CN106985300B - A kind of polycarbonate preparation system - Google Patents
A kind of polycarbonate preparation system Download PDFInfo
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- CN106985300B CN106985300B CN201710274273.9A CN201710274273A CN106985300B CN 106985300 B CN106985300 B CN 106985300B CN 201710274273 A CN201710274273 A CN 201710274273A CN 106985300 B CN106985300 B CN 106985300B
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- phenol
- auxiliary agent
- polycarbonate
- tank
- pipeline
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- 239000004417 polycarbonate Substances 0.000 title claims abstract description 115
- 229920000515 polycarbonate Polymers 0.000 title claims abstract description 114
- 238000002360 preparation method Methods 0.000 title claims abstract description 23
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 140
- 239000012752 auxiliary agent Substances 0.000 claims abstract description 89
- 230000003068 static effect Effects 0.000 claims abstract description 82
- 230000007246 mechanism Effects 0.000 claims abstract description 68
- 238000006068 polycondensation reaction Methods 0.000 claims abstract description 64
- 238000011084 recovery Methods 0.000 claims abstract description 52
- 238000001914 filtration Methods 0.000 claims abstract description 31
- 238000010438 heat treatment Methods 0.000 claims abstract description 24
- 238000001816 cooling Methods 0.000 claims abstract description 23
- 238000001125 extrusion Methods 0.000 claims abstract description 19
- 238000002844 melting Methods 0.000 claims description 32
- 230000008018 melting Effects 0.000 claims description 32
- 239000000155 melt Substances 0.000 claims description 17
- 239000010808 liquid waste Substances 0.000 claims description 12
- 229910052751 metal Inorganic materials 0.000 claims description 11
- 239000002184 metal Substances 0.000 claims description 11
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 claims description 4
- 244000178289 Verbascum thapsus Species 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 238000007500 overflow downdraw method Methods 0.000 claims description 3
- 238000004056 waste incineration Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 62
- 239000002699 waste material Substances 0.000 abstract description 41
- 238000004140 cleaning Methods 0.000 abstract description 38
- -1 aromatic hydroxy compound Chemical class 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 229960003742 phenol Drugs 0.000 description 118
- 239000000243 solution Substances 0.000 description 23
- 238000002309 gasification Methods 0.000 description 21
- 239000003795 chemical substances by application Substances 0.000 description 19
- 230000000087 stabilizing effect Effects 0.000 description 14
- 238000004519 manufacturing process Methods 0.000 description 13
- 239000002245 particle Substances 0.000 description 10
- 238000005453 pelletization Methods 0.000 description 10
- 239000006096 absorbing agent Substances 0.000 description 9
- 239000003963 antioxidant agent Substances 0.000 description 9
- 230000003078 antioxidant effect Effects 0.000 description 9
- 238000004064 recycling Methods 0.000 description 9
- 230000009471 action Effects 0.000 description 8
- 238000009833 condensation Methods 0.000 description 8
- 230000005494 condensation Effects 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 229960003666 liquefied phenol Drugs 0.000 description 8
- 239000007921 spray Substances 0.000 description 8
- 239000002253 acid Substances 0.000 description 7
- 238000002834 transmittance Methods 0.000 description 7
- 238000010792 warming Methods 0.000 description 7
- 238000007373 indentation Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 230000015556 catabolic process Effects 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000010935 stainless steel Substances 0.000 description 4
- 229910001220 stainless steel Inorganic materials 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 229920006351 engineering plastic Polymers 0.000 description 3
- 150000002148 esters Chemical group 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical compound C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 230000021615 conjugation Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 2
- 238000010348 incorporation Methods 0.000 description 2
- 230000003287 optical effect Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000004262 Ethyl gallate Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- RRTCFFFUTAGOSG-UHFFFAOYSA-N benzene;phenol Chemical compound C1=CC=CC=C1.OC1=CC=CC=C1 RRTCFFFUTAGOSG-UHFFFAOYSA-N 0.000 description 1
- 229940106691 bisphenol a Drugs 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- ROORDVPLFPIABK-UHFFFAOYSA-N diphenyl carbonate Chemical compound C=1C=CC=CC=1OC(=O)OC1=CC=CC=C1 ROORDVPLFPIABK-UHFFFAOYSA-N 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000011888 foil Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 150000002440 hydroxy compounds Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000012994 photoredox catalyst Substances 0.000 description 1
- 238000005498 polishing Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000013102 re-test Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 239000004416 thermosoftening plastic Substances 0.000 description 1
- 238000005809 transesterification reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/02—Mixing; Kneading non-continuous, with mechanical mixing or kneading devices, i.e. batch type
- B29B7/04—Mixing; Kneading non-continuous, with mechanical mixing or kneading devices, i.e. batch type with non-movable mixing or kneading devices
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
- B29B7/7476—Systems, i.e. flow charts or diagrams; Plants
- B29B7/7485—Systems, i.e. flow charts or diagrams; Plants with consecutive mixers, e.g. with premixing some of the components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B08—CLEANING
- B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
- B08B9/00—Cleaning hollow articles by methods or apparatus specially adapted thereto
- B08B9/02—Cleaning pipes or tubes or systems of pipes or tubes
- B08B9/027—Cleaning the internal surfaces; Removal of blockages
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B08—CLEANING
- B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
- B08B9/00—Cleaning hollow articles by methods or apparatus specially adapted thereto
- B08B9/02—Cleaning pipes or tubes or systems of pipes or tubes
- B08B9/027—Cleaning the internal surfaces; Removal of blockages
- B08B9/032—Cleaning the internal surfaces; Removal of blockages by the mechanical action of a moving fluid, e.g. by flushing
- B08B9/0321—Cleaning the internal surfaces; Removal of blockages by the mechanical action of a moving fluid, e.g. by flushing using pressurised, pulsating or purging fluid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B13/00—Conditioning or physical treatment of the material to be shaped
- B29B13/10—Conditioning or physical treatment of the material to be shaped by grinding, e.g. by triturating; by sieving; by filtering
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/02—Mixing; Kneading non-continuous, with mechanical mixing or kneading devices, i.e. batch type
- B29B7/22—Component parts, details or accessories; Auxiliary operations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
- B29B7/7476—Systems, i.e. flow charts or diagrams; Plants
- B29B7/748—Plants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/80—Component parts, details or accessories; Auxiliary operations
- B29B7/82—Heating or cooling
- B29B7/823—Temperature control
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/80—Component parts, details or accessories; Auxiliary operations
- B29B7/88—Adding charges, i.e. additives
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/80—Component parts, details or accessories; Auxiliary operations
- B29B7/88—Adding charges, i.e. additives
- B29B7/94—Liquid charges
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/02—Making granules by dividing preformed material
- B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/12—Making granules characterised by structure or composition
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G64/00—Macromolecular compounds obtained by reactions forming a carbonic ester link in the main chain of the macromolecule
- C08G64/20—General preparatory processes
- C08G64/205—General preparatory processes characterised by the apparatus used
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L69/00—Compositions of polycarbonates; Compositions of derivatives of polycarbonates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B08—CLEANING
- B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
- B08B2209/00—Details of machines or methods for cleaning hollow articles
- B08B2209/02—Details of apparatuses or methods for cleaning pipes or tubes
- B08B2209/027—Details of apparatuses or methods for cleaning pipes or tubes for cleaning the internal surfaces
- B08B2209/032—Details of apparatuses or methods for cleaning pipes or tubes for cleaning the internal surfaces by the mechanical action of a moving fluid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/32—Mixing; Kneading continuous, with mechanical mixing or kneading devices with non-movable mixing or kneading devices
- B29B7/325—Static mixers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
- B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
Abstract
The invention discloses a kind of polycarbonate preparation systems, it solves since cleaning needs a large amount of aromatic hydroxy compound, the problem of to increase environmental pressure, its key points of the technical solution are that: the system includes polycondensation reaction mechanism, auxiliary agent adds mechanism, hybrid filtering mechanism, extrusion molding granulating mechanism, phenol wiper mechanism is also connected between the polycondensation reaction mechanism and extrusion molding granulating mechanism, the phenol wiper mechanism includes the phenol recovery tank being connected between fondant filter and extrusion molding granulating mechanism, the bottom of the phenol recovery tank is provided with heating device, the phenol recovery tank is connected between polycondensation reactor and static mixer by cooling pipe, the first booster pump is provided on the cooling pipe, avoid the waste of phenol, improve the utilization rate of phenol, it reduces since the waste liquid that cleaning equipment generates makes environment At pressure.
Description
Technical field
The present invention relates to high molecular material, in particular to a kind of polycarbonate preparation system.
Background technique
Polycarbonate (polycarbonate, PC) is a kind of thermoplastic engineering plastic of function admirable, is had outstanding anti-
Impact capacity, creep resistance, it is in five large-engineering plastics that good stability of the dimension is heat-resisting, water absorption rate is low, nontoxic, dielectric properties are excellent
Unique product with good transparency, and the most fast general engineering plastic of growth rate in recent years, can be applied to glass plate,
Automobile Products, electrical appliance, optical articles etc., the market demand is increasing.Most of manufacturer is universal in the world at present
Using interface polycondensation or melt transesterification process.
Different from general polymerization object, due to the particularity of the structure of polycarbonate, to shear-sensitive.Shear action is easy
Cause polycarbonate degradation to generate conjugation chromophoric group, and then xanthochromia occur, the yellow colour index of polycarbonate particle is caused to increase,
It is unfavorable for later product deep processing, the application field especially having higher requirements to optical properties such as product light transmittance, mist degrees.
For ester exchange process, the terminal hydroxyl content of polycarbonate strand is relatively high.Since hydroxyl belongs to pole
Property group, be easy with metal occur adhesion effect, it is contemplated that polycarbonate melt oneself viscosity is big, material in-line stop when
Between it is longer, be easy to cause quality decline, and rest on dead angle for a long time pipeline is vortexed, localized degradation occurs in dead zone
Polycarbonate can crack carbonization, polluted product while, will also result in internal system carbon distribution, reduce equipment, pipe heat-transfer effect
Fruit influences production efficiency and product quality.
For this purpose, pipeline and preparing the needs of equipment used in polycarbonate and periodically being cleaned, general cleaning solution is fragrant
Race's monohydroxy compound, but since cleaning needs a large amount of aromatic hydroxy compound, and the hydroxy compounds of cleaning solution is only
It can serve as liquid waste processing, to increase environmental pressure.
Summary of the invention
The object of the present invention is to provide a kind of polycarbonate preparation systems, can be sufficiently mixed guaranteeing polycarbonate with auxiliary agent
Under the premise of, the yellow colour index of polycarbonate is effectively reduced, while cleaning solution is Ke Xunhuanliyong, reduces since cleaning equipment produces
Raw waste liquid pressure caused by environment.
Above-mentioned technical purpose of the invention has the technical scheme that
A kind of polycarbonate preparation system, the system include hybrid filtering mechanism and the contracting that connect with hybrid filtering mechanism
Poly- reaction mechanism and auxiliary agent add mechanism, and the hybrid filtering mechanism is also connected with extrusion molding granulating mechanism, the polycondensation reaction machine
Structure includes the polycondensation reactor that prepolymer product is polycondensed into polycarbonate melt using non-phosgene fusion method；The hybrid filtering machine
Structure includes the static mixer for being connected to polycondensation reactor and auxiliary agent add-on system, and the static mixer is connected with melt filtration
Device；Phenol wiper mechanism, the phenol wiper mechanism packet are also connected between the polycondensation reaction mechanism and extrusion molding granulating mechanism
The phenol recovery tank being connected between fondant filter and extrusion molding granulating mechanism is included, the bottom of the phenol recovery tank, which is provided with, to be added
Thermal, the phenol recovery tank are connected between polycondensation reactor and static mixer by cooling pipe, the cooling tube
The first booster pump is provided on road.
By using above-mentioned technical proposal, prepolymer product polycondensation is made poly- by polycondensation reaction mechanism application non-phosgene fusion method
Carbonic ester melt, the auxiliary agent in polycarbonate melt and auxiliary agent add-on system pass through pipeline transportation to static mixer respectively,
Uniform mixing is realized in static mixer, and under the premise of guaranteeing mixing adequately, by fondant filter to polycarbonate
Macromolecular gel present in melt is filtered, and gel is avoided to influence product quality, and extruding pelletization does not cause polycarbonate to exist
The extension of residence time in system avoids polycarbonate melt because of heated for a long time and aging, yellow occurs, ensure that product
Have preferable color and excellent mechanical performance；Cleaning solvent of the phenol as polycarbonate is remained in by dissolution
Polycarbonate melt in hybrid filtering mechanism makes remaining polycarbonate depolymerization form oligomer diphenyl carbonate and bisphenol-A,
And be dissolved in phenol and flowed back into phenol recovery tank together, since the bottom of phenol recovery tank is provided with heating device, reflux
After the heating, phenol gasification separates phenol in phenol recovery tank with oligomer, and the phenol after gasification passes through cooling pipe liquid
After change, the phenol after liquefaction can be passed through static mixer again by pipeline, clean again to pipeline and hybrid filtering mechanism；
The cleaning for remaining in pipeline, the polycarbonate that dead zone generation cracking is carbonized is realized by above-mentioned design, avoids system
Internal carbon distribution reduces the heat-transfer effect of equipment, pipeline, ensure that production efficiency stable in equipment operation production process, while energy
The influence of residue that polycarbonate melt is carbonized due to dead zone to product quality is enough effectively reduced, avoids product from occurring burnt
Grain, stain, and phenol can recycle, and avoid the waste of phenol, improve the utilization rate of phenol, reduce due to cleaning
Waste liquid pressure caused by environment that equipment generates.
Preferably, the phenol recovery tank is connected with liquid waste incinerator.
By using above-mentioned technical proposal, phenol after cleaning after heating, the phenol uplink that gasifies and be still liquefaction shape
The waste liquid containing oligomer of state remains in the bottom of phenol recovery tank, and the waste liquid containing oligomer is directly connected to liquid waste incineration
Furnace, waste liquid is although unvaporized at this time, but under the heating of heating device, and still in the condition of high temperature, the waste liquid containing oligomer is burnt
It burns, the waste liquid containing oligomer can be shortened and be heated to the ignition temperature desired time.
Preferably, being provided with first gear pump, pipe on pipeline between the polycondensation reactor and static mixer
Road includes branch, and branch road is provided with second gear pump.
By using above-mentioned technical proposal, since the viscosity of polycarbonate melt changes very big, use in temperature-rise period
The flow that gear pump can be such that polycarbonate melt keeps constant in the duct is avoided due to polycarbonate melt in the duct
Flow velocity too fast appearance turbulent flow, accelerate tube wall loss, also can be avoided since laminar flow occurs slowly excessively in flow velocity, cause polycarbonate molten
Body does not utilize the long-time service of pipeline equally for a long time in near-wall；The second gear pump designed in bypass can be used as increasing
Press pump, the lift for avoiding first gear from pumping is excessive, and excessive load is caused to upstream device, meanwhile, second gear is pumped and is designed
In branch, the flexibility of pipe control can be increased, select whether second gear pump is reinstated according to practical condition, in pipe
When pressure is enough, closing branch can choose, reduce the circulation distance of pipeline, shorten polycarbonate melt in pipeline
In residence time.
Preferably, the phenol recovery tank is also connected with pre- wet air duct, the pre- wet air duct is connected by the second booster pump
It connects on the pipeline between first gear pump and static mixer.
By using above-mentioned technical proposal, pre- wet air duct can the system enable before, to pipeline and hybrid filtering mechanism
It carries out gasification phenol to prewet, Certain residues is dissolved out, while preheating to pipeline, then in the phenol that will be in liquefaction
Cleaning solution is squeezed into pipeline, carries out secondary cleaning to pipeline, pipeline carries out heat exchange, phenol cleaning solution in the pipeline after preheating
Cleaning effect is more preferable, dissolve out residuum, and be discharged in the duct and together with liquefied phenol.
Preferably, the auxiliary agent addition mechanism includes several auxiliary agent melting tanks being mutually in parallel, the auxiliary agent melts tank
Lower section be provided with the heat-conducting medium heating mechanism of auxiliary agent meltingization.
By using above-mentioned technical proposal, the auxiliary agent that is mutually in parallel melting tank can according to the trade mark demand of polycarbonate from
By selection auxiliary agent collocation mode, setting can be farthest adjusted；Auxiliary agent is heated to melting by heat-conducting medium heating mechanism
State improves the uniform slot bottom mixed between the two, while reducing two when auxiliary agent is mixed with polycarbonate melt
The temperature difference between person avoids the addition due to auxiliary agent from influencing the temperature of polycarbonate melt, and polycarbonate melt is made to keep stablizing
State.
Preferably, adding y-type filter on the outlet conduit of the auxiliary agent melting tank.
By using above-mentioned technical proposal, y-type filter has the characteristics that resistance is small, blowdown is convenient, can helping melting
Solid impurity particle screen selecting present in agent comes out, and avoids solid particle polluter from influencing downstream line and rear method, apparatus, avoids
Accessory on pipeline, equipment, which is worn, even to be blocked, and enables a device to work normally, meanwhile, the filter cylinder of y-type filter is convenient
Disassembly, it is easy to maintain.
Preferably, the auxiliary agent melting tank passes through high-pressure sprayer and is connected on static premixed device.
By using above-mentioned technical proposal, the design of high-pressure sprayer can make the auxiliary agent of molten condition with spray discharge pattern into
Enter in static premixed device, realization is uniformly dispersed, and under the premise of keeping being uniformly mixed, shortens the incorporation time of auxiliary agent.
Preferably, the static state premixed device and static mixer are all made of SMX Plus hybrid element.
By using above-mentioned technical proposal, SMX Plus hybrid element has both most effective mixed compared to other product mix
The pressure drop of effect and only usual mixer 50% is closed, significantly reducing pressure drop can be used the small-power of more low energy consumption
Pump saves cost；Or use smaller mixer polycarbonate melt residence time in a device is greatly shortened, thus
Reduce the degradation rate of material in the duct.
Preferably, the static state premixed device is connected on static mixer by diaphragm booster pump.
By using above-mentioned technical proposal, after passing through static premixed device due to the auxiliary agent in molten condition, flow velocity can be big
It is big to reduce, and polycarbonate melt when by pipeline to static mixer, will increase static mixer after polycondensation reaction
Interior pressure, when pressure is excessive, auxiliary agent is difficult to be added in static mixer, therefore is helped by needing diaphragm pump to pump
Agent, while the setting of diaphragm pump is able to ascend mixing efficiency of the auxiliary agent in static premixed device, shortens incorporation time.
Preferably, the fondant filter selects disc-type filter or candle wick formula filter, and its filter element
Metal establishment strainer or metal is selected to filter felt, the filtering accuracy of the filter element is 1~40 μm.
By using above-mentioned technical proposal, since under high-temperature and high-pressure conditions, the macromolecular gel of polycarbonate melt exists
Deformational behavior, readily penetrates through strainer, and metal establishment strainer uses multilayer expansion aluminum foil web or stainless (steel) wire for the dedicated of filter
Filter material is rolled into wave net form, is formed by stacking so that correct angle is intersected with each other；Multilayer folding expansion is with different close
Degree, the arrangement of aperture from thick to thin, can make polycarbonate melt when through filter screen, flow direction is varied multiple times；Gold
Belonging to filter felt has the features such as three-dimensional netted, porous structure, porosity is high, and surface area is big, and size distribution is uniform, effectively more
It mends that metal Netease is stifled, delicate weakness, can make up for it the deficiency that powder filter product is frangible, flow is small, high porosity and excellent
Permeability, the pressure loss is small, and flow is big；Metal establishment strainer or metal filter felt can avoid passing through deformation through strainer
Macromolecular gel.
In conclusion the invention has the following advantages:
1, the polycarbonate preparation system by polycondensation reaction mechanism and auxiliary agent add mechanism pass through pipeline be connected to it is mixed
The combination for closing filter mechanism and extrusion molding granulating mechanism produces polycarbonate due to shearing force instead of with conventional twin screw extruder
The problem of causing polycarbonate to be easy xanthochromia, influence of the threaded rod shear shear force to polycarbonate molecule is avoided, compared to Screw Extrusion
Polycarbonate is manufactured, xanthochromia and light transmittance are significantly optimized；
2, the polycarbonate preparation system passes through the phenol wiper mechanism of cyclic design, cleans to pipeline and equipment,
Avoid polycarbonate melt remain in pipeline, dead zone occur cracking carbonization, avoid internal system carbon distribution reduce equipment,
The heat-transfer effect of pipeline, ensure that stable production efficiency in equipment operation production process, and recyclable phenol reduce by
In waste liquid pressure caused by environment that cleaning equipment generates.
Detailed description of the invention
Fig. 1 is a kind of overall flow figure of polycarbonate preparation system.
In figure, 1, polycondensation reactor；11, first gear pumps；12, second gear pumps；21, static mixer；22, melt mistake
Filter；31, auxiliary agent melts tank；311, antioxidant melts tank；312, release agent melts tank；313, ultraviolet absorbing agent melts tank；
314, the first toner melts tank；315, the second toner melts tank；316, third toner melts tank；32, y-type filter；33, static
Premixed device；34, diaphragm booster pump；41, die head；42, pelleter；5, phenol recovery tank；51, the first booster pump；52, the second pressurization
Pump, 53, third booster pump.
Specific embodiment
Below in conjunction with attached drawing, invention is further described in detail.
Referring to Fig. 1, a kind of polycarbonate preparation system, including be applied to non-phosgene and prepolymer product is polycondensed into poly- carbonic acid
The polycondensation reaction mechanism of ester melt and auxiliary agent for adding auxiliary agent add mechanism.Polycondensation reaction mechanism and auxiliary agent addition mechanism are equal
It is connected to hybrid filtering mechanism by pipeline, by hybrid filtering mechanism by after polycarbonate melt and auxiliary agent hybrid filtering, is led to
The extrusion molding granulating mechanism extruding pelletization after being connected to hybrid filtering mechanism is crossed, polycarbonate products are obtained.
Hybrid filtering mechanism includes by static mixer 21 that material mixes and being connected to 21 rear of static mixer and being used for
Separate the fondant filter 22 of the macromolecular gel in melt.Static mixer 21 uses stainless steel, steel of the grade of steel for 1.4418
Number for 1.4571 stainless steel, HasteAlloy 59 or Incone alloy one of which as Outer Tube, and Outer Tube is equal
It is processed by shot blasting, until roughness reaches RA0.5, and is mixed using the SMX Plus hybrid element of Sulzer company as internal
Close element.Fondant filter 22 selects the one of which of disk filter or candle wick formula filter, the wherein filtering of filter
It is that 1~40 μm of metal works out strainer or metal filters filter element of the one of which of felt as melt that element, which selects filtering accuracy,.
Polycondensation reaction mechanism includes polycondensation reactor 1, and polycondensation reactor 1 is connect by pipeline with static mixer 21.Pipe
Road is the one of which of stainless steel 304 L or Stainless steel 316 0L, and pipeline passes through polishing treatment, and roughness reaches RA0.5.Polycondensation
First gear pump 11 is provided on the pipeline of reactor 1 and static mixer 21, pipeline further includes setting in first gear pump 11
Branch between static mixer 21, branch road are provided with second gear pump 12.
Auxiliary agent add-on system includes several auxiliary agent melting tanks 31 being mutually in parallel, and auxiliary agent melting tank 31 includes that antioxidant is molten
Melt tank 311, release agent melting tank 312, ultraviolet absorbing agent melting tank 313, the first toner melting tank 314, the melting of the second toner
Tank 315, third toner melt tank 316, and the lower section of above-mentioned auxiliary agent melting tank 31 is provided with the heat-conducting medium of auxiliary agent meltingization
Heating mechanism, heat-conducting medium therein are the conduction oil for concentrating heat treatment, and heat-conducting medium heating mechanism will be helped by conduction oil
Agent is heated to the temperature of fusing point or more, keeps auxiliary agent in a molten state.And add on the outlet conduit of above-mentioned auxiliary agent melting tank 31
Equipped with y-type filter 32, auxiliary agent melting tank 31 is all connected in static premixed device 33 by pipeline, and auxiliary agent melts tank 31 and quiet
The pipeline of state premixed device 33 also on be equipped with that high-pressure fog is added to static premixed device in liquid form by the auxiliary agent of molten condition
High-pressure sprayer in 33.Static premixed device 33 is connected on static mixer 21 by diaphragm booster pump 34, by auxiliary agent and contracting
It is mixed after poly- by the polycarbonate melt of pipeline to static mixer 21.
Mixed polycarbonate melt passes through extrusion granulating mechanism after filtering macromolecular gel by fondant filter 22
Extruder die head 41 squeeze out after be granulated by pelleter 42, obtain polycarbonate products.
The polycarbonate preparation system further includes having phenol wiper mechanism, and phenol wiper mechanism includes phenol recovery tank 5, benzene
Phenol cleaning solution is connected to 1 rear of polycondensation reactor by being provided with the cooling pipe of the first booster pump 51 by phenol recycling can 5
On pipeline, 1 rear pipeline of polycondensation reactor and static mixer 21 and fondant filter 22 are carried out by phenol cleaning solution
Cleaning, the phenol cleaning solution cleaned are flowed back together with waste liquid by being connected to return pipe between fondant filter 22 and die head 41
To phenol recovery tank 5.The bottom of phenol recovery tank 5 is provided with heating device, and heating device is similarly to be heated by concentrating
Conduction oil, phenol is heated to boiling point by conduction oil, phenol gasification volatilization, is also connected with pre- wet air duct in phenol recovery tank 5, in advance
Wet air duct is connected on the pipeline between first gear pump 11 and static mixer 21 by the second booster pump 52, the second booster pump
52 are delivered to partial gasification phenol the pipeline for being used to convey polycarbonate melt and static mixer 21 and melt filtration
In device 22, the condensation after the cooling pipe for being provided with the first booster pump 51 exchanges heat of partial gasification phenol is collected or is directly entered
Secondary cleaning is carried out to pipeline into pipeline.First booster pump 51 is run when different from the second booster pump 52.Waste liquid remains in benzene
It is connected in liquid waste incinerator and is burned by devil liquor recovery pipe in phenol recycling can 5.
It by the polycarbonate preparation system prepared by the polycarbonate of the different trades mark, scheme is as follows:
Embodiment one
The valve that the valve and polycondensation reactor 1 that Step1 is closed between fondant filter 22 and die head 41 are connect with pipeline
Door, opens polycondensation reactor 1 to other valves between fondant filter 22, by the first booster pump 51 by phenol recovery tank 5
Interior phenol indentation pipeline, static mixer 21, in fondant filter 22, until keeping 10min after liquid level stabilizing；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step2
In tank 5；
Step3 closes the connecting valve of phenol wiper mechanism and pipeline, sets condensation temperature as 270 DEG C, by polycondensation reaction
After device 1 preheats, prepolymer product is delivered in polycondensation reactor 1, and by temperature control between 268 DEG C~272 DEG C, pressure control
System makes prepolymer product form polycarbonate melt, melt viscosity 400Pa after polycondensation between 0.10KPa~1.5Kpa
s；
Step4 polycarbonate melt is delivered in static mixer 21 by the first booster pump 51；
Step5 selects antioxidant melting tank 311, release agent melting tank 312, ultraviolet absorbing agent to melt tank 313, first
Toner melts tank 314 and by heat-conducting oil heating, and auxiliary agent is melted auxiliary agent temperature in tank 31 and is promoted to fusing point or more, is melted
The auxiliary agent of state；
After Step6 molten condition auxiliary agent is filtered by y-type filter 32, molten state is helped by high-pressure sprayer respectively
Agent sprays into static premixed device 33, realizes auxiliary agent premix；
The auxiliary agent for completing premix is delivered in static mixer 21 by Step7 by diaphragm booster pump 34, with polycarbonate
Melt is mixed；
Step8 completes mixed melt and squeezes out after the filtering of fondant filter 22 from die head 41, and passes through pelleter
42 pelletizings obtain the polycarbonate products that the trade mark is A；
It after the completion of Step9 manufacture, is heated by conduction oil Pyrogentisinic Acid recycling can 5, is warming up to phenol gasification, waste liquid
Still in liquid, gasification phenol is liquefied after cooling pipe is cooling, by liquefied phenol under the action of the first booster pump 51
Again pipeline, static mixer 21 are pressed into, in fondant filter 22, until keeping 10min after liquid level stabilizing, waste liquid is returned from phenol
5 bottom of closed cans is connected in liquid waste incinerator by devil liquor recovery pipe is burned；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step10
In tank 5.
Embodiment two
The valve that the valve and polycondensation reactor 1 that Step1 is closed between fondant filter 22 and die head 41 are connect with pipeline
Door, opens polycondensation reactor 1 to other valves between fondant filter 22, by the first booster pump 51 by phenol recovery tank 5
Interior phenol indentation pipeline, static mixer 21, in fondant filter 22, until keeping 10min after liquid level stabilizing；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step2
In tank 5；
Step3 closes the connecting valve of phenol wiper mechanism and pipeline, sets condensation temperature as 290 DEG C, by polycondensation reaction
After device 1 preheats, prepolymer product is delivered in polycondensation reactor 1, and by temperature control between 288 DEG C~292 DEG C, pressure control
System makes prepolymer product form polycarbonate melt, melt viscosity 800Pas after polycondensation between 0.1KPa~1.5Kpa；
Step4 polycarbonate melt is delivered in static mixer 21 by the first booster pump 51；
Step5 selects antioxidant melting tank 311, release agent melting tank 312, ultraviolet absorbing agent to melt tank 313, first
Toner melts tank 314 and by heat-conducting oil heating, and auxiliary agent is melted auxiliary agent temperature in tank 31 and is promoted to fusing point or more, is melted
The auxiliary agent of state；
After Step6 molten condition auxiliary agent is filtered by y-type filter 32, molten state is helped by high-pressure sprayer respectively
Agent sprays into static premixed device 33, realizes auxiliary agent premix；
The auxiliary agent for completing premix is delivered in static mixer 21 by Step7 by diaphragm booster pump 34, with polycarbonate
Melt is mixed；
Step8 completes mixed melt and squeezes out after the filtering of fondant filter 22 from die head 41, and passes through pelleter
42 pelletizings obtain the polycarbonate products that the trade mark is B；
It after the completion of Step9 manufacture, is heated by conduction oil Pyrogentisinic Acid recycling can 5, is warming up to phenol gasification, waste liquid
Still in liquid, gasification phenol is liquefied after cooling pipe is cooling, by liquefied phenol under the action of the first booster pump 51
Again pipeline, static mixer 21 are pressed into, in fondant filter 22, until keeping 10min after liquid level stabilizing, waste liquid is returned from phenol
5 bottom of closed cans is connected in liquid waste incinerator by devil liquor recovery pipe is burned；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step10
In tank 5.
Embodiment three
The valve that the valve and polycondensation reactor 1 that Step1 is closed between fondant filter 22 and die head 41 are connect with pipeline
Door, opens polycondensation reactor 1 to other valves between fondant filter 22, by the first booster pump 51 by phenol recovery tank 5
Interior phenol indentation pipeline, static mixer 21, in fondant filter 22, until keeping 10min after liquid level stabilizing；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step2
In tank 5；
Step3 closes the connecting valve of phenol wiper mechanism and pipeline, sets condensation temperature as 270 DEG C, by polycondensation reaction
After device 1 preheats, prepolymer product is delivered in polycondensation reactor 1, and by temperature control between 268 DEG C~272 DEG C, pressure control
System makes prepolymer product form polycarbonate melt, melt viscosity 800Pa after polycondensation between 0.02KPa~1.5Kpa
s；
Step4 polycarbonate melt is delivered in static mixer 21 by the first booster pump 51 and the second booster pump 52；
Step5 selects antioxidant melting tank 311, release agent melting tank 312, ultraviolet absorbing agent to melt tank 313, second
Toner melts tank 315 and by heat-conducting oil heating, and auxiliary agent is melted auxiliary agent temperature in tank 31 and is promoted to fusing point or more, is melted
The auxiliary agent of state；
After Step6 molten condition auxiliary agent is filtered by y-type filter 32, molten state is helped by high-pressure sprayer respectively
Agent sprays into static premixed device 33, realizes auxiliary agent premix；
The auxiliary agent for completing premix is delivered in static mixer 21 by Step7 by diaphragm booster pump 34, with polycarbonate
Melt is mixed；
Step8 completes mixed melt and squeezes out after the filtering of fondant filter 22 from die head 41, and passes through pelleter
42 pelletizings obtain the polycarbonate products that the trade mark is C；
It after the completion of Step9 manufacture, is heated by conduction oil Pyrogentisinic Acid recycling can 5, is warming up to phenol gasification, waste liquid
Still in liquid, gasification phenol is liquefied after cooling pipe is cooling, by liquefied phenol under the action of the first booster pump 51
Again pipeline, static mixer 21 are pressed into, in fondant filter 22, until keeping 10min after liquid level stabilizing, waste liquid is returned from phenol
5 bottom of closed cans is connected in liquid waste incinerator by devil liquor recovery pipe is burned；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step10
In tank 5.
Example IV
The valve that the valve and polycondensation reactor 1 that Step1 is closed between fondant filter 22 and die head 41 are connect with pipeline
Door, opens polycondensation reactor 1 to other valves between fondant filter 22, by the first booster pump 51 by phenol recovery tank 5
Interior phenol indentation pipeline, static mixer 21, in fondant filter 22, until keeping 10min after liquid level stabilizing；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step2
In tank 5；
Step3 closes the connecting valve of phenol wiper mechanism and pipeline, sets condensation temperature as 300 DEG C, by polycondensation reaction
After device 1 preheats, prepolymer product is delivered in polycondensation reactor 1, and by temperature control between 298 DEG C~302 DEG C, pressure control
System makes prepolymer product form polycarbonate melt, melt viscosity 800Pa after polycondensation between 0.15KPa~1.5Kpa
s；
Step4 polycarbonate melt is delivered in static mixer 21 by the first booster pump 51；
Step5 selects antioxidant melting tank 311, release agent melting tank 312, ultraviolet absorbing agent to melt tank 313, second
Toner melts tank 315 and by heat-conducting oil heating, and auxiliary agent is melted auxiliary agent temperature in tank 31 and is promoted to fusing point or more, is melted
The auxiliary agent of state；
After Step6 molten condition auxiliary agent is filtered by y-type filter 32, molten state is helped by high-pressure sprayer respectively
Agent sprays into static premixed device 33, realizes auxiliary agent premix；
The auxiliary agent for completing premix is delivered in static mixer 21 by Step7 by diaphragm booster pump 34, with polycarbonate
Melt is mixed；
Step8 completes mixed melt and squeezes out after the filtering of fondant filter 22 from die head 41, and passes through pelleter
42 pelletizings obtain the polycarbonate products that the trade mark is D；
It after the completion of Step9 manufacture, is heated by conduction oil Pyrogentisinic Acid recycling can 5, is warming up to phenol gasification, waste liquid
Still in liquid, gasification phenol is liquefied after cooling pipe is cooling, by liquefied phenol under the action of the first booster pump 51
Again pipeline, static mixer 21 are pressed into, in fondant filter 22, until keeping 10min after liquid level stabilizing, waste liquid is returned from phenol
5 bottom of closed cans is connected in liquid waste incinerator by devil liquor recovery pipe is burned；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step10
In tank 5.
Embodiment five
The valve that the valve and polycondensation reactor 1 that Step1 is closed between fondant filter 22 and die head 41 are connect with pipeline
Door, opens polycondensation reactor 1 to other valves between fondant filter 22, by the first booster pump 51 by phenol recovery tank 5
Interior phenol indentation pipeline, static mixer 21, in fondant filter 22, until keeping 10min after liquid level stabilizing；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step2
In tank 5；
Step3 closes the connecting valve of phenol wiper mechanism and pipeline, sets condensation temperature as 270 DEG C, by polycondensation reaction
After device 1 preheats, prepolymer product is delivered in polycondensation reactor 1, and by temperature control between 268 DEG C~272 DEG C, pressure control
System makes prepolymer product form polycarbonate melt, melt viscosity 1100Pa after polycondensation between 0.01KPa~1.0Kpa
s；
Step4 polycarbonate melt is delivered in static mixer 21 by the first booster pump 51 and the second booster pump 52；
Step5 selects antioxidant melting tank 311, release agent melting tank 312, ultraviolet absorbing agent to melt tank 313, third
Toner melts tank 316 and by heat-conducting oil heating, and auxiliary agent is melted auxiliary agent temperature in tank 31 and is promoted to fusing point or more, is melted
The auxiliary agent of state；
After Step6 molten condition auxiliary agent is filtered by y-type filter 32, molten state is helped by high-pressure sprayer respectively
Agent sprays into static premixed device 33, realizes auxiliary agent premix；
The auxiliary agent for completing premix is delivered in static mixer 21 by Step7 by diaphragm booster pump 34, with polycarbonate
Melt is mixed；
Step8 completes mixed melt and squeezes out after the filtering of fondant filter 22 from die head 41, and passes through pelleter
42 pelletizings obtain the polycarbonate products that the trade mark is E；
It after the completion of Step9 manufacture, is heated by conduction oil Pyrogentisinic Acid recycling can 5, is warming up to phenol gasification, waste liquid
Still in liquid, gasification phenol is liquefied after cooling pipe is cooling, by liquefied phenol under the action of the first booster pump 51
Again pipeline, static mixer 21 are pressed into, in fondant filter 22, until keeping 10min after liquid level stabilizing, waste liquid is returned from phenol
5 bottom of closed cans is connected in liquid waste incinerator by devil liquor recovery pipe is burned；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step10
In tank 5.
Embodiment six
The valve that the valve and polycondensation reactor 1 that Step1 is closed between fondant filter 22 and die head 41 are connect with pipeline
Door, opens polycondensation reactor 1 to other valves between fondant filter 22, by the first booster pump 51 by phenol recovery tank 5
Interior phenol indentation pipeline, static mixer 21, in fondant filter 22, until keeping 10min after liquid level stabilizing；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step2
In tank 5；
Step3 closes the connecting valve of phenol wiper mechanism and pipeline, sets condensation temperature as 290 DEG C, by polycondensation reaction
After device 1 preheats, prepolymer product is delivered in polycondensation reactor 1, and by temperature control between 288 DEG C~292 DEG C, pressure control
System makes prepolymer product form polycarbonate melt, melt viscosity 1100Pa after polycondensation between 0.02KPa~1.5Kpa
s；
Step4 polycarbonate melt is delivered in static mixer 21 by the first booster pump 51 and the second booster pump 52；
Step5 selects antioxidant melting tank 311, release agent melting tank 312, ultraviolet absorbing agent to melt tank 313, third
Toner melts tank 316 and by heat-conducting oil heating, and auxiliary agent is melted auxiliary agent temperature in tank 31 and is promoted to fusing point or more, is melted
The auxiliary agent of state；
After Step6 molten condition auxiliary agent is filtered by y-type filter 32, molten state is helped by high-pressure sprayer respectively
Agent sprays into static premixed device 33, realizes auxiliary agent premix；
The auxiliary agent for completing premix is delivered in static mixer 21 by Step7 by diaphragm booster pump 34, with polycarbonate
Melt is mixed；
Step8 completes mixed melt and squeezes out after the filtering of fondant filter 22 from die head 41, and passes through pelleter
42 pelletizings obtain the polycarbonate products that the trade mark is F；
It after the completion of Step9 manufacture, is heated by conduction oil Pyrogentisinic Acid recycling can 5, is warming up to phenol gasification, waste liquid
Still in liquid, gasification phenol is liquefied after cooling pipe is cooling, by liquefied phenol under the action of the first booster pump 51
Again pipeline, static mixer 21 are pressed into, in fondant filter 22, until keeping 10min after liquid level stabilizing, waste liquid is returned from phenol
5 bottom of closed cans is connected in liquid waste incinerator by devil liquor recovery pipe is burned；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step10
In tank 5.
Comparative example one
The extrusion temperature for controlling double screw extruder is 270 DEG C, and melt extrusion viscosity is the polycarbonate of 400Pas, is obtained
The polycarbonate products particle for being A to the trade mark.
Comparative example two
The extrusion temperature for controlling double screw extruder is 290 DEG C, and melt extrusion viscosity is the polycarbonate of 800Pas, is obtained
The polycarbonate products particle for being B to the trade mark.
Comparative example three
The extrusion temperature for controlling double screw extruder is 290 DEG C, and melt extrusion viscosity is the polycarbonate of 1100Pas,
Obtain the polycarbonate products particle that the trade mark is A.
Each trade mark polycarbonate products obtained are subjected to yellow colour index and light transmittance detection, retest 20 times, are taken
Average value.Test method:
1, it is molded sampling
Each trade mark polycarbonate products particle obtained is directly molded after 120 DEG C of removal moisture drying 4h, print is made；Control
300 DEG C of injection temperature processed, 80 DEG C of mold temperature；
2, testing standard
A, yellow colour index (YI), print thickness 4mm are tested according to ASTM E313 standard；
B, light transmittance (%), print thickness 4mm, installation ASTM D1003 standard are tested.
Test result see the table below:
To sum up, which is suitable for a variety of trades mark, and melt viscosity is in 400~1100Pas range
The extruding pelletization of polycarbonate melt avoids the particularity due to polycarbonate molecular structure, polycarbonate is caused to shear
It is easy to happen degradation under effect and generates conjugation chromophoric group, alleviates the xanthochromia degree of polycarbonate, reduces polycarbonate grain
The yellow colour index of son, while the light transmittance of polycarbonate particle is improved, be conducive to the post-production of polycarbonate particle；
Wherein, especially optimal with the yellow colour index of polycarbonate particle obtained by condition selected by embodiment three and light transmittance, because
This, selection example three carries out next step experiment as optimum embodiment.
Embodiment seven
The valve that the valve and polycondensation reactor 1 that Step1 is closed between fondant filter 22 and die head 41 are connect with pipeline
Door opens polycondensation reactor 1 to other valves between fondant filter 22, by heating oil heating phenol recovery tank 5
Phenol makes phenol gasify, start the second booster pump 52, by pre- wet air duct will gasify phenol be passed through pipeline, static mixer 21,
In fondant filter 22,3min is kept, incipient wetness, cleaning and preheating are carried out to pipeline；
Step2 close the second booster pump 52, by the first booster pump 51 by phenol recovery tank 5 phenol be pressed into pipeline,
In static mixer 21, fondant filter 22, until keeping 10min after liquid level stabilizing；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step3
In tank 5；
Step4 closes the connecting valve of phenol wiper mechanism and pipeline, sets condensation temperature as 270 DEG C, by polycondensation reaction
After device 1 preheats, prepolymer product is delivered in polycondensation reactor 1, and by temperature control between 268 DEG C~272 DEG C, pressure control
System makes prepolymer product form polycarbonate melt, melt viscosity 800Pa after polycondensation between 0.02KPa~1.5Kpa
s；
Step5 polycarbonate melt is delivered in static mixer 21 by the first booster pump 51 and the second booster pump 52；
Step6 selects antioxidant melting tank 311, release agent melting tank 312, ultraviolet absorbing agent to melt tank 313, second
Toner melts tank 315 and by heat-conducting oil heating, and auxiliary agent is melted auxiliary agent temperature in tank 31 and is promoted to fusing point or more, is melted
The auxiliary agent of state；
After Step7 molten condition auxiliary agent is filtered by y-type filter 32, molten state is helped by high-pressure sprayer respectively
Agent sprays into static premixed device 33, realizes auxiliary agent premix；
The auxiliary agent for completing premix is delivered in static mixer 21 by Step8 by diaphragm booster pump 34, with polycarbonate
Melt is mixed；
Step9 completes mixed melt and squeezes out after the filtering of fondant filter 22 from die head 41, and passes through pelleter
42 pelletizings obtain the polycarbonate products that the trade mark is C；
It after the completion of Step10 manufacture, is heated by conduction oil Pyrogentisinic Acid recycling can 5, is warming up to phenol gasification, waste liquid
Still in liquid, gasification phenol is liquefied after cooling pipe is cooling, by liquefied phenol under the action of the first booster pump 51
Again pipeline, static mixer 21 are pressed into, in fondant filter 22, until keeping 10min after liquid level stabilizing, waste liquid is returned from phenol
5 bottom of closed cans is connected in liquid waste incinerator by devil liquor recovery pipe is burned；
The phenol cleaning solution dissolved with waste liquid in pipeline is delivered to phenol recovery by third booster pump 53 by Step11
In tank 5.
Test result see the table below:
To sum up, it after gasification phenol wetting, then is cleaned by phenol cleaning solution, more to the cleaning effect of pipeline and equipment
It is good, it reduces in last time preparation, the remaining polycarbonate melt of institute in system can reduce yellow colour index, improve light transmittance.
This specific embodiment is only explanation of the invention, is not limitation of the present invention, those skilled in the art
Member can according to need the modification that not creative contribution is made to the present embodiment after reading this specification, but as long as at this
All by the protection of Patent Law in the scope of the claims of invention.
Claims (10)
1. a kind of polycarbonate preparation system, which includes hybrid filtering mechanism and the polycondensation that connect with hybrid filtering mechanism
Reaction mechanism and auxiliary agent add mechanism, and the hybrid filtering mechanism is also connected with extrusion molding granulating mechanism, which is characterized in that the contracting
Poly- reaction mechanism includes the polycondensation reactor (1) that prepolymer product is polycondensed into polycarbonate melt using non-phosgene fusion method；Institute
Stating hybrid filtering mechanism includes the static mixer (21) for being connected to polycondensation reactor (1) and auxiliary agent add-on system, the static state
Mixer (21) is connected with fondant filter (22)；Phenol is also connected between the polycondensation reaction mechanism and extrusion molding granulating mechanism
Wiper mechanism, the phenol wiper mechanism include the phenol recovery being connected between fondant filter (22) and extrusion molding granulating mechanism
Tank (5), the bottom of the phenol recovery tank (5) are provided with heating device, and the phenol recovery tank (5) is connected by cooling pipe
To between polycondensation reactor (1) and static mixer (21), the first booster pump (51) are provided on the cooling pipe.
2. a kind of polycarbonate preparation system according to claim 1, the phenol recovery tank (5) is connected with liquid waste incineration
Furnace.
3. a kind of polycarbonate preparation system according to claim 1, which is characterized in that the polycondensation reactor (1) and
First gear pump (11) is provided on pipeline between static mixer (21), pipeline includes branch, and branch road is arranged
There is second gear to pump (12).
4. a kind of polycarbonate preparation system according to claim 3, the phenol recovery tank (5) is also connected with pre- moisture
Pipe, the pre- wet air duct are connected to the pipe between first gear pump (11) and static mixer (21) by the second booster pump (52)
On road.
5. a kind of polycarbonate preparation system according to claim 1, which is characterized in that the auxiliary agent adds mechanism and includes
Several auxiliary agent meltings tank (31) being mutually in parallel, the auxiliary agent, which melts, to be provided with below tank (31) by the thermally conductive of auxiliary agent meltingization
Medium heating machine structure.
6. a kind of polycarbonate preparation system according to claim 5, which is characterized in that auxiliary agent melting tank (31)
Y-type filter (32) are added on outlet conduit.
7. a kind of polycarbonate preparation system according to claim 6, which is characterized in that auxiliary agent melting tank (31) is equal
It is connected on static premixed device (33) by high-pressure sprayer.
8. a kind of polycarbonate preparation system according to claim 7, which is characterized in that it is described static state premixed device (33) and
Static mixer (21) is all made of SMX Plus hybrid element.
9. a kind of polycarbonate preparation system according to claim 8, which is characterized in that the static state premixed device (33) is logical
Diaphragm booster pump (34) is crossed to be connected on static mixer (21).
10. a kind of polycarbonate preparation system according to claim 1, which is characterized in that the fondant filter (22)
Disc-type filter or candle wick formula filter are selected, and its filter element selects metal establishment strainer or metal to filter felt, it is described
The filtering accuracy of filter element is 1 ~ 40 μm.
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| FI3732008T3 (en) * | 2017-12-27 | 2023-04-04 | Versalis Spa | Circuit and process for managing transients in a plant for continuous mass production of granulated expandable polymers |
| CN108948339B (en) * | 2018-06-05 | 2021-04-06 | 浙江聚碳工程技术有限公司 | Device and method for preparing aromatic polycarbonate |
| CN109603618B (en) * | 2018-12-19 | 2022-01-14 | 宁波浙铁大风化工有限公司 | Polycarbonate additive mixing and adding system and using method thereof |
| CN110577633B (en) * | 2019-09-11 | 2023-12-19 | 利华益维远化学股份有限公司 | Pretreatment system and method for polycarbonate production raw materials |
| CN110538481B (en) * | 2019-10-11 | 2021-02-02 | 中国科学院过程工程研究所 | Phenol continuous extraction system, polycarbonate resin production system comprising phenol continuous extraction system and production method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08165342A (en) * | 1994-12-14 | 1996-06-25 | Daicel Chem Ind Ltd | Method for cleaning and drying resin production apparatus |
| DE10248951A1 (en) * | 2002-10-21 | 2004-05-06 | Bayer Ag | Production of polycarbonate for use in moulded and extruded products involves a total filtration concept in which all product streams, auxiliary substances and operating substances are passed through fine filters |
| CN104395374A (en) * | 2012-05-18 | 2015-03-04 | 三菱瓦斯化学株式会社 | Method for continuously producing high-molecular-weight polycarbonate resin |
| CN204779420U (en) * | 2015-07-13 | 2015-11-18 | 宁波浙铁大风化工有限公司 | Phenol recycle device |
-
2017
- 2017-04-24 CN CN201710274273.9A patent/CN106985300B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08165342A (en) * | 1994-12-14 | 1996-06-25 | Daicel Chem Ind Ltd | Method for cleaning and drying resin production apparatus |
| DE10248951A1 (en) * | 2002-10-21 | 2004-05-06 | Bayer Ag | Production of polycarbonate for use in moulded and extruded products involves a total filtration concept in which all product streams, auxiliary substances and operating substances are passed through fine filters |
| CN104395374A (en) * | 2012-05-18 | 2015-03-04 | 三菱瓦斯化学株式会社 | Method for continuously producing high-molecular-weight polycarbonate resin |
| CN204779420U (en) * | 2015-07-13 | 2015-11-18 | 宁波浙铁大风化工有限公司 | Phenol recycle device |
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