to further decrease labour
Load.
Preferably, which can be the radio frequency admittance type material positioning meter that can measure continuous material level.
In a specific example of the invention, which has upper limit material position value and lower limit material position value.The material
When the material-level measure value of bit detector is neighbouring or is higher than the upper limit material position value, the aperture which controls the flow control valve increases
Greatly, when the material-level measure value of the Charge level measurer is neighbouring or is lower than the lower limit material position value, which controls the flow control valve
Aperture reduce.It is possible thereby to which polypropylene continuous producing apparatus 10 is made to easily facilitate control.
Specifically, being connected with first by batch can 120 when being conveyed the polypropylene powder by batch can 120 to first
First pipe 141 on first switch valve open.With the input of the polypropylene powder, first by being somebody's turn to do in batch can 120
The material position of polypropylene powder constantly rises.When the Charge level measurer detect the polypropylene powder material position it is higher when, i.e., this is poly-
When the material position of propylene powder is neighbouring or is higher than the upper limit material position value, which, which can control, is connected with first by batch can 120
Third pipeline 143 on the aperture of the flow control valve become larger, so that first by the polypropylene powder in batch can 120
Material position drops in setting range.
As the aperture of the flow control valve on third pipeline 143 becomes larger or first feed break by batch can 120,
First material position by the polypropylene powder in batch can 120 constantly declines.When the Charge level measurer detects the polypropylene powder
When the material position of material is lower, i.e. when the material position of the polypropylene powder is neighbouring or is lower than the lower limit material position value, which be can control
The aperture for the flow control valve on third pipeline 143 being connected with first by batch can 120 becomes smaller.
It in this process, is continuously that the mode of operation of flash vaporization kettle 130 is batch by the mode of operation of batch can 120.
That is, (the flow adjusting that the flow control valve on the third pipeline 143 being connected with by batch can 120 is always on
The aperture of valve can change), multiple second switch valves on the multiple second pipes 142 being connected with by batch can 120 are
It opens in turn.In other words, it is continuously discharged by batch can 120, is connected the interval of flash vaporization kettle 130 of (cooperation) with this by batch can 120
The material feeding of (batch).
Therefore, it in entire production process, can be stably controlled in a certain range by the material position of batch can 120.Its
His operating process and aforesaid operations process by batch can 120 is essentially identical, therefore no longer describes in detail.
When the quantity by batch can 120 is more, when can be opened by the first switch valve in setting first pipe 141
Between be spaced, process control to multiple by material feeding in turn in batch can 120, as long as guaranteeing that continuous reaction apparatus 110 can be continuously defeated
The polypropylene powder out.
The present invention also provides intermittent bulk polypropylene production equipment remodeling methods.Interval sheet according to an embodiment of the present invention
Body polypropylene production equipment remodeling method the following steps are included:
A part in multiple batchwise polymerization kettles of intermittent bulk polypropylene production equipment is used as continuous reaction apparatus
110；
Rest part in multiple batchwise polymerization kettles of intermittent bulk polypropylene production equipment is used as by batch can 120,
In so that the feed inlet by batch can 120 is connected by first pipe 141 with the discharge port of continuous reaction apparatus 110, and managed first
First switch valve is set on road 141；With
Multiple interval flash vaporization kettles of the intermittent bulk polypropylene production equipment are used as multiple flash vaporization kettles 130, are made by batch can
120 discharge port is connected with the feed inlet of multiple flash vaporization kettles 130 correspondingly by multiple second pipes 142, and each
Second switch valve is set on second pipe 142.
Wherein, above-mentioned steps have no sequencing.For example, can be first by multiple of intermittent bulk polypropylene production equipment
The rest part having a rest in polymeric kettle is used as by batch can 120, then by multiple batchwise polymerization kettles of intermittent bulk polypropylene production equipment
In a part be used as continuous reaction apparatus 110.
Intermittent bulk polypropylene production equipment remodeling method according to an embodiment of the present invention is by by intermittent bulk polypropylene
A part in multiple batchwise polymerization kettles of production equipment is used as one of continuous reaction apparatus 110 or continuous reaction apparatus 110
Point, another part in multiple batchwise polymerization kettles of the intermittent bulk polypropylene production equipment is used as by batch can 120, and will
Multiple interval flash vaporization kettles of the intermittent bulk polypropylene production equipment are used as multiple flash vaporization kettles 130, so as to adaptation to local conditions
The device for largely utilizing existing intermittent bulk polypropylene production equipment, easily, easily by existing intermittent bulk poly- third
Alkene production equipment is transformed into can be with the polyacrylic polypropylene continuous producing apparatus 10 of continuous production.
By the way that there is transformation difficulty using intermittent bulk polypropylene production equipment remodeling method according to an embodiment of the present invention
The low, advantages such as improvement cost is low, can be improved stable product quality, increase production capacity, reduce work load, abundant product board
Number, improve added value, keep production operation conditional stability controllable.
In one embodiment of the invention, being somebody's turn to do multiple batchwise polymerization kettles of the intermittent bulk polypropylene production equipment
A part is used as liquid-phase bulk polymerization kettle 111, increases setting prepolymerization reactor 112 and vapor phase polymerizer 113, makes prepolymerization reactor 112
Discharge port be connected to the feed inlet of liquid-phase bulk polymerization kettle 111, the discharge port and vapor phase polymerizer of liquid-phase bulk polymerization kettle 111
113 feed inlet connection, the discharge port of vapor phase polymerizer 113 are connected to by the feed inlet of batch can 120.In other words, successive reaction
Device 110 may include prepolymerization reactor 112, liquid-phase bulk polymerization kettle 111 and vapor phase polymerizer 113.
The present invention also provides the operating methods of polypropylene continuous producing apparatus 10.Polypropylene according to an embodiment of the present invention
The operating method of continuous producing apparatus 10 the following steps are included:
Polypropylene powder is continuously produced using continuous reaction apparatus 110；
The polypropylene powder of production is continuously fed to by batch can 120；With
To be alternately transported in multiple flash vaporization kettles 130 by the polypropylene powder in batch can 120 (i.e. with this by batch can
120 connected multiple flash vaporization kettles 130), to be flashed in flash vaporization kettle 130.
By the operating method using polypropylene continuous producing apparatus 10 according to an embodiment of the present invention, so as to continuous
Ground produces polypropylene powder, have stable product quality is high, production capacity is big, work load is small, production operation conditional stability is controllable,
The advantages that product grade is abundant, added value is high.
Preferably, it can be multiple, the polypropylene powder of production be alternately transported to multiple by batch can by batch can 120
In 120.
In the description of the present invention, it is to be understood that, term " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom" "inner", "outside", " up time
The orientation or positional relationship of the instructions such as needle ", " counterclockwise ", " axial direction ", " radial direction ", " circumferential direction " be orientation based on the figure or
Positional relationship is merely for convenience of description of the present invention and simplification of the description, rather than the device or element of indication or suggestion meaning must
There must be specific orientation, be constructed and operated in a specific orientation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are used for descriptive purposes only and cannot be understood as indicating or suggesting relative importance
Or implicitly indicate the quantity of indicated technical characteristic.Define " first " as a result, the feature of " second " can be expressed or
Implicitly include at least one this feature.In the description of the present invention, the meaning of " plurality " is at least two, such as two, three
It is a etc., unless otherwise specifically defined.
In the present invention unless specifically defined or limited otherwise, term " installation ", " connected ", " connection ", " fixation " etc.
Term shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integral；It can be mechanical connect
It connects, is also possible to be electrically connected or can communicate each other；It can be directly connected, can also indirectly connected through an intermediary, it can be with
It is the interaction relationship of the connection or two elements inside two elements, unless otherwise restricted clearly.For this field
For those of ordinary skill, the specific meanings of the above terms in the present invention can be understood according to specific conditions.
In the present invention unless specifically defined or limited otherwise, fisrt feature in the second feature " on " or " down " can be with
It is that the first and second features directly contact or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature be directly above or diagonally above the second feature, or be merely representative of
First feature horizontal height is higher than second feature.Fisrt feature can be under the second feature " below ", " below " and " below "
One feature is directly under or diagonally below the second feature, or is merely representative of first feature horizontal height less than second feature.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or spy described in conjunction with this embodiment or example
Point is included at least one embodiment or example of the invention.In the present specification, schematic expression of the above terms are not
It must be directed to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be in office
It can be combined in any suitable manner in one or more embodiment or examples.In addition, without conflicting with each other, the skill of this field
Art personnel can tie the feature of different embodiments or examples described in this specification and different embodiments or examples
It closes and combines.
Although the embodiments of the present invention has been shown and described above, it is to be understood that above-described embodiment is example
Property, it is not considered as limiting the invention, those skilled in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, modifies, replacement and variant.
Claims (10)
1. a kind of polypropylene continuous producing apparatus characterized by comprising
Continuous reaction apparatus, the continuous reaction apparatus include the batchwise polymerization kettle of intermittent bulk polypropylene production equipment；
By batch can, the feed inlet by batch can is connected by first pipe with the discharge port of the continuous reaction apparatus, described
It is the batchwise polymerization kettle of the intermittent bulk polypropylene production equipment by batch can, wherein the first pipe is equipped with first switch
Valve；With
Multiple flash vaporization kettles, the discharge port by batch can by multiple second pipes correspondingly with multiple flash vaporization kettles
Feed inlet is connected, and each flash vaporization kettle is the interval flash vaporization kettle of the intermittent bulk polypropylene production equipment, wherein each institute
Second pipe is stated equipped with second switch valve.
2. polypropylene continuous producing apparatus according to claim 1, which is characterized in that the continuous reaction apparatus include according to
Secondary connected prepolymerization reactor, liquid-phase bulk polymerization kettle and vapor phase polymerizer, the liquid-phase bulk polymerization kettle are the intermittent bulk
The batchwise polymerization kettle of polypropylene production equipment, wherein the discharge port of the vapor phase polymerizer by the first pipe and it is described by
The feed inlet of batch can is connected.
3. polypropylene continuous producing apparatus according to claim 2, which is characterized in that the prepolymerization reactor is multiple, institute
State liquid-phase bulk polymerization kettle be it is multiple, the vapor phase polymerizer be a horizontal retort, the discharging of the plurality of prepolymerization reactor
Mouthful be connected to correspondingly with the feed inlet of multiple liquid-phase bulk polymerization kettles, the feed inlet of the vapor phase polymerizer with each
The discharge port of the liquid-phase bulk polymerization kettle is connected to.
4. polypropylene continuous producing apparatus according to claim 1 or 2, which is characterized in that it is described by batch can be multiple, institute
State first pipe be it is multiple, it is multiple described to be passed through multiple first pipes and the company correspondingly by the feed inlet of batch can
The discharge port of continuous reaction unit is connected,
Preferably, the discharge port by batch can is connected with the first end of third pipeline, the second end of the third pipeline and more
Each of a described second pipe is connected, wherein the third pipeline is equipped with flow control valve.
5. polypropylene continuous producing apparatus according to claim 4, which is characterized in that described to be equipped with by batch can for connecting
Detect the Charge level measurer of material position continuously, the polypropylene continuous producing apparatus further comprises controller, the controller with
Each of the Charge level measurer and described flow control valve are connected, so as to according to the material-level measure of the Charge level measurer
Value controls the aperture of the flow control valve.
6. polypropylene continuous producing apparatus according to claim 5, which is characterized in that the Charge level measurer has the upper limit
Material position value and lower limit material position value, wherein when the material-level measure value of the Charge level measurer is adjacent to or higher than the upper limit material position value,
The aperture that the controller controls the flow control valve increases, and the material-level measure value of the Charge level measurer is neighbouring or is lower than institute
When stating lower limit material position value, the aperture that the controller controls the flow control valve reduces.
7. polypropylene continuous producing apparatus according to claim 1, which is characterized in that it is described by batch can include propylene outlet
And feedback outlet, the polypropylene continuous producing apparatus further comprises:
Blender, the blender are located at described by batch can, and the blender is the intermittent bulk polypropylene production equipment
Blender；With
Cyclone separator, the feed inlet of the cyclone separator and the propylene outlet by batch can, the cyclonic separation
The solid outlet of device is connected to the feedback outlet by batch can, and the cyclone separator is that intermittent bulk polypropylene production is set
Standby cyclone separator.
8. the operating method of polypropylene continuous producing apparatus described in any one of -7 according to claim 1, which is characterized in that packet
Include following steps:
Polypropylene powder is continuously produced using the continuous reaction apparatus；
The polypropylene powder of production is continuously fed to described by batch can；With
The polypropylene powder by batch can is alternately transported in multiple flash vaporization kettles, so as in the flash distillation
It is flashed in kettle；
Preferably, it is described by batch can be it is multiple, the polypropylene powder of production is alternately transported to multiple described by batch can
It is interior.
9. a kind of intermittent bulk polypropylene production equipment remodeling method, which comprises the following steps:
A part in multiple batchwise polymerization kettles of intermittent bulk polypropylene production equipment is used as continuous reaction apparatus；
Rest part in multiple batchwise polymerization kettles of the intermittent bulk polypropylene production equipment is used as by batch can,
In so that the feed inlet by batch can is connected by first pipe with the discharge port of the continuous reaction apparatus, and described first
First switch valve is set on pipeline；With
Multiple interval flash vaporization kettles of the intermittent bulk polypropylene production equipment are used as multiple flash vaporization kettles, are made described by batch can
Discharge port is connected with the feed inlet of multiple flash vaporization kettles correspondingly by multiple second pipes, and each described second
Second switch valve is set on pipeline.
10. intermittent bulk polypropylene production equipment remodeling method according to claim 9, which is characterized in that
Described a part of multiple batchwise polymerization kettles of the intermittent bulk polypropylene production equipment is used as liquid-phase bulk polymerization
Kettle,
Increase setting prepolymerization reactor and vapor phase polymerizer, makes the discharge port of the prepolymerization reactor and the liquid-phase bulk polymerization kettle
Feed inlet is connected to, the discharge port of the liquid-phase bulk polymerization kettle is connected to the feed inlet of the vapor phase polymerizer, the gas phase is poly-
The discharge port for closing kettle is connected to the feed inlet by batch can.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710730817.8A CN109422829A (en) | 2017-08-23 | 2017-08-23 | Polypropylene continuous producing apparatus and intermittent bulk polypropylene production equipment remodeling method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710730817.8A CN109422829A (en) | 2017-08-23 | 2017-08-23 | Polypropylene continuous producing apparatus and intermittent bulk polypropylene production equipment remodeling method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112693024A (en) * | 2019-10-23 | 2021-04-23 | 中国石油化工股份有限公司 | Foaming equipment and foaming method for polypropylene material |
| CN113827994A (en) * | 2021-09-26 | 2021-12-24 | 金澳科技（湖北）化工有限公司 | Flash evaporation optimization method for polymerization powder |
-
2017
- 2017-08-23 CN CN201710730817.8A patent/CN109422829A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112693024A (en) * | 2019-10-23 | 2021-04-23 | 中国石油化工股份有限公司 | Foaming equipment and foaming method for polypropylene material |
| CN113827994A (en) * | 2021-09-26 | 2021-12-24 | 金澳科技（湖北）化工有限公司 | Flash evaporation optimization method for polymerization powder |
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