CN102233353A - Processing method of foaming polyurethane and volume reduction processing device of foaming polyurethane - Google Patents
Processing method of foaming polyurethane and volume reduction processing device of foaming polyurethane Download PDFInfo
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- CN102233353A CN102233353A CN2011101101078A CN201110110107A CN102233353A CN 102233353 A CN102233353 A CN 102233353A CN 2011101101078 A CN2011101101078 A CN 2011101101078A CN 201110110107 A CN201110110107 A CN 201110110107A CN 102233353 A CN102233353 A CN 102233353A
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- polyurathamc
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- 238000003672 processing method Methods 0.000 title claims abstract description 17
- 238000012545 processing Methods 0.000 title claims abstract description 8
- 239000004814 polyurethane Substances 0.000 title abstract description 40
- 229920002635 polyurethane Polymers 0.000 title abstract description 40
- 238000005187 foaming Methods 0.000 title abstract 9
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 title abstract 2
- 239000003814 drug Substances 0.000 claims description 44
- 238000006243 chemical reaction Methods 0.000 claims description 31
- 238000002347 injection Methods 0.000 claims description 15
- 239000007924 injection Substances 0.000 claims description 15
- 238000007906 compression Methods 0.000 claims description 12
- 230000006835 compression Effects 0.000 claims description 11
- 230000002411 adverse Effects 0.000 claims description 7
- 238000010298 pulverizing process Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 238000007872 degassing Methods 0.000 claims description 4
- BGOFCVIGEYGEOF-UJPOAAIJSA-N helicin Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@H]1OC1=CC=CC=C1C=O BGOFCVIGEYGEOF-UJPOAAIJSA-N 0.000 claims description 4
- 230000015556 catabolic process Effects 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 15
- 238000010008 shearing Methods 0.000 abstract description 13
- 239000002699 waste material Substances 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 19
- 238000002156 mixing Methods 0.000 description 12
- 229920005989 resin Polymers 0.000 description 10
- 239000011347 resin Substances 0.000 description 10
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 8
- 238000001125 extrusion Methods 0.000 description 7
- 238000011144 upstream manufacturing Methods 0.000 description 5
- 229920001187 thermosetting polymer Polymers 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 3
- 230000006866 deterioration Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000009413 insulation Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000004927 fusion Effects 0.000 description 2
- 230000010355 oscillation Effects 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 235000011187 glycerol Nutrition 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000001141 propulsive effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000013341 scale-up Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 150000005846 sugar alcohols Polymers 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000001149 thermolysis Methods 0.000 description 1
- 229920005992 thermoplastic resin Polymers 0.000 description 1
- 230000001052 transient effect Effects 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/505—Screws
- B29C48/52—Screws with an outer diameter varying along the longitudinal axis, e.g. for obtaining different thread clearance
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J11/00—Recovery or working-up of waste materials
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- 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
- B29B17/00—Recovery of plastics or other constituents of waste material containing plastics
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
- C08J9/33—Agglomerating foam fragments, e.g. waste foam
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/505—Screws
- B29C48/52—Screws with an outer diameter varying along the longitudinal axis, e.g. for obtaining different thread clearance
- B29C48/525—Conical screws
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Polymers & Plastics (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Materials Engineering (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
- Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
Abstract
The invention provides a processing method of foaming polyurethane and a volume reduction processing device of foaming polyurethane. The processing device continuously processes wastes of foaming polyurethane in large volumes and compresses the wastes into high-density wastes. The method comprises the steps of heating the foaming polyurethane; pressurizing the foaming polyurethane by applying shearing force; compressing the foaming polyurethane. Accordingly, volume is reduced and the density of the foaming polyurethane is increased. A screw extruder is preferably used.
Description
Technical field
The processing method and the polyurathamc that the present invention relates to polyurathamc subtract the appearance treating apparatus.
Background technology
In recent years, environmental problem gets most of the attention, and the expense of offal treatment simultaneously increases year by year.For polyurathamc, the trend of regeneration reuse is surging.
The density of the discarded object of polyurathamc is low to moderate below 0.1, and volume is very big.Therefore, when landfill, subtracting the method for holding processing also is important problem.
Recirculating technique to polyurathamc also carries out various researchs, but because the raw material volume is big, and have that so the separated foam that is used to keep thermal insulation and mechanical strength are high to be difficult to destroy bubble fully and to subtract reasons such as appearance, exist the volumetric efficiency (treating capacity/device occupy volume) of device low, cost and the big problem of consumed energy.
The cyclic regeneration facture of the resin that contains polyurathamc is disclosed in patent documentation 1, the fragmentation product that will contain the resin of polyurathamc are supplied to extruder, it is contacted with treatment fluid of HTHP etc. in this extruder, polyurathamc is decomposed refinement, thereby it evenly fine is dispersed in the molten resin.
In patent documentation 2, disclose the shrink process method of polyurathamc waste wood,, made the polyurathamc waste wood softening and shrink, then made its cooling and solidify at heating lower compression polyurathamc waste wood.
The thermolysis process of thermosetting resin is disclosed in the patent documentation 3, thermosetting resins such as polyurethane are mixed with aqueous distintegrant, and use screw extruder that the paste mixture of pulverous thermosetting resin and aqueous distintegrant is supplied to thermal decomposer continuously.
[patent documentation 1] Japanese kokai publication hei 8-20023 communique
[patent documentation 2] Japanese kokai publication hei 11-138540 communique
[patent documentation 3] TOHKEMY 2007-204516 communique
Summary of the invention
The objective of the invention is to, the discarded object of bulky polyurathamc is handled continuously, with its boil down to high density.
The processing method of polyurathamc of the present invention is characterised in that to have such operation: polyurathamc is heated and applies shearing force to pressurize, compress above-mentioned polyurathamc, subtract appearance thus, the density of above-mentioned polyurathamc is increased.
According to the present invention, can handle continuously the discarded object of the polyurathamc of use in household electrical appliances, automobile, building etc., its boil down to high density.
Description of drawings
Fig. 1 is that the polyurathamc of expression embodiment subtracts the summary pie graph that holds treating apparatus.
Fig. 2 is the synoptic diagram that the polyurathamc of expression embodiment subtracts the screw rod that holds treating apparatus.
Fig. 3 is the A cutaway view of Fig. 2.
Fig. 4 is that the polyurathamc of expression comparative example subtracts the summary pie graph that holds treating apparatus.
Fig. 5 is the summary pie graph that polyurathamc that expression is assembled with reaction vessel subtracts the example of holding treating apparatus.
Fig. 6 is the summary pie graph of the variation of presentation graphs 5.
Fig. 7 is near the cutaway view in the space of the screw front end of expression single shaft extruder.
Fig. 8 is the summary cutaway view that expression is built in the space of two rollers in the roll-type mixing roll.
Fig. 9 is the summary stereogram that expression is built in two rollers in the roll-type mixing roll.
Label declaration
1 cylinder; 2 screw rods; The 2a supply unit; The 2b pressurization part; The quantitative portion of 2c; 3 polyurathamcs; 4 subtract appearance polyurethane; 5 pistons; 6 flowing path sections; 101 dispensing ports; 102 protuberances; 103 recesses; 104 reaction vessels; 105 medicament injection portions.
The specific embodiment
The processing method and the polyurathamc that the present invention relates to polyurathamc subtract the appearance treating apparatus, thereby the discarded object of the polyurathamc that uses in household electrical appliances, automobile, building etc. compressed to subtract to be held and handle.Particularly relate to based on the landfill pre-treatment or used the recycling processing method and apparatus of the decomposition reaction of medicament.
Below, the processing method of the polyurathamc that an embodiment of the invention are related to and polyurathamc subtract and hold treating apparatus and describe.
The processing method of above-mentioned polyurathamc has such operation: polyurathamc is heated to more than 130 ℃, below 350 ℃, applies 20s
-1More than, 550s
-1Following shear rate also is forced into more than the 0.2MPa, subtracts the operation (below be also referred to as to subtract hold operation) of appearance thus with the compression polyurathamc, and making the density that subtracts the polyurathamc after the appearance is 0.5g/cm
3More than.The temperature that polyurathamc is heated is the scope more than 130 ℃, below 300 ℃ more preferably, is preferably the scope more than 130 ℃, below 200 ℃ especially.
In this manual, for example " more than 130 ℃ " are that 130 ℃ are included in the scope, and " below 300 ℃ " are that 300 ℃ are included in the scope." scopes more than 130 ℃, below 300 ℃ " are meant and are in more than 130 ℃ and are in scope below 300 ℃, be to comprise 130 ℃ and 300 ℃, and comprise the value between 130 ℃ and 300 ℃.And " less than 130 ℃ " are not comprise 130 ℃ in scope.
Under to the situation of polyurathamc applied pressure less than 0.2MPa, therefore fully effect of the frictional force between the metal of the internal face of polyurethane and formation cylinder, puts on the shearing force deficiency of polyurathamc.And from the withstand voltage properties aspect of common extruder, the pressure that puts on polyurathamc is preferably below the 50MPa.
When shearing force less than 20s
-1Situation under, can't fully stave bubble.
In the processing method of above-mentioned polyurathamc, preferably use screw extruder.
The polyurathamc of being supplied with is preferably under reduced pressure pulverized the degassing and is handled.
In the processing method of above-mentioned polyurathamc, also have and inject medicament, polyurathamc is carried out the operation of chemical breakdown, utilize power in the compression of polyurathamc to prevent the adverse current of medicament, continuously polyurathamc is supplied with.
By the operation with the medicament reaction is set, thereby promotes the decomposition of polyurethane and can easily remove bubble.
Above-mentioned polyurathamc subtracts the appearance treating apparatus and comprises: the extruder with dispensing port of polyurathamc; With the reaction vessel that is used to make polyurathamc and medicament reaction, and has the medicament injection portion of medicament being injected the polyurathamc that compresses by extruder.
To hold operation be not in the inside of extruder but under the situation of carrying out in the roll-type mixing roll subtracting, be provided with in the place ahead (upstream side) of the supply unit of extruder and subtract the appearance operation, medicament injection portion can be arranged at the back segment part of quantitative portion, the leading section of cylinder and the connecting portion or the reaction vessel of reaction vessel.In this case, the polyurathamc after will subtracting appearance in the roll-type mixing roll is supplied to the dispensing port of extruder.
Subtract in the appearance treating apparatus at above-mentioned polyurathamc, extruder preferably possesses the screw extruder of screw rod, and this screw rod has spiral helicine protuberance and recess.
Subtract in the appearance treating apparatus at above-mentioned polyurathamc, extruder is the single shaft extruder preferably.
Subtract in the appearance treating apparatus at above-mentioned polyurathamc, screw extruder preferably includes: the supply unit that does not have tapered portion at screw rod; The pressurization part that has tapered portion at screw rod; With the quantitative portion that does not have tapered portion at screw rod.
Medicament injection portion is being located under the situation of extruder, preferably is being located at the back segment part (downstream) of quantitative portion.
That is, subtract at above-mentioned polyurathamc and to hold in the treating apparatus, medicament injects the leading section of cylinder of back segment part that the quality award from the ministry choosing is arranged at quantitative portion, screw extruder and the connecting portion or the reaction vessel of reaction vessel.
Here, quantitatively the back segment of portion part (downstream) is meant, than the central point of the line segment of the end, upstream of the quantitative portion of the central axis direction that links cylinder and the downstream end part by the downstream.Therefore, medicament injection portion also can be arranged at the side surface part of the cylinder on the face of the orthogonality of center shaft of this central spot and cylinder.
Subtract at above-mentioned polyurathamc and to hold in the treating apparatus, preferably connect at dispensing port and pulverize degassing treating apparatus, this pulverizings treating apparatus that outgases is used to carry out such processing: under reduced pressure the polyurathamc that is supplied to extruder is pulverized and outgased.
Subtract in the appearance treating apparatus at above-mentioned polyurathamc, screw extruder is the single shaft extruder, the shape of screw rod is preferably, the flow path cross sectional area A of supply unit is that flow path cross sectional area is more than 4 than A/B with the ratio of the flow path cross sectional area B of quantitative portion, and in the cylinder with the length L of the corresponding part of pressurization part and pressurization part in the ratio L/D of inside diameter D of cylinder be more than 10.
Polyurathamc is used for padded coaming that heat-barrier material that household electrical appliances use and automobile use etc., and density is below 0.2.
Under reduced pressure polyurathamc being pulverized the method for handling that outgases in advance is to get final product as the general method that adopts of landfill pre-treatment at present.
Be preferably the compound that in glycol, polyalcohol, glycerine equimolecular, has plural hydroxyl with the medicament of polyurathamc reaction.
Preferred pressure is different because of the chemical reaction that is utilized for polyurathamc is reacted with medicament, but because used medicament is stayed in the reaction unit, so need be the pressure more than the vapour pressure of medicament.Need be the pressure more than the vapour pressure at least in the part (sealing) of reaction unit.
As promoting and the condition of the chemical reaction of medicament, enumerate temperature and pressure, but for this condition, use small-sized autoclave etc. to study in advance, can determine the continuous operating condition of device thus.
Usually, the single shaft extruder is about 1/10 a price of the two-axis extruder of same size, is the equipment more cheap than two-axis extruder, and simple structure, therefore, has advantage at the aspects such as the limit of resistance to pressure and torque.
Fig. 1 is that the polyurathamc of expression embodiment subtracts the summary pie graph that holds treating apparatus.
And Fig. 2 is the synoptic diagram that the polyurathamc of expression embodiment subtracts the screw rod that holds treating apparatus.
It is the single shaft extruder that polyurathamc shown in Figure 1 subtracts the appearance treating apparatus.
This single shaft extruder possesses cylinder 1, is inserted in the screw rod 2 of cylinder 1 and the dispensing port 101 of supplying with polyurathamc 3.Screw rod 2 has spiral helicine protuberance 102 and recess 103.The inside of cylinder 1 is divided into the part that is called supply unit 2a, pressurization part 2b and the quantitative 2c of portion.The screw rod 2 that is positioned at the zone corresponding with supply unit 2a and the quantitative 2c of portion does not have tapered portion.On the other hand, has tapered portion at the screw rod 2 that is positioned at the zone corresponding with pressurization part 2b.
The polyurathamc of supplying with from dispensing port 101 3 is admitted to pressurization part 2b from supply unit 2a.In pressurization part 2b, at the recess 103 of screw rod 2 tapered portion is set, follow the rotation of screw rod 2, polyurathamc 3 is pressed into the little zone of volume by protuberance 102 and is pressurized.And then the leading section that subtracts the cylinder 1 that holds polyurethane 4 right side from figure in the quantitative 2c of portion after the adjustment density is discharged from.
Fig. 3 is the A cutaway view of Fig. 2.
In the figure, flowing path section 6 illustrates the cross section in the gap that the internal face by the protuberance 102 of supply unit 2a and recess 103 and cylinder 1 forms.Polyurathamc 3 flows through this flowing path section 6.Here, show the flowing path section 6 of the supply unit 2a with tapered portion, but also be formed with same gap at pressurization part 2b with tapered portion and the quantitative 2c of portion that do not have a tapered portion.Thus, pressurization part 2b and the quantitative 2c of portion also have flowing path section 6 equally with supply unit 2a.
Here, about the area of flowing path section 6, be flow path cross sectional area, get supply unit 2a and the quantitative ratio of the 2c of portion, this is compared R than being defined as flow path cross sectional area.The following record of mathematical expression.
R=(flow path cross sectional area of supply unit 2a)/(the quantitatively flow path cross sectional area of the 2c of portion)
Usually, two-axis extruder using more than 300 rev/mins, under this condition, applies high shearing force mostly, and therefore, resin might deterioration.
On the other hand, under the situation of using the single shaft extruder, the problem points that exists material to slide easily.
In order to solve the problem that polyurathamc slides easily in compression process, preferably use the screw rod shape.Thus, do not compress polyurathamc hastily, compress lentamente, thus, suppress polyurathamc and slide while apply shearing force, can be with the ratio press-resin higher than the extruder of common thermoplastic resin.
And the length of establishing in the cylinder 1 with the corresponding part of pressurization part 2b is L, and the internal diameter of establishing the cylinder 1 among the pressurization part 2b is D, and the rate of change of R is defined as under the situation of R/ (L/D), produce when the rate of change of R too high, the problem of pressure transient then.Therefore, the rate of change of R is preferably more than 0.4, below 2.0.And R is preferably more than 4, below 20.
In addition, if the length L a of supply unit 2a is too short, the supply instability of polyurathamc then.Therefore, more than the preferred La/D=5.
About density, sample is put into 81cm
3Cylindrical vessel in, measure the quality W (g (gram)) of this sample, with W/81 (g/cm
3) as density.
Using the speed and the gap between screw rod outermost perimembranous and the cylinder of screw rod outermost perimembranous is that the shearing force that is applied by extruder is calculated in the space.That is, establishing the space is t (mm), and the relative moving speed of establishing screw rod outermost perimembranous is v (mm/s), and then shear rate is defined as v/t (s
-1).
For example under the situation of extruder, the material between cylinder surface and screw surface is applied shearing force.At this moment, have only screw rod with respect to fixing cylinder surface activity, therefore, relative moving speed v represents with the diameter * rotary speed of the tooth portion (protuberance) of π * screw rod.
The on-stream rotation speed change that also makes thus, can at random make shear rate change, and makes the operating condition optimization thereby can feed back the information of product.
Here, the space t to the single shaft extruder describes.
Fig. 7 shows near the cutaway view of the central axis direction of the cylinder the quantitative 2c of portion that is positioned at the single shaft extruder.
In the figure, be the state that screw rod 202 is in the inside that is inserted in cylinder 201.
Be provided with spiral helicine protuberance 203 at screw rod 202.
The space t of single shaft extruder shown in this Fig is the gap (distance) between the peripheral part of the internal face of cylinder 201 and protuberance 203.
Fig. 8 shows the cross section of two rollers that are built in the roll-type mixing roll, and shows its space t.
In the figure, the gap (distance) between two rollers 302 is space t.
[embodiment 1]
Polyurathamc uses thermosetting resin, therefore, and not fusion fully.But, can utilize the propulsive force of screw rod to pressurize and it is pushed.
In the extruder, the inside diameter D of cylinder is 20mm, and the length of establishing cylinder integral body is Lc, uses the extruder of Lc/D=25.And then making the temperature cylinder of supply unit is 150 ℃, and making the temperature cylinder of pressurization part is 160 ℃, and the temperature cylinder that makes quantitative portion is 170 ℃ and pushes.Quantitatively the pressure of portion is that 4MPa, maximum are in the scope of 5MPa in minimum of a value, changes in extrusion process.Because the stability of the pressure during compression significantly changes because of the temperature of the cylinder of quantitative portion, therefore, quantitatively the temperature of the cylinder of portion is preferably the scope more than 130 ℃, below 200 ℃.Less than 130 ℃ the time, the insufficient fusion of polyurathamc can't be pushed.Bubble can be fully not broken yet.On the other hand, when the high temperature that surpasses 200 ℃, polyurathamc slides easily.
On the other hand, in the part of the mould of the leading section that is positioned at extruder, make to subtract and hold polyurethane and slide and discharge swimmingly, therefore, the temperature of the part of mould is preferably more than 180 ℃.In the present embodiment, the temperature of mould is 200 ℃.
After in the hopper (dispensing port) of supply unit, use pulverizing the polyurathamc of heat insulation usefulness, screen and passed through the polyurathamc behind the sieve with the mesh of 5mm.Use in scale-up mode under the situation of more large-scale extruder, can increase the pulverizing size.
And the rotary speed of screw rod is 21rpm, and the space is 1mm.When being scaled screw rod and putting on the shear rate of polyurathamc, be 20s
-1
The rotary speed of screw rod is preferably the scope that 20rpm is above, 200rpm is following.This when being scaled screw rod and putting on the shear rate of polyurathamc, is in 19s under the situation of D=20mm, t=1mm
-1More than, 188s
-1Following scope.
And extruder is supplied with polyurathamc to hopper and is used feed appliance, supplies with polyurathamc to hopper quantitatively.And, agitator is installed in feed appliance is stirred, prevent the powder cross-over connection of polyurathamc and make supply to the extruder unsettled situation that becomes.
In addition, the amount of the polyurathamc of supplying with from feed appliance is supplied with in following scope: the scope more than 50% that does not cover the surface of the screw rod that rotates in the hopper the supply unit of extruder.This be because, the polyurathamc powder is very easy to cross-over connection, is covering under the situation 50% or more of screw surface, the polyurathamc powder is to the supply instability of extruder, the amount of resin of being extruded by extruder produces deviation, the instability thereby processing becomes.
In addition, the screw rod shape of extruder is used following shape: flow path cross sectional area is 4 than R, and the length of establishing the part with tapered portion (pressurization part) that sectional area changes is L, and when the internal diameter of the cylinder of extruder was D, L/D was 10.
Obtain density according to subtract shape (volume) and the weight of holding polyurethane that extruding obtains, estimate the effect that compression subtracts appearance in quantitative mode.
Its result, the product density of the polyurethane that obtains is 0.55g/cm
3
[embodiment 2]
Quantitatively the temperature of the cylinder of portion is 250 ℃, and the rotary speed of screw rod is 70rpm, and shear rate is 66s
-1, other condition is identical with embodiment 1.
Its result, the product density of the polyurethane that obtains is 0.54g/cm
3
[embodiment 3]
As the polyurathamc of supplying with to the hopper of extruder, use the polyurethane of behind the polyurathamc of pulverizing heat insulation usefulness, under vacuum decompression, having removed the gas of thermophore and having obtained.The rotary speed of screw rod is 70rpm, and shear rate is 66s
-1, other condition is identical with embodiment 1.
Its result, the product density of the polyurethane that obtains is 1.02g/cm
3
[embodiment 4]
Leading section at extruder is installed reaction unit, and making the temperature in the reaction vessel is 250 ℃, injects ethylene glycol as medicament in reaction vessel, thus, confirms that whether medicament is to supply unit side adverse current.The rotary speed of screw rod is 70rpm, and shear rate is 66s
-1, other condition is identical with embodiment 1.
Its result, the product density of the polyurethane that obtains is 1g/cm
3
Fig. 5 illustrates combination extruder and reaction unit and the polyurathamc that obtains subtracts the summary pie graph that holds treating apparatus.
Identical for extruder with the structure of Fig. 1, be connected with reaction vessel 104 at the leading section of cylinder 1.Upstream side at reaction vessel 104 is provided with medicament injection portion 105.Thus, the polyurethane that subtracts in extruder after the appearance is further subtracted appearance.
In addition, though not shown, medicament preferably pressurizes by the medicament injection pump from chemical tank, and injects via medicament injection portion 105.This is in order to prevent that medicament is to the chemical tank adverse current.
Fig. 6 shows the variation of Fig. 5.
In the figure, medicament injection portion 105 is located at the back segment part of the quantitative 2c of portion of cylinder 1.According to this structure, can mechanically carry out mixing by screw rod 2 to polyurethane and medicament.
In the present embodiment, the injected volume of polyurathamc is 1: 1 with the ratio of medicament injection rate.In this case, in cylinder 1, find no medicament in the upstream of supply unit and adhere to etc., medicament is not to the supply side adverse current of polyurethane as can be known.
The medicament injection rate can be lacked than the injected volume of polyurathamc.
In the present embodiment, the back segment of the quantitative 2c of portion that shows at the upstream side of reaction vessel 104 or cylinder 1 partly is provided with the example of medicament injection portion 105, but be not limited thereto, also can medicament injection portion 105 be set at the leading section of cylinder 1 and the connecting portion of reaction vessel 104.By utilizing the compression section of extruder, thereby condition of high voltage can both be kept in the inside of the inside of cylinder 1 and reaction vessel 104, therefore, can promote the reaction of polyurethane and medicament.
[embodiment 5]
The situation of using the roll-type mixing roll is shown.
Fig. 9 shows two rollers that are built in the roll-type mixing roll.
In the figure, between two rollers 302 from above supply with polyurathamc 401 and carry out mixing, thereby obtaining subtracting holds polyurethane 402.Repeatedly carry out above-mentioned steps repeatedly.By making the rotary speed difference of two rollers 302, thus can be to applying shearing force by the polyurathamc 401 between two rollers 302.
Repeated multiple times carries out supplying with polyurathamc and heating, applying the operation of shearing force then to the roll-type mixing roll, accumulation carry out two minutes mixing.
Roller is of a size of 6 inches, and roller rotary speed separately in front and back is 22rpm, 18rpm, and space t is 1.5mm.The shear rate that this condition is equivalent to that polyurathamc is applied is 21s
-1Situation.The surface temperature of roller is 190 ℃.Pressure between roller is 3MPa.
Shape (volume) and weight according to the article shaped of the sheet that obtains are obtained density.Its result, the product density of the polyurethane that obtains is 0.51g/cm
3
[embodiment 6]
The screw rod shape of extruder is used following shape: flow path cross sectional area is 4 than R, and the L/D of the part with tapered portion of sectional area variation is 1.5.The rotary speed of screw rod is 70rpm, and shear rate is 66s
-1Other condition is identical with embodiment 1.
Its result, quantitatively the pressure of portion is that 0.3MPa, maximum are in the scope of 5MPa in minimum of a value, changes in extrusion process, compares with embodiment 1, pressure oscillation becomes about 4MPa, instability.The product density of resulting polyurethane is 0.52g/cm
3
[embodiment 7]
The temperature of compression unit and quantitative portion all is 200 ℃.Other condition is identical with embodiment 6.
Its result, quantitatively the pressure of portion is that 0.2MPa, maximum are in the scope of 5MPa in minimum of a value, changes in extrusion process, compares with embodiment 1, pressure oscillation becomes about 4MPa, instability.The product density of resulting polyurethane is 0.52g/cm
3
In the above-described embodiments, use the extruder of the diameter of cylinder, but, can use the large-scale extruder that about 80mm is above, 150mm is following in order fully to guarantee treating capacity as 20mm.And,, be 500s preferably in shear rate for fear of the secondary product that the deterioration that generates the polymer that causes because of shearing produces
-1Carry out under the following operating condition.
[embodiment 8]
Extruder use cylinder bore diameter D as 50mm, R be 6, L/D is 10 extruder, shear rate is 176s
-1Other condition is identical with embodiment 6.
Its result, quantitatively the pressure of portion is that 5MPa, maximum are in the scope of 6MPa in minimum of a value, changes in extrusion process.
The product density of resulting polyurethane is 0.60g/cm
3
[embodiment 9]
Extruder use cylinder bore diameter D as 152mm, R be 10, L/D is 10 extruder, shear rate is 550s
-1Other condition is identical with embodiment 6.
Its result, quantitatively the pressure of portion is that 6MPa, maximum are in the scope of 7MPa in minimum of a value, changes in extrusion process.
The product density of resulting polyurethane is 0.62g/cm
3
[embodiment 10]
Extruder use cylinder bore diameter D as 152mm, R be 20, L/D is 10 extruder, shear rate is 550s
-1Other condition is identical with embodiment 6.
Its result, quantitatively the pressure of portion is that 6MPa, maximum are in the scope of 8MPa in minimum of a value, changes in extrusion process.
The product density of resulting polyurethane is 0.65g/cm
3
Table 1 gathers the data of embodiment 1～10 and represents.
[table 1]
(comparative example 1)
The temperature cylinder that makes the quantitative portion of extruder is 120 ℃ and experimentizes.Other condition is identical with embodiment 2.
Its result, the product density of resulting polyurethane is 0.21g/cm
3
(comparative example 2)
The temperature cylinder that makes the quantitative portion of extruder is 400 ℃ and experimentizes.Other condition is identical with embodiment 2.
Its result, the product density of resulting polyurethane is 0.56g/cm
3But product can produce sintering etc. and variable color, and apparent viscosity reduces.Think that molecular weight reduces because of thermal decomposition.Usually, be since when temperature be more than 400 ℃ the time, the C-C chemical bonds that the skeleton of polymer is contained etc. also decompose, deterioration develops.
(comparative example 3)
Use piston compressor shown in Figure 4, do not apply shearing force, making temperature in the cylinder is that pressure in 170 ℃, cylinder is that 5MPa compresses.
In the figure, put into polyurathamc 3, by the piston 5 compression polyurathamcs 3 that insert cylinder 1 in the inside of cylinder 1.
Its result, the product density of resulting polyurethane is 0.35g/cm
3
(comparative example 4)
Leading section at extruder is installed reaction unit, and making the temperature cylinder of the quantitative portion of extruder is 120 ℃, and making the temperature in the reaction vessel is 250 ℃.In reaction vessel, inject under the situation of ethylene glycol as medicament, confirm that whether medicament is to supply unit side adverse current.Other condition is identical with embodiment 4.
Its result, medicament is to the supply side adverse current.
Its reason is as follows.
The temperature of extruder is low, and polyurethane is not softening.Therefore, can't compress polyurethane, between the particle of the polyurethane of the cylinder interior that is positioned at extruder, produce the gap.Medicament spills from this gap.
(comparative example 5)
Repeated multiple times carries out supplying with polyurathamc and heating, applying the operation of shearing force then to roller, accumulation carry out two minutes mixing.Roller is of a size of 6 inches, and roller rotary speed separately in front and back is 22rpm, 18rpm, and space t is 10mm.Under this condition, the shear rate that polyurathamc is applied is equivalent to 3.2s
-1The surface temperature of roller is 190 ℃.Pressure between roller is 1MPa.
Shape (volume) and weight according to the article shaped of resulting sheet are obtained density.
Its result, the density of resulting polyurethane product are 0.21g/cm
3
(comparative example 6)
Extruder use cylinder bore diameter D as 55mm, R be 4, L/D is 10 two-axis extruder.The rotary speed of screw rod is 300rpm, and space t is 1mm, and shear rate is 832s
-1, quantitatively the temperature of the cylinder of portion is set at 170 ℃.Quantitatively the pressure of portion is that 4MPa, maximum are in the scope of 5MPa in minimum of a value, changes in extrusion process.
Its result, the product density of resulting polyurethane is 0.4g/cm
3And, produce sintering, also produce gas.
Table 2 gathers the data of comparative example 1～6 and represents.
[table 2]
According to the present invention, can handle continuously the discarded object of the polyurathamc of use in household electrical appliances, automobile, building etc., its boil down to high density.
And, according to the present invention, can provide based on the landfill pre-treatment or the supply of the polyurathamc when making the recycling processing of decomposition reaction of with medicament in effective means.
Claims (11)
1. the processing method of a polyurathamc is characterized in that,
This processing method has such operation: polyurathamc is heated to more than 130 ℃, below 350 ℃, applies 20s
-1More than, 550s
-1Following shear rate also is forced into more than the 0.2MPa, and compress above-mentioned polyurathamc and subtract appearance thus,
Making the density that subtracts the above-mentioned polyurathamc after the appearance is 0.5g/cm
3More than.
2. the processing method of polyurathamc according to claim 1 is characterized in that,
Use screw extruder to carry out the compression of above-mentioned polyurathamc.
3. the processing method of polyurathamc according to claim 1 and 2 is characterized in that,
Under reduced pressure the above-mentioned polyurathamc of being supplied with being pulverized the degassing handles.
4. according to the processing method of each the described polyurathamc in the claim 1 to 3, it is characterized in that,
This processing method also has such operation: injects medicament to above-mentioned polyurathamc, above-mentioned polyurathamc carried out chemical breakdown,
Utilize power in the above-mentioned compression to prevent the adverse current of above-mentioned medicament, supply with above-mentioned polyurathamc continuously.
5. a polyurathamc subtracts the appearance treating apparatus, it is characterized in that,
This polyurathamc subtracts the appearance treating apparatus and comprises: the extruder with dispensing port of polyurathamc; With the reaction vessel that is used to make above-mentioned polyurathamc and medicament reaction,
And have above-mentioned medicament is injected medicament injection portion by the above-mentioned polyurathamc after the above-mentioned extruder compression.
6. polyurathamc according to claim 5 subtracts the appearance treating apparatus, it is characterized in that,
Above-mentioned extruder is the screw extruder that possesses screw rod, and this screw rod has spiral helicine protuberance and recess.
7. subtract the appearance treating apparatus according to claim 5 or 6 described polyurathamcs, it is characterized in that,
Above-mentioned extruder is the single shaft extruder.
8. subtract the appearance treating apparatus according to claim 6 or 7 described polyurathamcs, it is characterized in that,
Above-mentioned screw extruder comprises: the supply unit that does not have tapered portion at above-mentioned screw rod; The pressurization part that has tapered portion at above-mentioned screw rod; And the quantitative portion that does not have tapered portion at above-mentioned screw rod.
9. polyurathamc according to claim 8 subtracts the appearance treating apparatus, it is characterized in that,
Above-mentioned medicament injection portion is arranged at leading section and the connecting portion between the above-mentioned reaction vessel or the above-mentioned reaction vessel of the above-mentioned cylinder of the back segment part of above-mentioned quantitative portion, above-mentioned screw extruder.
10. subtract the appearance treating apparatus according to each the described polyurathamc in the claim 5 to 9, it is characterized in that,
Be connected with at above-mentioned dispensing port and pulverize degassing treating apparatus, this pulverizings treating apparatus that outgases is used to carry out such processing: under reduced pressure the above-mentioned polyurathamc that is supplied to above-mentioned extruder is pulverized and outgased.
11. subtract the appearance treating apparatus according to each the described polyurathamc in the claim 6 to 10, it is characterized in that,
Above-mentioned screw extruder is the single shaft extruder, being shaped as of above-mentioned screw rod: the flow path cross sectional area A of above-mentioned supply unit is that flow path cross sectional area is more than 4 than A/B with the ratio of the flow path cross sectional area B of above-mentioned quantitative portion, and in the above-mentioned cylinder with the length L of the corresponding part of above-mentioned pressurization part and above-mentioned pressurization part in the ratio L/D of inside diameter D of above-mentioned cylinder be more than 10.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2010-104900 | 2010-04-30 | ||
| JP2010104900A JP5553343B2 (en) | 2010-04-30 | 2010-04-30 | Method for treating foamed polyurethane and volumetric treatment equipment for foamed polyurethane |
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| CN102233353A true CN102233353A (en) | 2011-11-09 |
| CN102233353B CN102233353B (en) | 2014-04-02 |
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| JP (1) | JP5553343B2 (en) |
| KR (1) | KR101339128B1 (en) |
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| CN111497054A (en) * | 2020-05-07 | 2020-08-07 | 安徽森泰木塑集团股份有限公司 | Production method of polyurethane foam powder solid waste particles |
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| JP7420357B1 (en) | 2023-07-14 | 2024-01-23 | 株式会社アーケム | How to recycle polyurethane foam |
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| JP2004143464A (en) * | 2003-12-12 | 2004-05-20 | Toshiba Corp | Apparatus for decomposing foamed resin and method for decomposing foamed resin |
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- 2010-04-30 JP JP2010104900A patent/JP5553343B2/en not_active Expired - Fee Related
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| JPH05285970A (en) * | 1992-04-08 | 1993-11-02 | Asahi Glass Co Ltd | Manufacture of polyurethane moldings |
| JPH1192590A (en) * | 1997-09-18 | 1999-04-06 | Toshiba Corp | Disposal method or disposal device of waste containing expandable plastic |
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| JP2011230458A (en) | 2011-11-17 |
| KR101339128B1 (en) | 2013-12-09 |
| KR20110121562A (en) | 2011-11-07 |
| CN102233353B (en) | 2014-04-02 |
| JP5553343B2 (en) | 2014-07-16 |
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