CN106132653A - The method that converting-plastics is become wax - Google Patents
The method that converting-plastics is become wax Download PDFInfo
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- CN106132653A CN106132653A CN201580011050.2A CN201580011050A CN106132653A CN 106132653 A CN106132653 A CN 106132653A CN 201580011050 A CN201580011050 A CN 201580011050A CN 106132653 A CN106132653 A CN 106132653A
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- waste plastic
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
-
- 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
- C08J11/04—Recovery or working-up of waste materials of polymers
- C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
- C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/08—Halides
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Wood Science & Technology (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Sustainable Development (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The method that present invention provide for converting-plastics becomes wax.In one embodiment, include being introduced in chamber waste plastic for waste plastic changes into the method for wax, and hydrogen is added to described chamber.Described method includes fully heating waste plastic and hydrogen so that described waste plastic thermal depolymerization, thus forms the wax product comprising alkane and olefin(e) compound.
Description
Technical field
Technical field relates generally to the method forming wax, and more specifically it relates to is used for processing plastics to incite somebody to action
Described converting-plastics becomes the method for wax.
Background technology
Wax is broadly divided into several groups clearly established, including paraffin (generally by oil lubrication distillation obtain),
Microwax (generally being obtained by remaining lubricating oil fraction) and Tissuemat E are (typically by low-molecular-weight, high-density raw material
Prepare).Have been found that the wax of these types each has special physical property so that they are lattice for specific application
The most attractive.Such as, Tissuemat E be often used for the formula of plastic colorant, PVC STABILIZERS/LUBRICANTS, binding agent, with
And to reduce friction in ink.Tissuemat E is also act as releasing agent or slipping agent.
Tissuemat E compositions comprises various polyethylene.In most of the cases, the polyethylene used in Tissuemat E
Weight average molecular weight range is about 1500 grams every mole (g/mol) to about 20,000g/mol.High-grade Tissuemat E can pass through second
The controllable polymerization of alkene obtains, thus obtains destination properties, such as molecular weight, fusing point, viscosity and hardness.Recently, lower grade
The use of Tissuemat E occurs in that growth, described lower grade Tissuemat E are typically derived from the thermal decomposition of polyvinyl resin.This
The use in product quality application on the back burner for cost or occasion of the product of class lower grade is
Become universal.But, the Tissuemat E derived from the thermal decomposition of polyvinyl resin is the most with low quality, and such as, they show
Undesirable color, low-molecular-weight and whole production batch are inconsistent.
Accordingly, it is desired to provide a kind of method of low cost, improve the Tissuemat E of character in order to manufacture to have.It addition, the phase
Hope and a kind of method that waste plastic changes into the wax with destination properties is provided.Additionally, other desired features and characteristics will
According to detailed description below and appended claim, become in conjunction with accompanying drawing and technical field above and background technology
Substantially.
Summary of the invention
The method that present invention provide for converting-plastics becomes wax.In an exemplary embodiment, for giving up
Abandon converting-plastics to become the method for wax to include waste plastic to be introduced in chamber, and hydrogen is added to described chamber.Described
Method includes fully heating waste plastic and hydrogen so that described waste plastic thermal depolymerization, thus is formed and comprise alkane and alkene
The wax product of compound.
In another embodiment, for becoming the method for wax to include making plastics contact with hydrogen converting-plastics.It addition,
Described method includes abundant heating of plastic and hydrogen so that described plastic hot is degraded, thus forms Saybolt color (ASTM D156)
It is at least about the wax product of 0.
In another embodiment, it is provided that a kind of method for waste plastic being changed into Tissuemat E.Described
Method includes making waste plastic melt.Hydrogen is dissolved in described waste plastic.Waste plastic is pyrolyzed in the presence of hydrogen gas
Poly-to form the Tissuemat E product comprising alkane and olefin(e) compound.
Accompanying drawing is sketched
The embodiment of method for converting-plastics becomes wax, Qi Zhongxiang are described hereinafter in connection with the following drawings
With reference represent identical element, and wherein:
An exemplary herein according to Fig. 1, for becoming the schematic diagram of the method for wax by converting-plastics；
An alternate embodiment herein according to Fig. 2, for becoming the schematic diagram of the method for wax by converting-plastics；And
And
Another alternate embodiment herein according to Fig. 3, for becoming the schematic diagram of the method for wax by converting-plastics.
Detailed Description Of The Invention
Detailed description below is merely exemplary in nature, and is not intended to limit for converting-plastics is become wax
Method.Additionally, be not intended by any theory proposed in background above or detailed description below
Constraint.
Present invention provide for processing plastics with the method that converting-plastics becomes wax.As used in this article, " mould
Material " refer to TPO.TPO includes polyethylene, such as, have formula (C2H4)nH2Polyethylene, wherein n lead to
It is often 50 to 100, and polypropylene, such as there is formula (C3H6)mH2Polypropylene, wherein m is usually 50 to 100, or thermoplasticity
Polyolefinic mixture.Method disclosed herein can improve the control of the character of the reaction to plastics and gained wax product
System.In an exemplary embodiment, charging plastics are Low Density Polyethylene (LDPE) plastic refuse.Such as, charging is moulded
Material can be polyethylene film or the Polythene Bag of process recycling after recirculation or industry after consumption.
The method provided in this article utilizes thermal degradation to make the long chain units of charging plastics rupture, thus forms alkene and chain
Alkane.More particularly, the illustrative methods provided in this article makes charging plastic hot depolymerization to form alkene and alkane.Plastics
Heat treatment carry out in controllable hydrogen environment.Its theory is, the further reaction of hydrogen environment suppression gained alkene, and prevents
Only alkene forms the compound showing non-white and other non-targeted character.As a result, the product obtained can have close to white
The color of color.Test material association of the U.S. (ASTM) recommends the Saybolt color method according to ASTM D156 and measures oil product
Thing connects the test of subalbous color.Described Saybolt color method provides the experience definition of transparent petroleum liquid color, its base
In scale be-16 (the darkest) to+30 (the brightest).By finding out when observing through column length, vision matching is carried by ASTM D156
The post height of the sample of the optical filter standard of confession derives numerical value.In order to test, make wax sample melt to higher than its condensation point 8 DEG C-
17 DEG C, and poured into suitable tintometer post.As described herein, exemplary products wax close to water white,
And its Saybolt color (ASTMD156) is about+25 to about+30, e.g., from about+28 to about+30, e.g., from about+30.An example
Property embodiment in, the Saybolt color (ASTMD156) of product wax be at least about 0, the most about+5, the most about+10.
The Saybolt color (ASTMD156) of a kind of exemplary products is at least about+15, the most about+18, e.g., from about+20.
Fig. 1 is simplification of flowsheet figure, which illustrates, by thermal degradation in the hydrogen gas atmosphere, converting-plastics is become wax
One embodiment of method.This process chart is simplified, does not wherein show that and usually there will be in such technique
Mechanical device part, including pump, pressure, temperature and flow monitoring and control system.
In FIG, plastic raw materials 12 is changed into wax product 14, such as Tissuemat E by plastic processing device 10.As above institute
Stating, plastic raw materials 12 can be formed by waste plastic, for example originating from the film of process recycling after recirculation after consumption or industry
Or bag.The plastics forming raw material 12 can be limited to the plastics of single type, such as polyethylene or polypropylene, or can include moulding
The mixture of material compound, such as polyethylene and polypropylene.
As shown, plastic raw materials 12 and purging gas 18 are fed to reaction zone 20.Purging gas 18 includes inertia
Gas or multiple gases.In an exemplary embodiment, purging gas 18 is the purest hydrogen.Other embodiment party
In case, purging gas 18 is the mixture of hydrogen and noble gas.Such as, purging gas 18 can be the mixing of hydrogen and nitrogen
Thing, such as, hydrogen partial pressure is at least about 0.5 atmospheric pressure (atm), the mixture of the most about 0.8atm, e.g., from about 1atm.
Purging gas 18 can before plastic raw materials 12 is introduced to reaction zone, afterwards or simultaneously be introduced to reaction
District 20.Do not consider plastic raw materials 12 and purging gas 18 are fed the order to reaction zone 20, when by purging gas 18 from instead
Answer and district 20 removes surrounding air and when making plastic raw materials 12 receive in reaction zone 20, it is believed that plastic raw materials 12 is introduced into instead
Answer the hydrogen environment in district 20.After plastic raw materials 12 is introduced to hydrogen environment, described technique can continue to make plastics former
Material 12 melts.
As shown in FIG. 1, reaction zone 20 is equipped with heater 24.In an exemplary embodiment, heater 24
Through controlling to run under low pretreatment temperature, so that plastic raw materials 12 melts.Such as, heater 24 can be by reaction zone 20
It is heated to about 100 DEG C to about 150 DEG C, the temperature of e.g., from about 135 DEG C.Low pretreatment temperature can be remained selected by heater 24
Persistent period, e.g., from about 1 minute to about 90 minute.After making plastic raw materials 12 melted, heater 24 is through controlling to react at height
At a temperature of run so that the cracking of molten plastic raw materials 12 thermal degradation, i.e. plastic raw materials 12 (include thermal depolymerization and its
Its cracking process).Such as, the reaction zone 20 including plastic raw materials 12 and hydrogen purge gas 18 can be heated to by heater 24
About 300 DEG C to about 500 DEG C, the high reaction temperature of e.g., from about 405 DEG C.High reaction temperature can be maintained and be sufficient so that by heater 24
The persistent period of essentially all of plastic raw materials 12 thermal degradation.As used in this article, term " essentially all of plastics
Raw material " refer to the plastic raw materials 12 of at least about 95 percentage by weights (wt%).In an exemplary embodiment, heater 24
High reaction temperature is maintained about 1 minute to about 45 minutes, the persistent period of such as 30 minutes.An exemplary
In, plastic raw materials 12 experiences thermal depolymerization (one of thermal degradation process), rather than random scission or side base eliminate.Plastic raw materials 12
Oxidation is impossible, because all of oxygen is all removed from reaction zone by purging gas 18.
In order to make the thermal degradation of essentially all of plastic raw materials 12, hydrogen purge gas 18 is mixed and to make it dissolve in the most molten
In the plastic raw materials 12 melted.Therefore, can be furnished with agitator 28 molten to promote hydrogen purge gas 18 to dissolve in reaction zone 20
Plastic raw materials 12 in.For batch technology, Exemplary mixers 28 can include blender (blender) or other mix
Close mechanism, in order to stir and to mix molten plastic raw materials 12 and hydrogen purge gas 18.For flow type (flow
Through), for continuous processing, Exemplary mixers 28 includes static mixer 28, molten plastic raw materials 12 and hydrogen
The mixture of purging gas 18 is extruded by it.
Reaction zone 20 is heated to time that high reaction temperature persistently selectes so that essentially all of plastic raw materials 12
Thermal degradation also forms wax product 14.A kind of exemplary wax product comprises alkane and olefin(e) compound, and can be only by alkane
Hydrocarbon and alkene composition.Stoichiometric depolymerization cracking reaction generally forms alkane and alkene with the ratio of 1: 1.Alkene enter one
Step reaction it may happen that, but it is generally suppressed by hydrogen or inert environments.Therefore, wax product 14 can have about 1: 1 to about
1.4: 1, the alkane of e.g., from about 1.1: 1: alkene ratio.In an exemplary embodiment, putting down of the wax product 14 formed
Average molecular weight is about 5000 grams every mole (g/mol) to about 15000g/mol, e.g., from about 6000g/mol to about 9000g/mol.
In an exemplary embodiment, reaction zone 20 is provided with catalyst, such as depolymerization catalyst.Exemplary solution
Poly-catalyst can include solid acid catalyst, liquid acid catalyst, radical initiator, hydrogenation catalyst (such as nickel), boiling
Catalyst etc. on stone, carrier (such as aluminium oxide or silicon dioxide).Additionally or alternatively, the container of reaction zone 20 is formed
Wall can serve as depolymerization catalyst.
After its formation, can be in reaction zone 20 and in purging gaseous environment, in reaction zone 20 and at release purging
Under environmental condition after gas, or after removal from reaction zone 20, wax product 14 is cooled to ambient temperature.
The device 10 of Fig. 1 can be used in batch technology, and wherein reaction zone 20 is formed by autoclave or other chamber, or can
In continuous flow process, wherein reaction zone 20 is flow type autoclave, pressurized stream formula reactor and/or extruder.
Fig. 2 illustrates a kind of substituted device 10, and it may be relatively beneficial to continuous flow process.Similar with Fig. 1, the plastics of Fig. 2
Plastic raw materials 12 is changed into wax product 14, such as Tissuemat E by processing unit (plant) 10.A kind of exemplary plastic raw material 12 is discarded
Plastics, including the film or the bag that are derived from process recycling after recirculation after consumption or industry.The plastics forming raw material 12 can be limited
In the plastics of single type, such as polyethylene or polypropylene, or the mixture of plastic compound can be included.
As shown, plastic raw materials 12 and purging gas 18 are fed respectively to reaction zone 20.A kind of exemplary blowing
Scavenging body 18 includes hydrogen, and can include noble gas or multiple gases.In an exemplary embodiment, purging
Gas 18 is the purest hydrogen.As used in this article, term " the purest hydrogen " refers to that purging gas has
The hydrogen content of at least about 95wt%.In specific embodiments, the hydrogen content of purging gas is at least about 99wt%.Example
As, exemplary purging gas includes the non-hydrogen compound of less than 100 parts (ppm) in parts per million.In other embodiments,
Purging gas 18 is the mixture of hydrogen and noble gas.Such as, purging gas 18 can be the mixture of hydrogen and nitrogen, example
As hydrogen partial pressure is at least about 0.5atm, the mixture of the most about 0.8atm, e.g., from about 1atm.A kind of exemplary mixture
Hydrogen partial pressure be at least about 1.5atm, the most about 2.0atm.
As shown in Figure 2, plastic raw materials 12 and purging gas 18 are independently through pretreatment heater 32.At other
In embodiment, purging gas 18 is introduced to plastic raw materials 12, and makes the two together through pretreatment heater 32.Arbitrary
In kind of situation, pretreatment heater 32 can fully heating of plastic raw material 12 so that molten thermoplastic material.An example
Property embodiment in, pretreatment heater 32, through controlling to run under low pretreatment temperature, thus is being not resulted in thermal degradation
In the case of make plastic raw materials 12 melt.Such as, plastic raw materials 12 can be heated to about 100 DEG C to about by pretreatment heater 32
150 DEG C, the temperature of e.g., from about 135 DEG C.Make the plastic raw materials 12 persistent period required for pretreatment heater 32 can be through
Control so that plastic raw materials 12 substantially completely melts, such as, can be about 1 through the persistent period of pretreatment heater 32
Minute to about 90 minutes.
In an exemplary embodiment, pretreatment heater 32 is furnished with pre-treatment stirrer 36.Especially, for
For the embodiment before pretreatment heater 32 or wherein plastic raw materials 12 and hydrogen purge gas 18 mutually introduced, in advance
Processing agitator 36 can mix and promote hydrogen purge gas 18 to dissolve in plastic raw materials 12.A kind of exemplary pretreatment is stirred
Mixing device 36 is static mixer, and plastic raw materials 12 and hydrogen purge gas 18 are extruded by it.
Although in specific embodiments, pretreatment heater 32 can be used for making plastic raw materials 12 melted and making hydrogen purge
Gas 18 dissolves in plastic raw materials 12, but it is also alternatively used for pre-fibres from thermoplastics materials 12 and hydrogen purge gas 18, and
It is not result in melting, thus reduces the heating burden in downstream.Such as, plastic raw materials can be heated to about by pretreatment heater 32
60 DEG C to about 90 DEG C.For such embodiment, plastic raw materials 12 and hydrogen purge gas 18 are introduced to reaction zone 20, and
Heated by heater 24 so that plastic raw materials 12 melts under low pretreatment temperature.Such as, heater 24 can be by reaction zone 20
It is heated to about 100 DEG C to about 150 DEG C, the temperature of e.g., from about 135 DEG C.Low pretreatment temperature can be remained selected by heater 24
Persistent period, e.g., from about 1 minute to about 90 minute.In order to make the thermal degradation of essentially all of plastic raw materials 12, pass through agitator
Hydrogen purge gas 18 is mixed by 28 (such as blender or other mixed organization or static mixers) and to make it dissolve in the most molten
In the plastic raw materials 12 melted, molten plastic raw materials 12 and the mixture of hydrogen purge gas 18 are by described static mixer
Extrusion.
Make plastic raw materials 12 melted by pretreatment heater 32 or heater 24 and made by agitator 36 or 28
After hydrogen purge gas 18 dissolves in plastic raw materials 12, heater 24 runs under controlling with at high reaction temperature, so that
Obtain molten plastic raw materials 12 thermal degradation.From reaction zone 20, non-inert gas is removed to promote in heat by purging gas 18
Target response in degradation process.The reaction zone 20 including plastic raw materials 12 and hydrogen purge gas 18 can be added by heater 24
Heat to about 300 DEG C to about 500 DEG C, the high reaction temperature of e.g., from about 405 DEG C.High reaction temperature can be maintained and be enough to by heater 24
Make the persistent period of essentially all molten plastic raw materials 12 thermal degradation, such as, maintain about 1 minute to about 45 minutes, example
Such as the persistent period of 30 minutes.In an exemplary embodiment, plastic raw materials 12 experience thermal depolymerization (thermal degradation process it
One), rather than random scission or side base eliminate.The oxidation of plastic raw materials 12 is impossible, because all of oxygen all passes through
Purging gas 18 is removed from reaction zone.
Reaction zone 20 is heated to time that high reaction temperature persistently selectes so that essentially all of plastic raw materials 12
Thermal degradation also forms wax product 14.A kind of exemplary wax product comprises alkane and olefin(e) compound.Stoichiometric depolymerization is split
Change reaction and generally form alkane and alkene with the ratio of 1: 1.The further reaction of alkene it may happen that, but it generally passes through
Hydrogen or inert environments suppression.Therefore, wax product 14 can have about 1: 1 to about 1.4: 1, the alkane of e.g., from about 1.1: 1: alkene
Hydrocarbon ratio.In an exemplary embodiment, the mean molecule quantity of the wax product 14 formed is about 5000 grams of every mole of (g/
Mol) to about 15000g/mol, e.g., from about 6000g/mol to about 9000g/mol.
In an exemplary embodiment, the reaction zone 20 in Fig. 2 is provided with catalyst, such as depolymerization catalyst.One
Plant exemplary depolymerization catalyst and can include solid acid catalyst, liquid acid catalyst, radical initiator, hydrogenation catalyst
Catalyst etc. on (such as nickel), zeolite, carrier (such as aluminium oxide or silicon dioxide).Additionally or alternatively, formed instead
The chamber wall answering district 20 can serve as depolymerization catalyst.
After its formation, can be in reaction zone 20 and in purging gaseous environment, in reaction zone 20 and at release purging
Under environmental condition after gas, or after removal from reaction zone 20, wax product 14 is cooled to ambient temperature.
Fig. 3 illustrates another embodiment of the device 10 for plastic raw materials 12 changes into wax product 14.At Fig. 3
In, only plastic raw materials 12 is through pretreatment heater 32.Described plastic raw materials 12 can be heated so that it substantially completely melts
Melt, or preheating is to reduce the heating burden of downstream heater 24.In an exemplary embodiment, plastic raw materials 12 is added
Heat to about 100 DEG C to about 150 DEG C, the low pretreatment temperature of e.g., from about 135 DEG C.Plastic raw materials 12 is in pretreatment heater 32
The time of staying can be the selected persistent period of e.g., from about 1 minute to about 90 minutes.As shown, pretreatment heater 32 is also
It is not equipped with agitator, because hydrogen is undissolved in plastic raw materials 12.
After plastic raw materials 12 leaves pretreatment heater 32, it is introduced into reaction zone 20.As shown, purging
Gas 18 such as hydrogen can be introduced to plastic raw materials 12 in the upstream of reaction zone 20.Alternately, and as shown in FIG. 1,
Purging gas 18 can be fed directly to reaction zone 20, and is incorporated herein to plastic raw materials 12.In either case, plastics are made
Raw material 12 and purging gas 18 receive in reaction zone 20.Non-inert gas is removed from reaction zone 20 by purging gas 18.
Melt if plastic raw materials 12 is not through pretreatment heater 32, then plastic raw materials 12 and hydrogen purge gas
18 are heated so that plastic raw materials 12 melts by heater 24 under low pretreatment temperature.Such as, heater 24 can will react
District 20 is heated to about 100 DEG C to about 150 DEG C, the temperature of e.g., from about 135 DEG C.Low pretreatment temperature can be maintained choosing by heater 24
The fixed persistent period, e.g., from about 1 minute to about 90 minute.In order to make the thermal degradation of essentially all of plastic raw materials 12, by stirring
Mix device 28 (such as blender or other mixed organization or static mixer) mixed by hydrogen purge gas 18 and make it dissolve in
In molten plastic raw materials 12, molten plastic raw materials 12 and the mixture of hydrogen purge gas 18 are mixed by described static state
Clutch is extruded.
Hydrogen is made to blow making plastic raw materials 12 melt by pretreatment heater 32 or heater 24 and pass through agitator 28
After scavenging body 18 dissolves in plastic raw materials 12, heater 24 runs under controlling with at high reaction temperature, so that molten
Plastic raw materials 12 thermal degradation.From reaction zone 20, non-inert gas is removed to promote at thermal degradation process by purging gas 18
In target response.The reaction zone 20 including plastic raw materials 12 and hydrogen purge gas 18 can be heated to about by heater 24
300 DEG C to about 500 DEG C, the high reaction temperature of e.g., from about 405 DEG C.High reaction temperature can be maintained and be sufficient so that base by heater 24
The persistent period of all molten plastic raw materials 12 thermal degradations in basis, such as, maintain about 1 minute to about 45 minutes, such as 30 points
The persistent period of clock.In an exemplary embodiment, plastic raw materials 12 experiences thermal depolymerization (one of thermal degradation process), rather than
Random scission or side base eliminate.The oxidation of plastic raw materials 12 is impossible, because all of oxygen is all by purging gas
18 remove from reaction zone.
Reaction zone 20 is heated to time that high reaction temperature persistently selectes so that essentially all of plastic raw materials 12
Thermal degradation also forms wax product 14.A kind of exemplary wax product comprises alkane and olefin(e) compound.Stoichiometric depolymerization is split
Change reaction and generally form alkane and alkene with the ratio of 1: 1.The further reaction of alkene it may happen that, but it generally passes through
Hydrogen or inert environments suppression.Therefore, wax product 14 can have about 1: 1 to about 1.4: 1, the alkane of e.g., from about 1.1: 1: alkene
Ratio.In an exemplary embodiment, the mean molecule quantity of the wax product 14 formed is about 5000 grams every mole (g/mol)
To about 15000g/mol, e.g., from about 6000g/mol to about 9000g/mol.
In an exemplary embodiment, the reaction zone 20 in Fig. 3 is provided with catalyst, such as depolymerization catalyst.One
Plant exemplary depolymerization catalyst and can include solid acid catalyst, liquid acid catalyst, radical initiator, hydrogenation catalyst
Catalyst etc. on (such as nickel), zeolite, carrier (such as aluminium oxide or silicon dioxide).Additionally or alternatively, formed instead
The chamber wall answering district 20 can serve as depolymerization catalyst.
After its formation, can be in reaction zone 20 and in purging gaseous environment, in reaction zone 20 and at release purging
Under environmental condition after gas, or after removal from reaction zone 20, wax product 14 is cooled to ambient temperature.
The embodiment of method for converting-plastics to be become wax is presented herein below.Described embodiment carries merely for illustrative purpose
Supply, it is not intended to be limited in multiple embodiments contemplated herein by any way.
Embodiment
In the first embodiment of the embodiment of the method for converting-plastics being become wax, by the low-density of 50 grams (g)
Polyethylene (LDPE) is introduced in stainless steel autoclave.Hydrogen is used to purge height with 40 sccm (sccm)
Pressure still environment, and autoclave is heated to 135 DEG C, continue 60 minutes, so that LDPE melts.Subsequently, molten LDPE is added
Heat, to 405 DEG C, continues 30 minutes, makes LDPE depolymerization under continuous hydrogen purge.Then autoclave is cooled to ambient temperature,
And reclaim product wax.The composition using the product wax of hydrogen formation illustrates in the following table.
In the second embodiment of the embodiment of the method for converting-plastics being become wax, low by 50 or 20 grams (g)
Density polyethylene (LDPE) is introduced in stainless steel autoclave.Nitrogen is used to blow with 40 sccm (sccm)
Sweep autoclave environment, and autoclave is heated to 135 DEG C, continue 60 minutes, so that LDPE melts.Subsequently, by molten
LDPE is heated to 405 DEG C, continues 30 minutes, makes LDPE depolymerization under continuous nitrogen purges.Then autoclave is cooled to ring
Border temperature, and reclaim product wax.Do not use hydrogen and the composition with the product wax only using the autoclave of nitrogen purging to be formed
Illustrate in the following table.
Table
As in table it can be seen that the product wax using the technique of hydrogen purge gas to obtain has the vision face of rice white
Color or outward appearance, its for application-specific be commercial preferably.
As described herein, there has been provided for the method that converting-plastics is become wax.In an exemplary embodiment, mould
Expect the product wax that depolymerization in the hydrogen gas atmosphere comprises alkane and alkene with formation.
Although having been proposed that at least one exemplary in foregoing detailed description it should be appreciated that
It is to there is also substantial amounts of modification.It is to be further understood that described exemplary or various exemplary embodiment are only
Embodiment, it is not intended to limit the scope of theme required for protection, the suitability or configuration.But, above
Detailed description will provide route map easily for those skilled in the art, be used for implementing one or more exemplary embodiment party
Case.In the case of it being understood that the scope illustrated in without departing substantially from claims, describe in an exemplary embodiment
The function of key element and layout aspect can make various change.
Claims (10)
1., for the method that waste plastic (12) is changed into wax, said method comprising the steps of:
Waste plastic is introduced in chamber (20)；
Hydrogen (18) is added to described chamber；
Fully heating waste plastic and hydrogen is so that waste plastic thermal depolymerization, thus is formed and comprise alkane and olefin(e) compound
Wax product (14).
2. the method for claim 1, it farther includes to provide the chamber with depolymerization catalyst, described depolymerization catalyst to be selected from
Solid acid catalyst, liquid acid catalyst, radical initiator, hydrogenation catalyst, zeolite and supported catalyst.
3. the process of claim 1 wherein:
Waste plastic is made to melt the temperature including that waste plastic is heated to about 100 DEG C to about 150 DEG C；And
Heating waste plastic and hydrogen include the temperature that waste plastic and hydrogen are heated to about 300 DEG C to about 500 DEG C.
4. the process of claim 1 wherein, heating waste plastic and hydrogen include formed with at least about 1.1: 1 alkane: alkene
Hydrocarbon ratio comprises alkane and olefin(e) compound and weight average molecular weight is about 5000 grams every mole (g/mol) to about 15000g/mol
Tissuemat E product.
5. the process of claim 1 wherein and include in waste plastic is introduced to chamber being introduced by waste plastic with batch technology
To chamber.
6. the process of claim 1 wherein after waste plastic is introduced in chamber, hydrogen is added to described chamber.
7. the process of claim 1 wherein that fully heating waste plastic and hydrogen are so that waste plastic thermal depolymerization includes forming match
Family name's colourity (ASTM D156) is at least about the wax product of 0.
8. the method for claim 7, the most fully heating waste plastic and hydrogen are so that waste plastic thermal depolymerization includes that formation is flat
Average molecular weight is about 5000 grams every mole (g/mol) to the wax product of about 15000g/mol.
9. the method for claim 7, the most fully heating waste plastic and hydrogen are so that waste plastic thermal depolymerization includes that formation is flat
Average molecular weight is about 6000 grams every mole (g/mol) to the wax product of about 9000g/mol.
10. the process of claim 1 wherein that fully heating waste plastic and hydrogen are so that waste plastic thermal depolymerization includes forming match
Family name's colourity (ASTM D156) is at least about the wax product of+20.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201461946047P | 2014-02-28 | 2014-02-28 | |
| US61/946047 | 2014-02-28 | ||
| US14/620,057 US20150247096A1 (en) | 2014-02-28 | 2015-02-11 | Methods for converting plastic to wax |
| US14/620057 | 2015-02-11 | ||
| PCT/US2015/016583 WO2015130545A1 (en) | 2014-02-28 | 2015-02-19 | Methods for converting plastic to wax |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106132653A true CN106132653A (en) | 2016-11-16 |
Family
ID=54006471
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201580011050.2A Pending CN106132653A (en) | 2014-02-28 | 2015-02-19 | The method that converting-plastics is become wax |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US20150247096A1 (en) |
| EP (1) | EP3110604A4 (en) |
| JP (1) | JP2017513964A (en) |
| KR (1) | KR20160127758A (en) |
| CN (1) | CN106132653A (en) |
| MX (1) | MX2016010924A (en) |
| WO (1) | WO2015130545A1 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107922851A (en) * | 2016-03-31 | 2018-04-17 | 索尔维公司 | For by cracking by method of the converting-plastics into wax and thus obtained hydrocarbon mixture |
| CN113813883A (en) * | 2021-09-16 | 2021-12-21 | 上海簇睿低碳能源技术有限公司 | Method for recycling waste polyethylene |
| CN114867823A (en) * | 2019-12-23 | 2022-08-05 | 雪佛龙美国公司 | Recycle economics for conversion of plastic waste to polyethylene and chemicals by refinery crude unit |
Families Citing this family (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2898257C (en) | 2013-01-17 | 2021-10-05 | Greenmantra Recycling Technologies Ltd. | Catalytic depolymerisation of polymeric materials |
| US20170232416A1 (en) * | 2015-12-30 | 2017-08-17 | Greenmantra Recycling Technologies Ltd. | Reactor For Continuously Treating Polymeric Material |
| US10472487B2 (en) | 2015-12-30 | 2019-11-12 | Greenmantra Recycling Technologies Ltd. | Reactor for continuously treating polymeric material |
| CN108779398B (en) | 2016-02-13 | 2022-03-01 | 绿色颂歌再生科技有限公司 | Polymer modified asphalt with wax additive |
| MX2018011492A (en) * | 2016-03-24 | 2019-02-20 | Greenmantra Recycling Tech Ltd | Wax as a melt flow modifier and processing aid for polymers. |
| US20190119191A1 (en) * | 2016-03-31 | 2019-04-25 | Solvay Sa | Process for converting plastic into waxes by catalytic cracking and a mixture of hydrocarbons obtained thereby |
| CN108026453A (en) | 2016-03-31 | 2018-05-11 | 索尔维公司 | For by catalytic cracking by method of the converting-plastics into wax and thus obtained hydrocarbon mixture |
| US20170283525A1 (en) * | 2016-03-31 | 2017-10-05 | Honeywell International Inc.; Mail Stop 4D3 | Methods of producing a polyolefin wax product |
| JP2019512586A (en) * | 2016-03-31 | 2019-05-16 | ソルヴェイ（ソシエテ アノニム） | Process for the conversion of plastics into waxes by decomposition and mixtures of hydrocarbons obtained thereby |
| JP7071346B2 (en) | 2016-09-29 | 2022-05-18 | グリーンマントラ リサイクリング テクノロジーズ リミテッド | Reactor for processing polystyrene materials |
| US10723858B2 (en) | 2018-09-18 | 2020-07-28 | Greenmantra Recycling Technologies Ltd. | Method for purification of depolymerized polymers using supercritical fluid extraction |
| KR101995951B1 (en) * | 2019-03-12 | 2019-07-03 | 주식회사 라이온켐텍 | A continuous method for manufacturing polyolefin copolymer |
| CN110229685B (en) * | 2019-06-12 | 2020-08-25 | 中国科学院广州能源研究所 | Method for preparing fuel oil by high-pressure thermal conversion of waste plastics |
| CA3151493A1 (en) * | 2019-08-27 | 2021-03-04 | Greenmantra Recycling Technologies Ltd. | Modification of asphalt formulations containing recycled materials with polymers derived from depolymerized plastics |
| JP7325621B2 (en) * | 2019-09-09 | 2023-08-14 | バーゼル・ポリオレフィン・イタリア・ソチエタ・ア・レスポンサビリタ・リミタータ | Polyolefin depolymerization using metal oxides |
| CA3222774A1 (en) * | 2019-12-23 | 2021-07-01 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polyethylene and lubricating oil via crude and isomerization dewaxing units |
| JP2023508353A (en) | 2019-12-23 | 2023-03-02 | シェブロン ユー．エス．エー． インコーポレイテッド | Circular Economy of Waste Plastics to Polyethylene via Refining FCC and Alkylation Units |
| US11566182B2 (en) | 2020-03-30 | 2023-01-31 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polyethylene via refinery FCC feed pretreater and FCC units |
| US11964315B1 (en) | 2023-03-31 | 2024-04-23 | Nexus Circular LLC | Hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics and methods of making and use thereof |
| US11952545B1 (en) | 2023-03-31 | 2024-04-09 | Nexus Circular LLC | Hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics and methods of making and use thereof |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB728551A (en) * | 1952-04-01 | 1955-04-20 | Basf Ag | Improvements in the production of wax-like saturated polyethylenes |
| US4851601A (en) * | 1988-01-19 | 1989-07-25 | Mobil Oil Corporation | Processing for producing hydrocarbon oils from plastic waste |
| US5079385A (en) * | 1989-08-17 | 1992-01-07 | Mobil Oil Corp. | Conversion of plastics |
| EP0577279A1 (en) * | 1992-06-29 | 1994-01-05 | Bp Exploration Operating Company Limited | Process for the conversion of polymers |
| CA2202941A1 (en) * | 1997-04-17 | 1998-10-17 | Andrzej Z. Krzywicki | Depolymerization |
| CN103168016A (en) * | 2010-07-15 | 2013-06-19 | 绿色颂歌再生科技有限公司 | Method and producing waxes and grease base stocks through catalytic depolymerisation of waste plastics |
| CN103328619A (en) * | 2011-01-18 | 2013-09-25 | 雪佛龙美国公司 | Process for making high viscosity index lubricating base oils |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH369899A (en) * | 1956-08-01 | 1963-06-15 | Hoechst Ag | Process for the production of low molecular weight polymers of olefins |
| US3441628A (en) * | 1965-12-13 | 1969-04-29 | Leuna Werke Veb | Process for producing waxlike low molecular ethylene polymers and copolymers |
| ATE141294T1 (en) * | 1991-03-05 | 1996-08-15 | Bp Chem Int Ltd | CRACKING OF POLYMERS |
| US5158982A (en) * | 1991-10-04 | 1992-10-27 | Iit Research Institute | Conversion of municipal waste to useful oils |
| DE19822568A1 (en) * | 1998-05-20 | 1999-11-25 | Sebastian Hein | Treatment of plastic waste by pyrolysis |
| US6143940A (en) * | 1998-12-30 | 2000-11-07 | Chevron U.S.A. Inc. | Method for making a heavy wax composition |
| CN1894367A (en) * | 2003-12-19 | 2007-01-10 | 国际壳牌研究有限公司 | Systems, methods, and catalysts for producing a crude product |
| KR101162612B1 (en) * | 2011-11-30 | 2012-07-04 | 이엔에프씨 주식회사 | Oil production system from waste material and catalyst therefor |
-
2015
- 2015-02-11 US US14/620,057 patent/US20150247096A1/en not_active Abandoned
- 2015-02-19 CN CN201580011050.2A patent/CN106132653A/en active Pending
- 2015-02-19 MX MX2016010924A patent/MX2016010924A/en unknown
- 2015-02-19 KR KR1020167025196A patent/KR20160127758A/en unknown
- 2015-02-19 JP JP2016554442A patent/JP2017513964A/en active Pending
- 2015-02-19 WO PCT/US2015/016583 patent/WO2015130545A1/en active Application Filing
- 2015-02-19 EP EP15756041.8A patent/EP3110604A4/en not_active Withdrawn
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB728551A (en) * | 1952-04-01 | 1955-04-20 | Basf Ag | Improvements in the production of wax-like saturated polyethylenes |
| US4851601A (en) * | 1988-01-19 | 1989-07-25 | Mobil Oil Corporation | Processing for producing hydrocarbon oils from plastic waste |
| US5079385A (en) * | 1989-08-17 | 1992-01-07 | Mobil Oil Corp. | Conversion of plastics |
| EP0577279A1 (en) * | 1992-06-29 | 1994-01-05 | Bp Exploration Operating Company Limited | Process for the conversion of polymers |
| CA2202941A1 (en) * | 1997-04-17 | 1998-10-17 | Andrzej Z. Krzywicki | Depolymerization |
| CN103168016A (en) * | 2010-07-15 | 2013-06-19 | 绿色颂歌再生科技有限公司 | Method and producing waxes and grease base stocks through catalytic depolymerisation of waste plastics |
| CN103328619A (en) * | 2011-01-18 | 2013-09-25 | 雪佛龙美国公司 | Process for making high viscosity index lubricating base oils |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107922851A (en) * | 2016-03-31 | 2018-04-17 | 索尔维公司 | For by cracking by method of the converting-plastics into wax and thus obtained hydrocarbon mixture |
| CN114867823A (en) * | 2019-12-23 | 2022-08-05 | 雪佛龙美国公司 | Recycle economics for conversion of plastic waste to polyethylene and chemicals by refinery crude unit |
| CN114867823B (en) * | 2019-12-23 | 2024-02-13 | 雪佛龙美国公司 | Recycling economy for converting plastic waste into polyethylene and chemicals by refinery crude unit |
| CN113813883A (en) * | 2021-09-16 | 2021-12-21 | 上海簇睿低碳能源技术有限公司 | Method for recycling waste polyethylene |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2015130545A1 (en) | 2015-09-03 |
| KR20160127758A (en) | 2016-11-04 |
| EP3110604A1 (en) | 2017-01-04 |
| US20150247096A1 (en) | 2015-09-03 |
| MX2016010924A (en) | 2016-11-14 |
| EP3110604A4 (en) | 2017-10-04 |
| JP2017513964A (en) | 2017-06-01 |
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