CN108291150A - By plastics-production hydrocarbon fuel - Google Patents
By plastics-production hydrocarbon fuel Download PDFInfo
- Publication number
- CN108291150A CN108291150A CN201680068435.7A CN201680068435A CN108291150A CN 108291150 A CN108291150 A CN 108291150A CN 201680068435 A CN201680068435 A CN 201680068435A CN 108291150 A CN108291150 A CN 108291150A
- Authority
- CN
- China
- Prior art keywords
- hydrocarbon
- extraction
- fuel
- reative cell
- kiln
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B27/00—Arrangements for withdrawal of the distillation gases
- C10B27/06—Conduit details, e.g. valves
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
-
- 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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- 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
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/20—Nitrogen-containing compounds
-
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/27—Organic compounds not provided for in a single one of groups C10G21/14 - C10G21/26
-
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
Abstract
Disclosed herein is a kind of by the kiln (100) used in plastics-production hydrocarbon fuel.Kiln (100) includes the washer (200) being in fluid communication with reative cell (130), washer (200) is configured in condensation reaction room gaseous product flow (501) higher than the hydrocarbon of predetermined upper hydrocarbon context, to return it to reative cell (130) for further being heated there is no oxygen.There is disclosed herein waste plastics is converted in the method for the business useful form of diesel oil or the like.This method thick fuel caused by plastics in pyrolysis processing including the use of the first extraction step and the processing of the second extraction step, the first extraction step include adverse current liquid-liquid extraction, and the second extraction step includes solvent of the adverse current extraction from the first extraction step.
Description
Cross reference to related applications
The priority of the following Australian Provisional Patent Application of patent application claims：AU2015904828, in 2015
November 24 submitted, entitled " by the kiln used in plastics-production hydrocarbon fuel "；AU2016901654, May 5 in 2016
Day submits, entitled " plastics derivatived fuel and its manufacturing method "；And AU2016902869, it is submitted on July 21st, 2016,
Entitled " plastics derivatived fuel and its manufacturing method II ", the disclosure of which is incorporated herein by reference in their entirety.
Technical field
The present disclosure generally relates to produce hydrocarbon fuel by plastics waste material.
Background technology
Plastics are the materials typically formed by long chain organic polymers.Since production cost is relatively low and manufacture is held
Easily, therefore plastic material is used for all over the world in various products comprising a large amount of disposable products are such as packed.With by
The consumption of disposable products made of plastic material increases, and relevant plastics waste material also increases, due to plastic material send to
Long lifespan in the case of landfill yard, leads to environmental problem.Other problems related with waste plastics is toppled over include soil pollution and not
It educates.
Plastics recovery is recycling waste material or waste plastics and the process that the material is reprocessed into useful products.However, with
Metal recovery is different, and the recycling of plastic material is low and challenging due to economic benefit.Due to the change of long chain organic polymers
Learning property makes them be difficult to, and the recycling of plastics faces more difficulties.In addition, plastics waste material usually requires to be sorted into use
In the various plastic resin types of independent recycling processing, for example, polyethylene terephthalate (PET), high-density polyethylene
Alkene (HDPE), polyvinyl chloride (PVC).
Since plastics are formed by the long chain organic polymers containing hydrogen and carbon, develop for by long chain polymeric
The technique that object is converted into the hydrocarbon fuel product (such as gasoline or diesel oil) of short length.These techniques are usually directed to plastic material
Pyrolysis long-chain polymer to be reduced into the polymer of smaller chain length.
Technology currently used for plastic material to be processed into hydrocarbon fuel product typically results in the production of wax and tar class product
Raw, these products can pollute the equipment used in technique and pipeline.In addition, the system of introducing or the particle formed during the reaction
The presence of material can lead to the formation of the product of the reluctant similar sludge of low-purity in condensation.In addition, overall need
The hydrocarbon directly condensed after pyrolytic reaction is reheated to isolate required hydrocarbon.
The alternative of plastics in landfills disposition is to burn.However, this results in such as stove damage and noxious gas emission with
And the problem of stench.Burning is considered as a kind of generally unwelcome and can not held by the ever-increasing environmental consciousness of society
Continuous Treatment of Waste Plastics method.
In the U.S., nineteen ninety-five has formulated " the recycling of packaging utilization method " that regulation recycles the responsibility of plastics.In view of
These situations have been made a variety of trials and have been recycled plastic wastes as resource recently.However, after method promulgation
In 20 years, actually only 8% plastic wastes are recycled utilization.It is apparent that in the presence of about the environment for improving the rate of recovery
Driving.However, logistics and lasting social factor still decide that most plastic wastes are dumped, even worse burnt
It burns.
Disappear further consideration is that accounting for annual global crude oil to the mineral cost of the ever-increasing plastics of global provisioning demand
About the 7% of consumption.In brief, production plastics are needed using oil as cost --- unless the plastics are oily after reaching its commercial object
It can recycle, otherwise our global mineral debt can only increase.
Her rattan profit one of Japanese invention people has promoted the idea for converting waste plastics to by plastics pyrolysis fuel oil.Pyrolysis is
Thermochemical Decomposition is carried out to the organic material of such as plastics at elevated temperatures in the absence of oxygen.It is related to chemistry at
Change while dividing with physics phase, and is irreversible.Usually within the temperature range of 400-900 DEG C, under small overvoltage
It is pyrolyzed.For example, the technique is widely used in oil plant to obtain low molecular weight monomers from naphtha, and can be used for firing
The waste plastics processing of material production, as its incineration or the alternative of landfill.
In this process, the long polymer molecule of plastic material is broken down into short chain hydrocarbon with the help of heat and pressure
Compound.In essence, which has imitated the property that organic material resolves into oil within thousands of or even millions of years.Short
Pyrolytic process is realized by heat-flash in closed anaerobic system in time.Temperature can be reduced using catalyst and increase
Add yield.Other substances that can be pyrolyzed are biomass, damaged tire, lubricating oil, coal and petroleum residues；Waste tyre pyrolytic is wherein
It is most popular and most profitable.
The basic process of pyrolysis carries out as follows：(1) comminution step, wherein waste must detach, and in feasible situation
Lower cleaning.Then it is shredded to accelerate to react and ensure that the reaction was complete.(2) anaerobic heating stepses, wherein being reacted in anaerobic
The material of chopping is heated in device in a controlled manner.One of the factor of most critical is to maintain appropriate temperature (plastics in this operation
About 430 DEG C) and the rate of heat addition, because they define the quality and quantity of final products.(3) condensing steps, wherein by making
The gas come out from reactor is by condenser pipe or is directly blasted in water and is condensed.(4) distilation steps, wherein the oil of gained
Mixture can be used as furnace oil, but not pure enough for engine.In order to be used as engine fuel, need by dividing
It evaporates or required product is extracted from mixture and purified to some other purification means.
Some benefits of pyrolysis are that the process not will produce noxious pollutant, and by-product may be used as running the device
Fuel.For plastics, it is gasoline, kerosene, bavin that can be pyrolyzed some valuable fuel of extraction and solvent by waste plastics
Oil, benzene, liquefied petroleum gas, toluene and dimethylbenzene.In addition, pyrolytic process relative efficiency, because one kilogram of waste may produce up to 1
The fuel risen.By directly comparing, the plastics for burning identical quantity will produce three kilograms of carbon dioxide.
No aquathermolysis can be used for producing the liquid fuel similar to the diesel oil from plastic wastes, compared with conventional diesel,
Its Cetane number is higher, and sulfur content is relatively low.It is most preferably selected from second extracted in waste plastic after fuel is recycling using pyrolysis
It selects, it is more excellent than filling in the environment, and can help to reduce the dependence to external fossil fuel and geographical extraction.In addition, modeling
Diesel fuel derived from material can by commercial distribution and consumption it is upper it is sufficiently pure in the form of obtain.On the other hand, these technologies are still
It is in the junior stage --- and target known in the art is to find the more efficient means that fuel is obtained from waste plastics.
0 620 264 A2 of European patent application discloses a kind of technique manufacturing lubricating oil with waste plastics.The technology utilization
Process in inert solid fluid bed and with such as nitrogen stream.By crackate in the aluminium oxide containing metal component
Hydrotreating on catalyst or other refractory metal oxide carriers, then optional isoversion.However, gross production rate is less than pre-
Phase.The heterogeneous catalyst part instructed leads to the result.There is no the introductions for using better heterogeneous catalyst.Moreover, EP
The technique that 0 620 264A2 do not instruct production high yield heavy grease.
Become known for preparing many methods of low boiling point hydrocarbon from waste plastics and higher boiling point hydrocarbon compound.US4,
851,601 describe the pyrolytic reaction in reaction kettle (vertically or horizontally), and the wherein outer wall of kettle is heated at high temperature, and its
In substance heated indirectly.In this approach, when reactor directly heats at high temperature, outer wall is easily deformed.Due to
Hot-spot, substance are easy to be sintered on inner wall so that the conversion ratio of reaction and the service life of reactor substantially reduce.In addition, anti-
Answer device heat transfer coefficient relatively low, reaction residue is difficult to be discharged, and the catalysis reaction in fixed bed needs independent heat supply.These are
The common drawback of reaction kettle in the prior art.
It is similar to the above in the helical reactors that some special dimensions use.Working time connects transmission heat.Reactor
Outer wall directly heats at high temperature, makes the substance indirectly heat in reactor.Therefore, heat transfer coefficient is unsatisfactory.
It can also be appreciated that in the case where this method itself generates a large amount of contaminated solvent slops, from plastics
The feasibility for extracting the method for diesel oil is limited.Therefore it provides for regenerate or recycle used in extracting method it is useless molten
The means of agent are also advantageous.
Therefore, in a preferred form, one or more embodiments of current open design, which can be used as, effectively independently connects
Continuous (or in case of need even batch) technological operation provides be used for from diesel from waste plastics and recycling at once
The solvent extracted.
Although describing General Principle disclosed herein hereinafter with reference to specific example, those skilled in the art will
Understand, they can be embodied as many other forms.
Any explanation of the file, action, material, equipment, the article that include in this specification etc. is not construed as recognizing any
Or all these items are because it has existed the composition prior art before the priority date of each claim of the application
Basis a part, or with the common sense in the relevant field of the disclosure.
Invention content
Throughout the specification, term " include (comprise) " or such as " including (comprises) " or " include
(comprising) " deformation will be understood as implying including stated element, entirety or step or element, entirety or step
Rapid group, but it is not excluded for any other element, integer or step or element, the group of integer or step.
In a first aspect, providing a kind of by the kiln used in plastics-production hydrocarbon fuel, which includes：
Reative cell；
Feed inlet, plastic raw materials for being supplied in reative cell by feed inlet；
Heater, heater is for heating reative cell；And
Washer, washer and reative cell in direct fluid communication；
Wherein kiln is configured to make the plastic raw materials in reative cell to be heated there is no oxygen, thus by plastics
At least part of raw material resolves into the reative cell gaseous product flow for including the hydrocarbon for being suitable as fuel, and
Wherein washer is configured to make hydrocarbon higher than predetermined upper hydrocarbon context in reative cell gaseous product flow
Compound removal is further heated with returning it to reative cell there is no oxygen.
Kiln can be configured as the temperature of the reative cell gaseous product flow for making the to leave reative cell base before entering washer
Do not decline in sheet.
Washer is configurable to make to leave the washer air-flow of washer in the temperature less than 350 DEG C.
Kiln can be the cylindrical horizontal kiln for including cylindrical shell, and reative cell may include being concentrically positioned in circle
Inner tube in cylindrical outer cover.
Heater for heating reative cell may include being flowed in the annular space limited between central inner pipe and shell
Dynamic hot-fluid medium, so that the outer surface of heat source medium heating inner tube.
The outer surface of inner tube may include multiple vortex generators, be imitated with increasing the heat transfer from heat source medium to reative cell
Rate.
Kiln may further include the blender for being stirred to react the plastic raw materials in room.In addition, kiln can be further
Including catalyst in the reaction chamber, catalyst is used to that the hydrocarbon for pushing it is expected chain length to and/or required aromatics will to be reacted
Hydrocarbon.
The kiln may further include the useless particle outlet for removing the granular materials that gives up from reative cell.
Second aspect, provides a kind of system by plastics-production hydrocarbon fuel, which includes according to first aspect
Kiln.
The system may further include at least one hydrocarbon retracting device, which uses
Hydrocarbon in the predetermined hydrocarbon context of recycling.During at least one hydrocarbon retracting device can be following
One or more：It is configured to condense the fractionating column of the hydrocarbon of the diesel range from hydrocarbon fuel streams；Match
Set the condenser of the hydrocarbon for condensing the gasoline-range from hydrocarbon fuel streams；And/or it is configured to condense
The compression set of the hydrocarbon of liquefied petroleum gas (LPG) range from hydrocarbon fuel streams.It is to be appreciated that with
The selection that the equipment of the condensation hydrocarbon gas of kiln is left in condensation depends on desired final product.
Fractionating column can be connected to the gas outlet stream of washer.Fractionating column can be further configured at least one
Partial condensation diesel oil is transferred to washer for use as cleaning solution.
Vacuum column can be set for removing water from the hydrocarbon of the diesel range condensed by fractionating column.
Condenser can be connected to the gas outlet stream of fractionating column.
Compression set can be connected to the gas outlet stream of condenser.
In the third aspect, provide a kind of by the assembly used in plastics-production hydrocarbon fuel, which includes：
Kiln comprising：
Reative cell；
Feed inlet, plastic raw materials for being supplied in reative cell by feed inlet；And
Heater, heater is for heating reative cell；
Wherein kiln is configured to make the plastic raw materials in reative cell to be heated there is no oxygen, thus by plastics
At least part of raw material resolves into the reative cell gaseous product flow for including the hydrocarbon for being suitable as fuel,
Washer, washer are in fluid communication with reative cell, and wherein washer is configured to make in reative cell gaseous product flow
Hydrocarbon higher than predetermined upper hydrocarbon context remove and make removed hydrocarbon return reative cell with
For further being heated there is no oxygen；And
Hydrocarbon retracting device, hydrocarbon retracting device are connected to washer fluid to receive reative cell gas
The remainder of product stream, hydrocarbon retracting device are configured to remove predetermined hydrocarbon from the remainder
Hydrocarbon in range.
In fourth aspect, a kind of method obtaining fuel from plastics is provided, this method includes making a certain amount of plastics
Pyrolysis processing is carried out, at least part of plastics is thus converted to thick fuel；And directly available shape is extracted in the following manner
The fuel of formula：
First extraction step, first extraction step include carrying out adverse current liquid-liquid using one or more Extraction solvents to carry
It takes to extract one or more impurity from thick fuel；
Second extraction step, second extraction step include countercurrently extracting contaminated one obtained by the first extraction step
Kind or a variety of Extraction solvents；And
Optionally Extraction solvent purification step, wherein by contaminated one or more Extraction solvent purifying to realize rear
Solvent reuses in continuous one or more extraction steps.
In one embodiment, the second extraction step includes the highly polar liquid using or mixtures thereof such as water, ethyl alcohol
It improves the polarity of contaminated Extraction solvent, and then Extraction solvent is made to repel extract；Then it is distilled out from Extraction solvent
One or more polar compounds.
It can be substantially as described in Fig. 2 and 3 about attached drawing according to the method that fourth aspect limits.
The 5th aspect, provide it is a kind of from plastics obtain fuel method, this method include make a certain amount of plastics into
Thus at least part of plastics is converted to thick fuel by row pyrolysis processing；And directly available form is extracted in the following manner
Fuel：
First extraction step comprising carry out adverse current liquid-liquid extraction using one or more Extraction solvents with from thick fuel
The middle one or more impurity of extraction；
Second extraction step comprising countercurrently extract the contaminated one or more extractions obtained by the first extraction step
Solvent.
In one embodiment, the second extraction step includes that use is extracted aromatic compounds from Extraction solvent and had similar
The light fraction nonpolar solvent of or mixtures thereof such as heptane, hexane of polar compound；Then it is distilled from Extraction solvent
Light fraction solvent.
It can be substantially as described in the Figure 4 and 5 about attached drawing according to the method that the 5th aspect limits.
In one or more embodiments, Extraction solvent is that n-methyl-2-pyrrolidone or similar dipolar aprotic are molten
Agent, such as dimethylformamide, dimethyl sulfoxide (DMSO).It is to be recognized, however, that can use has physics appropriate and pole
Any solvent of property feature.
In one or more embodiments, solvent purification step is extracted.It extracts in a substantial continuous manner
Solvent purification step is to provide the substantially continuous operation of the first and/or second extraction step.
In one or more embodiments, in adverse current is extracted, Extraction solvent enters the top of packed tower and thick fuel
Into the bottom of packed tower.Optionally, Extraction solvent enters the bottom of packed tower, and coarse fodder fuel enters the top of packed tower.
In one or more embodiments, Extraction solvent extracts impurity, and contaminated Extraction solvent is made to leave packed tower
Bottom and purify the top that fuel leaves packed tower.Optionally, contaminated Extraction solvent may exit off the top of packed tower,
And the fuel purified may exit off the bottom of packed tower.
In one or more embodiments, or mixtures thereof contaminated Extraction solvent and water, ethyl alcohol etc. mix so that such as
The non-polar compound of aromatic compounds comes out from solution.Suitable solvent can be had in the range of ethyl alcohol is to water
Polar any solvent.
In one or more embodiments, impurity compound is flowed out from the Extraction solvent being polluted by water.
In one or more embodiments, water is distilled from Extraction solvent using conventional climbing film evaporator.It is this
Distillation may or will not carry out under vacuum, and may or will not reduce distillation heat using a series of multi-effect evaporators
It can demand.Distillation can be realized by routine techniques.
In one or more embodiments, water and Extraction solvent are all recycled.This recycling has apparent environment
And economic advantages, and to discharge some manageable but additionally may act as the thick pyrolysis of the remnants of marine diesel oil fuel or boiler oil
Product.
In one or more embodiments, in adverse current is extracted, Extraction solvent enters the top of packed tower and thick fuel
Into the bottom of packed tower.Optionally, in adverse current is extracted, Extraction solvent can enter the bottom of packed tower, and thick fuel
The top of packed tower can be entered.
In one or more embodiments, Extraction solvent extraction impurity makes contaminated Extraction solvent leave packed tower
Bottom and purify the top that fuel leaves packed tower.Optionally, contaminated Extraction solvent may exit off the top of packed tower,
The fuel of purifying leaves the bottom of packed tower.
In one or more embodiments, contaminated Extraction solvent is pumped into another adverse current extraction element, the device
Aromatic compounds, sulphur compound and analog are extracted from Extraction solvent using light fraction nonpolar solvent.
In one or more embodiments, light fraction nonpolar solvent is distilled and is recycled, leave the aromatics of concentration
Compound, sulphur compound and analog and limpid Extraction solvent.
In one or more embodiments, light fraction nonpolar solvent and Extraction solvent are all recycled.
In one or more embodiments, fuel is diesel fuel mixtures.
In one or more embodiments, plastics are to be originally used for recycling, landfill or the waste plastics burned.
In one or more embodiments, converting-plastics are that the pyrolysis processing of thick fuel carries out about 30 minutes at about 450 DEG C
Period.It is understood, however, that any temperature and time that can be pyrolyzed are suitable for the present invention.
In one or more embodiments, the first and second extraction steps substantially environmental pressure, about 80 DEG C and small
Adverse current extraction time section in about 20 minutes occurs.It is understood, however, that any pressure, the temperature that can extract
It is suitable for presently disclosed principle with the period.
In one or more embodiments, this method is suitable for being extended to more than the commercial size of daily 1000 tons of fuel.
In one or more embodiments, this method extends also to pilot plant scale.
In one or more embodiments, this method generates about 70% (w/w) diesel oil peace treaty of per unit plastics
The yield of 15% (w/w) gasoline.However, to a considerable extent, fuel is recycled from waste plastics first by waste plastics
Composition and pyrolysis step carry out condition (temperature, pressure, time) determine.
In one or more embodiments, Extraction solvent is n-methyl-2-pyrrolidone (NMP；CAS872-50-4).
In one or more embodiments, fuel can be transferred directly to the sale of commercial gas station and meet Australia
Diesel fuel quality standard (fuel standard (the automobile bavins in 2001 revised according to the 21st article of fuel quality standard bill in 2000
Oil) measure).
In one or more embodiments, this method is suitable for the economically beneficial oil down to about 16 Australian Dollars/bucket.So
And, it is to be understood that the refinement with this method and raising efficiency, every barrel of profitability also can accordingly increase.
In one or more embodiments, the waste product obtained after recycling Extraction solvent be suitable as boiler oil or
Marine diesel oil, or can store.
In one or more embodiments, Extraction solvent purification step includes that contaminated one or more Extraction solvents exist
Enter climbing film evaporator between about -80kPa to -90kPa.
The method of 4th and/or the 5th aspect can be exported by the kiln of the first, second or third aspect, system or assembly
Thick fuel on carry out.
The 6th aspect in, provide it is a kind of using according to the 4th or the 5th aspect limit method obtain diesel oil mix
Object fuel.In one or more embodiments, which can be transferred directly to the sale of commercial gas station, and meet the big profit of Australia
The sub- diesel fuel quality standard (fuel standard (automobiles in 2001 revised according to the 21st article of fuel quality standard bill in 2000
Diesel oil) measure) and ASTMD975-15c and EN590 standards.
7th aspect provides a kind of one kind of the recycling obtained using the method limited according to the 4th or the 5th aspect
Or a variety of Extraction solvents.
In one or more embodiments, it is found that one or more Extraction solvents of recycling have enough purity to allow
It is reused in other one or many repetitions of processes disclosed herein.
Description of the drawings
The embodiment of the kiln of the disclosure is only described in an illustrative manner with reference to the drawings, wherein：
Fig. 1 is for the schematic diagram by converting-plastics for the system of hydrocarbon fuel；
Fig. 2 is the schematic diagram of the embodiment of the method for obtaining fuel by plastics；
Fig. 3 indicates process identical with the process described in Fig. 2, wherein showing other nmp solvent purifying step；
Fig. 4 is the schematic diagram of another embodiment of the method for obtaining fuel by plastics；
Fig. 5 indicates process identical with the process described in Fig. 4, wherein showing other nmp solvent purifying step；
Fig. 6 is the schematic diagram of the rear end nmp solvent purification process limited in the current some embodiments for disclosing principle；
Fig. 7 is the photo of the thick plastics derivative diesel oil after thick waste plastics pyrolysis；
Fig. 8 is the photo of extraction step；And
Fig. 9 is the final purifying diesel product after NMP extraction steps.
Specific implementation mode
With reference to figure 1, provide a kind of for being hydrocarbon fuel (such as diesel oil, gasoline and liquefied petroleum gas by converting-plastics
(LPG)) system 10.The classification of hydrocarbon fuel depends primarily on the chain length range of hydrocarbon in fuel mixture, such as
Diesel oil hydrocarbon context is usually C10-C25, and gasoline hydrocarbons are C4-C12 and liquefied petroleum gas (LPG) is usual
Including propane (C3H8) and butane (C4H10) mixture.
System 10 includes being supplied to the plastic raw materials 500 of kiln 100.Plastic raw materials 500 can be by long chain organic polymers
Any plastic material formed, such as plastics waste material (such as plastics package or automobile tire).Before introducing kiln 100, modeling
Material raw material 500 can be pre-processed, such as crushed or shredded to improve processing and the surface area of plastic raw materials, or it is dry so that
The water of introducing system minimizes.By feeder 120 by plastic raw materials 500 to reduce heat from kiln and gas loss
Mode is supplied to the feed inlet 110 of kiln 100.It is, for example, possible to use double sliding door formula feeder or plug feeding screw are by plastics
Raw material 500 is fed into feed inlet 110.Feeder 120 also allows control into the flow velocity of the plastic raw materials 500 of kiln 100.
Kiln 100 is the reative cell 130 and heater for including central inner pipe form, and plastic raw materials 500 flow through central inner pipe,
Heater includes the heat source 800 for heating reative cell.Reative cell 130 include installed at a right angle with horizontal rotation shaft 150 it is more
A blender 140, the plastic raw materials that blender 140 is used to be stirred to react in room 130.It conducts heat in addition to improving to plastic raw materials 500
Except, Stirring device 140 also contributes to remove discarded granular materials from reative cell 130 and prevents wax from accumulating in reaction
On 130 inner wall of room.
Heat source 800 can be for heating reative cell 130 and its content (for example through concentric outerhose 160 and reative cell
The heat source medium of annular space between 130) any suitable heat source, heat passes through reative cell 130 by heat source medium 800
Outer wall.Heat source medium 800 can derive from the other processing equipments for using or being used in combination with the system within the system, example
If heat source medium 800 can be the burning gases from vortex burner 170, burning gases are used to handle useless from system
Object, such as on-condensible gas and coke.The outer wall of reative cell 130 further includes multiple vortex generator (not shown) to increase heat source medium
Heat transference efficiency between 800 and reative cell 130.
In reative cell 130, plastic raw materials 500 are heated in the absence of oxygen, so that plastic raw materials 500 are extremely
A few part melts first, then resolves into reative cell gaseous product flow 501, which includes from hydrogen to weight wax
Hydrocarbon, wherein most gas is within the scope of liquid fuel.It can further provide for being catalyzed in reative cell 130
Agent, such as activated alumina, for the hydrocarbon for pushing it is expected chain length to and/or required aromatic hydrocarbon will be reacted.
As plastic raw materials 500 are heated, the useless granular materials such as coke, dust and ash can also be formed in reative cell 130, or
It can be concomitantly introduced into plastic raw materials 500.The kiln is provided with useless particle outlet 180, and give up particle outlet 180 and reative cell 130
It is in fluid communication, to remove at least part of the useless granular materials formed in the reaction chamber.
Kiln 100 further includes product exit 190 and the washer 200 at product exit 190.Reative cell gaseous product flow
501 leave reative cell 130 by product exit 190 and flow through washer 200.It is understood that leaving the gas of reative cell
Body product stream 501 can also include a part of above-mentioned useless granular materials.Washer 200 is preferably comprising plate ring shape filler
Stuffing washing tower.In washer 200, reative cell gaseous product flow 501 is set to be contacted with hydrocarbon cleaning solution 502, with cold
Heavier, higher hydrocarbon present in solidifying reative cell gaseous product flow 501, wherein the hydrocarbon condensed
It flow back into reative cell with cleaning solution and is further reacted.The hydrocarbon of remaining lighter weight is as washer gas
Body product stream 503 leaves washer.Cleaning solution 502 is additionally operable to wash the reative cell gaseous product flow 501 of useless particulate matter, this is anti-
Room gaseous product flow 501 is answered to flow back to reative cell 130 together with cleaning solution 502 and the heavier hydrocarbon of condensation.
It is to be appreciated that washer 200 and 130 in direct fluid communication of reative cell, so as to leave the anti-of reative cell 130
Room gaseous product flow 501 is answered to flow directly into washer 200.This is by reative cell gaseous product flow 501 before entering washer 200
Any cooling minimum of solid waxy residue can be resulted in, which is deposited on connection reative cell 130
In the conduit of washer 200.The above-mentioned relative positioning of reative cell 130 and washer 200 further avoids to isolate
The hydrocarbon that needs and reheat the demand of the product from reative cell 130.
System 10 further comprises at least one carbon for recycling the hydrocarbon in predetermined hydrocarbon context
Hydrogen compound retracting device.In the system 10 of Fig. 1, provide for recycling each of the hydrocarbon gas product stream generated in kiln
Multiple hydrocarbon retracting devices of kind component, are explained in detail below comprising are configured to condensation diesel range
Hydrocarbon fractionating column 210, be configured to condensation gasoline-range hydrocarbon condenser 240 and be configured to
The gas compression and cooling device of the hydrocarbon of condensation liquefaction oil gas (LPG) range.
Washer gaseous product flow 503 is subsequently into fractionating column 210, wherein washer gaseous product flow 503 and hydrocarbonization
504 contact of object reflux is closed, hydrocarbon reflux 504 is selected for that diesel range hydrocarbon 506 is made to condense and flows
Go out 210 bottom of fractionating column, and gasoline and light hydrocarbon leave the top of fractionating column 210 as fractionation gaseous product flow 505
Portion.The part for leaving the diesel range hydrocarbon 506 of fractionating column 210 is used as washing reaction room gaseous product flow 501
Cleaning solution 502.
Then remaining diesel oil 507 can be handled before being stored into Diesel oil storage container.In one example, example
Remaining diesel oil 507 is such as handled to remove moisture by vacuum drying 220, and the diesel oil of processing 508 is collected and stored in
In diesel oil storage container 230.In another example, diesel oil can undergo solvent extraction processing, as described in more detail below, with
Extraction such as aromatic compounds, the impurity of sulphur compound and analog.
It should be understood that the operating condition of kiln 100 and washer 200 depends on the class of pending plastic raw materials 500
Type and desired hydrocarbon product to be recycled.For example, the target of the hydrocarbon of light-weight liquefied petroleum gas (LPG) range
Recycling needs the operation temperature in kiln higher than the temperature of the hydrocarbon of target recycling diesel range.Although the temperature in kiln 100
Spend critically important, but carefully control products export 190 (i.e. washer entrance) and the temperature in washer exit can produced finally
It plays an important role in product composition.It can be for example by controlling temperature and/or the control entrance of wash liquid 502 in reative cell 130
The flow velocity of washer 200 controls these temperature.Preferably, the temperature for leaving the washer gas stream 503 of washer is maintained
At 350 DEG C hereinafter, so that be not suitable for use in the weight of fuel long chain hydrocarbon condense and flow back to reative cell 130 for into
The processing of one step.
The fractionation gaseous product flow 505 for leaving fractionating column 210 flows through condenser 240, and condenser 240 is configured to condensation point
Evaporate the gasoline-range hydrocarbon 504,509 in gaseous product flow 505.It is hydrocarbon using the condensation gasoline-range for leaving condenser
Hydrocarbon reflux 504 of the part for compound as fractionating column 210.It collects remaining gasoline 509 and is stored
In petrol storage container 250.As described in above for diesel oil 507, gasoline 509 can in being stored in petrol storage container it
Before handled.For example, gasoline 509 can undergo solvent extracting process, as described in more detail below, with extraction such as aromatics
Close the impurity of object, sulphur compound and analog.
There is no any residual gas (i.e. due to low-down molecular weight and low boiling point) conduct of condensation in condenser 240
Condenser-air product stream 510 leaves condenser 240.Condenser-air product stream 510 is supplied to gas compression and cooling dress
In setting 260, gas compression and cooling device 260 are configured to extract liquefied petroleum gas from condenser-air product stream 510
(LPG) hydrocarbon of range.The hydrocarbon 511 for the LPG ranges extracted, which is collected and is stored in LPG storages, to be held
In device 270.
The non-condensable gas 512 not recycled in gas compression and cooling device 260 can be used for other processing equipments
In, such as at least partly vortex burner 170 fuels as described above.
Fig. 2 in referring now to the drawings provides the schematic diagram of the technique indicated according to fourth aspect.This aspect defines
Method for obtaining fuel from plastics, this method include that a certain amount of plastics is made to carry out the preliminary of pyrolysis processing (not shown)
Step is gas-oil (1) in this case to be thick fuel by least part converting-plastics.Converting-plastics are thick combustion
The pyrolysis processing of material carries out about 30 minutes periods at about 450 DEG C.
It is understood that pyrolysis processing can be it is above-mentioned with reference to kiln 100 describe, wherein thick fuel is grasped by kiln 100
Make any hydrocarbon fuel stream generated, such as diesel oil 507, gasoline 509.
The technique includes the first extraction step of the fuel for obtaining the form that can be used directly in the following manner：First extraction
Step includes that adverse current liquid-liquid extraction is carried out in packed tower (2) using one or more Extraction solvents (3), and Extraction solvent is preferred
In the form of n-methyl-2-pyrrolidone (NMP).NMP from thick fuel for extracting one or more impurity.The diesel oil of purifying
(4) it is obtained from the discharge stream from the top or bottom of packed tower (2).
Then this method includes the second extraction step, which includes adverse current extraction by the first extraction step
(5) the contaminated NMP obtained.Second extraction step includes contaminated to increase using or mixtures thereof water, ethyl alcohol etc. (6A)
Extraction solvent polarity, and then make Extraction solvent repel extract.Second reverse flow step also occur in packed tower (7) and
Generate the discharge stream of pollutant (8A) discharge stream of such as sulphur compound, aromatic compounds and the nmp solvent (9) of water pollution.
Solvent purification step is optionally extracted, wherein being by the purifying of contaminated Extraction solvent can be subsequent
One or more extraction steps in reuse；This will be further explained below.
Adverse current of first and second extraction steps under substantially environmental pressure, at about 80 DEG C and less than about 20 minutes carries
The period is taken to carry out.
In last step, the nmp solvent (9) of standard destilling tower (10) distillation water pollution is then used, is generated again
The NMP (12) of recirculated water (11A) and recycling.The waste product obtained after recycling Extraction solvent is suitable as boiler oil or ship
Use diesel oil.
It is understood that extraction purification diesel oil (4) carries out in the first extraction step, the second extraction step and subsequent
Distilation steps are used to provide the means of recycling NMP and aqueous solvent.
This method is suitable for extending to the commercial size more than daily 1000 tons of fuel.However, during expansion scale,
This method also extends to pilot-scale.
This method generates the production of about 70% (w/w) diesel oil and about 15% (w/w) gasoline of per unit plastics
Rate.However, to a large extent, recycle from waste plastics fuel first by waste plastics form and pyrolysis step carries out
Condition (temperature, pressure, time) determines.
Diesel fuel after purification can be converted into the sale of commercial gas station, and meet Australian diesel oil combustion
(fuel standard (motor vehicle diesel) surveys in 2001 revised according to the 21st article of fuel quality standard bill in 2000 of material quality standard
It is fixed).
It is understood that the technique described according to fig. 3 is substantially identical as the technique of Fig. 2, wherein carrying out other carry
Take solvent purification step.
In general, it has been discovered that there are serious pollutants in Extraction solvent (NMP), the pollutant is except through one
It will not be removed other than a or multiple intentional purification steps.It has been discovered that pollutant can be one kind that boiling point is higher than NMP
Or a variety of heavy hydrocarbons.Therefore, can by other simple distillation step that is as shown in Figure 6 and illustrating below come
Purify NMP.
In order to complete, about Fig. 4 of attached drawing, the schematic diagram of the technique indicated according to the 5th aspect is provided.Subsequent
In the description of second aspect, had been assigned unanimously with the action or reagent that those of reference is equal in fourth aspect (Fig. 2 and Fig. 3)
Title, such as NMP (3) etc..
5th aspect define it is a kind of for from plastics obtain fuel method, this method include make a certain amount of plastics into
The earlier step of row pyrolysis processing (not shown), to convert at least part of plastics to thick fuel, in this case
It is gas-oil (1).Converting-plastics are the period that the pyrolytic process of thick fuel carries out about 30 minutes at about 450 DEG C.
The technique includes the first extraction step of the fuel for obtaining the form that can be used directly in the following manner：First extraction
Step is included in packed tower (2) carries out adverse current liquid-liquid extraction using one or more Extraction solvents (3), one or more to carry
Take solvent (3) preferably in the form of n-methyl-2-pyrrolidone (NMP).NMP is one or more miscellaneous for being extracted from thick fuel
Matter.The diesel oil (4) of purifying is obtained from the discharge stream from the top or bottom of packed tower (2).
Then this method includes the second extraction step, which includes adverse current extraction by the first extraction step
(5) the contaminated NMP obtained.Second extraction step includes being got dirty using or mixtures thereof hexane, heptane etc. (6B) to change
The polarity of the Extraction solvent of dye, and then Extraction solvent is made to repel extract.Second reverse flow step also occurs in packed tower (7) simultaneously
And generate the discharge stream of such as hexane and heptane impurity pollutant (8B).
First and second extraction steps substantially environmental pressure, about 80 DEG C and less than about 20 minutes adverse current extraction when
Between carry out under section.
In the final step, standard destilling tower (10) is then used to distill contaminated nmp solvent (9), generation follows again
The NMP (12) of the hexane/heptane (11B) and recycling of ring.The waste product obtained after recycling Extraction solvent is suitable as boiler
Fuel or marine diesel oil.
It is understood that it is substantially the same with the technique of Fig. 4 according to the technique that Fig. 5 is described, wherein carrying out other carry
Take solvent purification step.
In general, it has been discovered that there are heavy contaminant in Extraction solvent (NMP), the pollutant except through one or
It will not be removed other than multiple intentional purification steps.It has been discovered that pollutant can be one kind or more that boiling point is higher than NMP
Kind heavy hydrocarbon.It therefore, can be by other simple distillation step that is as shown in Figure 5 and illustrating below come pure
Change NMP.
It is used for contaminated Extraction solvent is pure referring now to Figure 6, providing individually (or embedded) device, the device
Change the purity level that can be extremely reused in the successive iterations of the technique.
In purifying step shown in Fig. 6, the contaminated NMP (12) with contaminant remaining enter it is overall by steam or
The climbing film evaporator (D) of heat-transfer oil (13) heating.Climbing film evaporator is in vacuum state in the sides NMP.Generally, vacuum condition will
Between about -80kPa to -90kPa.Generally, the temperature of climbing film evaporator will be controlled as promoting NMP under required vacuum
Boiling.NMP leaves heavy contaminant and the condensation in NMP vacuum condensers (E) as NMP steam (14) evaporation.Heavy contaminant
(17) climbing film evaporator is left to refine as industry heating fuel or further.Then the NMP (16) of recycling and purifying is returned
To the successive iterations of extracting method.
About it is above-mentioned it is each in terms of, it should be understood that purifying diesel oil (4) extraction carried out in the first extraction step,
Second extraction step and subsequent distilation steps are used to provide the means of recycling NMP and aqueous solvent.
This method is suitable for being extended to more than the commercial size of daily 1000 tons of fuel.However, during expansion scale, it should
Method also extends to pilot-scale.
This method generates the production of about 70% (w/w) diesel oil and about 15% (w/w) gasoline of per unit plastics
Rate.However, to a considerable extent, fuel is recycled from waste plastics first by the item of waste plastics formed and pyrolysis step carries out
Part (temperature, pressure, time) determines.Diesel fuel after purification can be converted directly into the sale of business gas station, and meet
Australian diesel fuel quality standard is (according to fuel standards in 2001 of the 21st article of revision of fuel quality standard bill in 2000
(motor vehicle diesel) measures).
The thick plastics that Fig. 7 describes after thick waste plastics pyrolysis derive diesel samples.Apparent feature is black and opaque.This
Kind crude product is not suitable for the commercial distribution of gas station.Fig. 8 is the photo of extraction step, wherein NMP is mixed with sample and makes it
It is deposited to bottom.Impurities/contaminant is dissolved into NMP；The relatively limpid layer for staying in top is relatively pure diesel oil.Fig. 9 is retouched
The sample of the final purifying diesel product after NMP extraction steps is stated.As pointed by elsewhere, which can be with
It is directly changed into the sale of business gas station, and meets Australian diesel fuel quality standard (according to fuel mass in 2000
Fuel standard (motor vehicle diesel) measurement in 2001 of the 21st article of revision of standard bill) and ASTM D975-15c and EN590 marks
It is accurate.
It is understood that the above method waste plastics is converted to by way of purifying diesel fuel it is commercially useful
Form.Moreover, The inventive process provides the means for recycling any solvent used in this extraction process.
It, can be with it will be appreciated by those skilled in the art that in the case where not departing from the broad sense general range of the disclosure
Many variations and/or modification are made to above-described embodiment.Therefore, the present embodiment be regarded as in all respects it is illustrative rather than
It is restrictive.
Claims (44)
1. a kind of by the kiln used in plastics-production hydrocarbon fuel, the kiln includes：
Reative cell；
Feed inlet, plastic raw materials for being supplied in the reative cell by the feed inlet；
Heater, the heater is for heating the reative cell；And
Washer, the washer and the reative cell in direct fluid communication；
The wherein described kiln is configured to make the plastic raw materials in the reative cell to be heated there is no oxygen, by
At least part of the plastic raw materials is resolved into the reative cell gas comprising the hydrocarbon for being suitable as fuel and produced by this
Logistics, and
The wherein described washer is configured to make in the reative cell gaseous product flow higher than predetermined upper hydrocarbon context
Hydrocarbon removal is further heated with returning it to the reative cell there is no oxygen.
2. kiln according to claim 1, wherein the temperature for leaving the reative cell gaseous product flow of the reative cell exists
Do not decline substantially before into the washer.
3. kiln according to claim 1 or 2, wherein the washer is configured to make to leave the washer gas of the washer
Body stream is in the temperature less than 350 DEG C.
4. kiln according to any one of the preceding claims, wherein the kiln is to include the cylindrical horizontal of cylindrical shell
Kiln, and the reative cell includes the inner tube being concentrically positioned in the cylindrical shell.
5. kiln according to claim 4, wherein the heater includes hot-fluid medium, the hot-fluid medium is at the center
It is flowed in the annular space limited between inner tube and the shell, so that the outer surface of heat source medium heating said inner tube.
6. kiln according to claim 5, the wherein outer surface of said inner tube include being situated between for increasing from the heat source
Multiple vortex generators of the matter to the heat transfer efficiency of the reative cell.
7. kiln according to any one of the preceding claims further comprises for stirring the modeling in the reative cell
Expect the blender of raw material.
8. kiln according to any one of the preceding claims further comprises the catalyst in the reative cell.
9. kiln according to any one of the preceding claims further comprises for removing particulate material of giving up from the reative cell
Useless particle outlet.
10. a kind of system for by plastics-production hydrocarbon fuel, the system comprises according to any one of preceding claims
The kiln.
11. system according to claim 10 further comprises hydrocarbon in predetermined hydrocarbon context for recycling
At least one hydrocarbon retracting device of compound.
12. system according to claim 11, wherein during at least one hydrocarbon retracting device is following
It is one or more：It is configured to condense the fractionating column of the hydrocarbon of the diesel range from hydrocarbon fuel streams；Configuration
Condenser for the hydrocarbon for condensing the gasoline-range from hydrocarbon fuel streams；And/or it is configured to condensation and comes
From the compression set of the hydrocarbon of liquefied petroleum gas (LPG) range of hydrocarbon fuel streams.
13. system according to claim 12, wherein the fractionating column is connected to the gas outlet stream of the washer.
14. system according to claim 13, wherein the fractionating column is further configured to condense at least part
Diesel oil be transferred to the washer for use as cleaning solution.
15. according to the system described in any one of claim 12-14, further comprise for from being condensed by the fractionating column
The vacuum column of water removal is removed in the hydrocarbon of the diesel range.
16. according to the system described in any one of claim 12-15, wherein the gas of the condenser and the fractionating column goes out
Mouth is in fluid communication.
17. according to the system described in any one of claim 12-16, wherein the gas of the compression set and the condenser
Communication.
18. a kind of by the assembly used in plastics-production hydrocarbon fuel, the assembly includes：
Kiln, the kiln include：
Reative cell；
Feed inlet, plastic raw materials for being supplied in the reative cell by the feed inlet；And
Heater, the heater is for heating the reative cell；
The wherein described kiln is configured to make the plastic raw materials in the reative cell to be heated there is no oxygen, by
At least part of the plastic raw materials is resolved into the reative cell gas comprising the hydrocarbon for being suitable as fuel and produced by this
Logistics,
Washer, the washer is in fluid communication with the reative cell, wherein the washer is configured to make the reative cell
Hydrocarbon in gaseous product flow higher than predetermined upper hydrocarbon context removes and makes removed hydrocarbonization
It closes object and returns to the reative cell for further being heated there is no oxygen；And
Hydrocarbon retracting device, the hydrocarbon retracting device are connected to described anti-to receive with the washer fluid
The remainder of room gaseous product flow, the hydrocarbon retracting device is answered to be configured to remove from the remainder pre-
Determine the hydrocarbon in hydrocarbon context.
19. a kind of method obtaining fuel from plastics, the method includes making a certain amount of plastics carry out pyrolysis processing, thus
Convert at least part of the plastics to thick fuel；And the fuel of directly available form is extracted in the following manner：
First extraction step, first extraction step include carrying out adverse current liquid-liquid extraction using one or more Extraction solvents
To extract one or more impurity from the thick fuel；
Second extraction step, second extraction step include adverse current extraction obtained by first extraction step it is contaminated
One or more Extraction solvents；And
Optionally Extraction solvent purification step, wherein by contaminated one or more Extraction solvent purifying to realize rear
Solvent reuses described in continuous one or more extraction steps.
20. according to the method for claim 19, wherein second extraction step includes using water, ethyl alcohol etc. or its mixing
Object changes the polarity of the contaminated Extraction solvent, and then the Extraction solvent is made to repel extract；Then it is carried from described
It takes and distills out one or more polar compounds in solvent.
21. according to the method for claim 19, wherein second extraction step is carried including use from the Extraction solvent
Take the light fraction nonpolarity of or mixtures thereof such as heptane, hexane of aromatic compounds and the compound with similar polarity molten
Agent；Then the light fraction solvent is distilled from the Extraction solvent.
22. according to the method described in any one of claim 19-21, wherein the Extraction solvent is N- methyl -2- pyrrolidines
Ketone or similar dipolar aprotic solvent, such as dimethylformamide, dimethyl sulfoxide (DMSO) etc..
23. according to the method described in any one of claim 19-22, wherein extracting solvent purification step.
24. carrying out according to the method for claim 23, including in a substantial continuous manner the Extraction solvent purifying step
Suddenly to provide the substantially continuous operation of the described first and/or second extraction step.
25. the method according to claim 19 or 20, wherein in adverse current extraction, the Extraction solvent enters filler
The top of tower and the thick fuel enter the bottom of the packed tower.
26. according to the method for claim 25, wherein the Extraction solvent extract impurity, make contaminated Extraction solvent from
It opens the bottom of the packed tower and purifies the top that fuel leaves the packed tower.
27. according to the method for claim 26, wherein or mixtures thereof described contaminated Extraction solvent and water, ethyl alcohol etc.
Mixing so that as the non-polar compound of aromatic compound comes out from solution.
28. according to the method for claim 27, wherein impurity compound is flowed out from the Extraction solvent being polluted by water.
29. according to the method for claim 28, wherein using conventional climbing film evaporator by water from the Extraction solvent
It distills.
30. according to the method for claim 29, wherein the water and the Extraction solvent are all recycled.
31. the method according to claim 19 or 21, wherein in adverse current extraction, the Extraction solvent enters filler
The top of tower, and the thick fuel enters the bottom of the packed tower.
32. according to the method for claim 31, wherein the Extraction solvent extracts impurity, keep the contaminated extraction molten
Agent leaves the bottom of the packed tower and purifies the top that fuel leaves the packed tower.
33. according to the method for claim 32, being extracted wherein the contaminated Extraction solvent is pumped into another adverse current
Device, described device extract aromatic compounds, sulphur compound and class using light fraction nonpolar solvent from the Extraction solvent
Like object.
34. according to the method for claim 33, wherein the light fraction nonpolar solvent is distilled and recycles, leaving
Aromatic compounds, sulphur compound and the analog and limpid Extraction solvent of concentration.
35. according to the method for claim 34, wherein the light fraction nonpolar solvent and the Extraction solvent are all by again
Cycle.
36. according to the method described in any one of claim 19-35, wherein the fuel is diesel fuel mixtures.
37. according to the method described in any one of claim 19-36, wherein the converting-plastics are the described of the thick fuel
Pyrolysis processing carries out about 30 minutes periods at about 450 DEG C.
38. according to the method described in any one of claim 19-37, wherein first extraction step and second extraction
Step is under substantially environmental pressure, about 80 DEG C and the adverse current extraction time section generation less than about 20 minutes.
39. according to the method for claim 19, wherein the Extraction solvent is n-methyl-2-pyrrolidone (NMP).
40. according to the method described in any one of claim 19-39, wherein what is obtained after recycling the Extraction solvent is useless
Product is suitable as boiler oil or marine diesel oil, or can store.
41. according to the method described in any one of claim 19-40, wherein the Extraction solvent purification step include it is described by
One or more Extraction solvents of pollution enter climbing film evaporator between about -80kPa to -90kPa.
42. according to the method described in any one of claim 19-40, wherein the thick fuel is use according to claim 1-
Kiln described in any one of 9, the system according to any one of claim 10-17 or according to claim 18 total
At the hydrocarbon fuel of processing obtained by plastics.
43. the diesel blended fuel obtained using the method according to any one of claim 19-42.
44. one or more extractions using the recycling of the method acquisition according to any one of claim 19-42 are molten
Agent.
Applications Claiming Priority (7)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2015904828 | 2015-11-23 | ||
| AU2015904828A AU2015904828A0 (en) | 2015-11-23 | Kiln for use in the production of hydrocarbon fuels from plastics | |
| AU2016901654 | 2016-05-05 | ||
| AU2016901654A AU2016901654A0 (en) | 2016-05-05 | Plastics-derived fuels and methods of making same | |
| AU2016902869 | 2016-07-21 | ||
| AU2016902869A AU2016902869A0 (en) | 2016-07-21 | Plastics-derived fuels and methods of making same II | |
| PCT/AU2016/051144 WO2017088015A1 (en) | 2015-11-23 | 2016-11-23 | Production of hydrocarbon fuels from plastics |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108291150A true CN108291150A (en) | 2018-07-17 |
Family
ID=58762856
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201680068435.7A Pending CN108291150A (en) | 2015-11-23 | 2016-11-23 | By plastics-production hydrocarbon fuel |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20180355256A1 (en) |
| EP (1) | EP3380583A4 (en) |
| CN (1) | CN108291150A (en) |
| AU (1) | AU2016358310A1 (en) |
| WO (1) | WO2017088015A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113795712A (en) * | 2019-03-07 | 2021-12-14 | 瑞菲尼缇有限公司 | Process for upgrading pyrolysis oil and upgrading solution used therein |
Families Citing this family (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AR110493A1 (en) | 2016-12-08 | 2019-04-03 | Shell Int Research | A METHOD FOR PRE-TREAT AND CONVERT HYDROCARBONS |
| US20190344771A1 (en) * | 2018-05-11 | 2019-11-14 | Ethan J. Novek | Systems and methods for preventing fouling of marine structures |
| SG11202110307RA (en) | 2019-04-18 | 2021-11-29 | Shell Int Research | Recovery of aliphatic hydrocarbons |
| FR3095450B1 (en) * | 2019-04-25 | 2023-07-21 | Earth Wake | DEVICE AND METHOD FOR THE TREATMENT OF MATERIALS IN PARTICULAR PLASTICS |
| FI20195446A1 (en) | 2019-05-28 | 2020-11-29 | Neste Oyj | Alkali-enhanced hydrothermal purification of plastic pyrolysis oils |
| US11180699B1 (en) * | 2019-07-01 | 2021-11-23 | Gen Tech PTD, LLC | System and method for converting plastic into diesel |
| CN110643375A (en) * | 2019-09-10 | 2020-01-03 | 宁夏凯铭瑞环保科技有限公司 | Novel vertical retort of active carbon |
| KR20220117901A (en) | 2019-12-23 | 2022-08-24 | 셰브런 유.에스.에이.인크. | Circular Economy of Plastic Waste to Polyethylene and Lubricants with Crude Oil and Isomerization Dewaxing Units |
| GB2590525B (en) * | 2020-08-14 | 2022-08-31 | Clean Planet Energy | Commercial grade ultra-low sulphur diesel production process from mixed waste plastics pyrolysis oil |
| WO2022079060A1 (en) | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
| WO2022079057A1 (en) | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
| WO2022079025A1 (en) | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
| CN116348572A (en) | 2020-10-16 | 2023-06-27 | 国际壳牌研究有限公司 | Recovery of aliphatic hydrocarbons |
| KR20230086710A (en) | 2020-10-16 | 2023-06-15 | 쉘 인터내셔날 리써취 마트샤피지 비.브이. | Recovery of aliphatic hydrocarbons |
| WO2022079046A1 (en) | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
| JP2023546122A (en) | 2020-10-16 | 2023-11-01 | シエル・インターナシヨナル・リサーチ・マートスハツペイ・ベー・ヴエー | Recovery of aliphatic hydrocarbons |
| WO2022079012A1 (en) | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
| CN116529342A (en) | 2020-11-13 | 2023-08-01 | 国际壳牌研究有限公司 | Recovery of aliphatic hydrocarbons |
| CN116438281A (en) | 2020-11-13 | 2023-07-14 | 国际壳牌研究有限公司 | Recovery of aliphatic hydrocarbons |
| US20230016539A1 (en) | 2021-07-01 | 2023-01-19 | Shell Usa, Inc. | Treatment of plastic-derived oil |
| WO2023285472A2 (en) * | 2021-07-13 | 2023-01-19 | Indaver Plastics2Chemicals | "method for producing purified fractions of a liquid crude pyrolysis oil from a hydrocarbon based waste plastic" |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4983278A (en) * | 1987-11-03 | 1991-01-08 | Western Research Institute & Ilr Services Inc. | Pyrolysis methods with product oil recycling |
| US20090200208A1 (en) * | 2007-02-26 | 2009-08-13 | Gabriel Farkas | Method of producing mineral oils based on hydrocarbon distillates |
| CN101906317A (en) * | 2010-08-09 | 2010-12-08 | 华中科技大学 | Method for preparing environment-friendly aromatic oil from catalytic cracking slurry oil |
| US20140228606A1 (en) * | 2013-02-12 | 2014-08-14 | Saudi Basic Industries Corporation | Conversion of plastics to olefin and aromatic products with product recycle |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4589973A (en) * | 1985-07-15 | 1986-05-20 | Breckinridge Minerals, Inc. | Process for recovering oil from raw oil shale using added pulverized coal |
| US6657095B1 (en) * | 1998-04-01 | 2003-12-02 | Recycled Energy, L.L.C. | Continuous temperature variance pyrolysis for extracting products from tire chips |
| WO2001094498A1 (en) * | 2000-06-08 | 2001-12-13 | Valtion Teknillinen Tutkimuskeskus | Method and apparatus for producing pyrolysis oil |
| US6451197B1 (en) * | 2001-02-13 | 2002-09-17 | Uop Llc | Process for hydrocracking a hydrocarbonaceous feedstock |
| WO2011034989A2 (en) * | 2009-09-16 | 2011-03-24 | Envion, Inc. | Decomposition of waste plastics |
| US20140336427A1 (en) * | 2013-05-09 | 2014-11-13 | Uop Llc | Methods of and apparatuses for upgrading a hydrocarbon stream including a deoxygenated pyrolysis product |
-
2016
- 2016-11-23 WO PCT/AU2016/051144 patent/WO2017088015A1/en active Application Filing
- 2016-11-23 US US15/778,587 patent/US20180355256A1/en not_active Abandoned
- 2016-11-23 EP EP16867448.9A patent/EP3380583A4/en not_active Withdrawn
- 2016-11-23 AU AU2016358310A patent/AU2016358310A1/en not_active Abandoned
- 2016-11-23 CN CN201680068435.7A patent/CN108291150A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4983278A (en) * | 1987-11-03 | 1991-01-08 | Western Research Institute & Ilr Services Inc. | Pyrolysis methods with product oil recycling |
| US20090200208A1 (en) * | 2007-02-26 | 2009-08-13 | Gabriel Farkas | Method of producing mineral oils based on hydrocarbon distillates |
| CN101906317A (en) * | 2010-08-09 | 2010-12-08 | 华中科技大学 | Method for preparing environment-friendly aromatic oil from catalytic cracking slurry oil |
| US20140228606A1 (en) * | 2013-02-12 | 2014-08-14 | Saudi Basic Industries Corporation | Conversion of plastics to olefin and aromatic products with product recycle |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113795712A (en) * | 2019-03-07 | 2021-12-14 | 瑞菲尼缇有限公司 | Process for upgrading pyrolysis oil and upgrading solution used therein |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2016358310A1 (en) | 2018-06-21 |
| EP3380583A1 (en) | 2018-10-03 |
| WO2017088015A1 (en) | 2017-06-01 |
| US20180355256A1 (en) | 2018-12-13 |
| EP3380583A4 (en) | 2019-07-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108291150A (en) | By plastics-production hydrocarbon fuel | |
| CA2879192C (en) | Hybrid thermal process to separate and transform contaminated or uncontaminated hydrocarbon materials into useful products, uses of the process, manufacturing of the corresponding system and plant | |
| US4618735A (en) | Process and apparatus for the conversion of sludges | |
| EP2435368B1 (en) | Method of production of high-value hydrocarbon products from waste plastics | |
| RU2621097C2 (en) | Device for thermal destruction of waste from polyethylene and polypropylene | |
| RU2496587C2 (en) | Method of organic and polymer wastes processing | |
| CN202576344U (en) | Equipment for extracting oil fuel from sandy oil sludge or/and organic waste | |
| Manickavelan et al. | A review on transforming plastic wastes into fuel | |
| KR20230037052A (en) | Integrated continuous conversion and separation method for upcycling mixed plastic waste to clean gasoline and diesel fuel and other products | |
| EP0678116B1 (en) | Process for recovery of tank bottom wastes | |
| EP2834323A1 (en) | System and method for converting plastic/rubber to hydrocarbon fuel by thermo-catalytic process | |
| EP3312223B1 (en) | Method for thermally decomposing polyethylene and polypropylene waste | |
| US20140130404A1 (en) | System for converting organic materials into oil, fuel and uncondensed vapors utilizing a pyrolysis chamber | |
| US20190177621A1 (en) | Hydrocarbon recycling of carbonizer hot gases | |
| CN103145305A (en) | Process for preparing synthesis gas or synthetic natural gas or synthetic gasoline by utilizing oil-containing sludge and incinerator thereof | |
| AU2021106834A4 (en) | A system for the chemical recycling of end of life plastics to a plastic feedstock and fuel products using a multi-stage pyrolysis kiln | |
| CA2153395C (en) | Process for recovery of tank bottom wastes | |
| KR100508334B1 (en) | Manufacturing Device of Alternative Fuel Oil from Non-Catalytic Pyrolysis Process | |
| RU167118U1 (en) | DEVICE FOR THERMAL DESTRUCTION OF POLYETHYLENE AND POLYPROPYLENE WASTE | |
| US11649403B2 (en) | Multi-step process for conversion of waste plastics to hydrocarbon liquids | |
| WO2017017692A2 (en) | Multi-stage cracking system and process thereof for conversion of non-degradable waste into fuels | |
| RU2766091C1 (en) | Rotor element for use in an ablative pyrolysis reactor, an ablative pyrolysis reactor and a pyrolysis method | |
| KR0182769B1 (en) | Process for recovery of tank bottom wastes | |
| Parku | Pyrolysis of waste polypropylene plastics for energy recovery: Investigation of operating parameters and process development at pilot scale | |
| WO1995013338A1 (en) | Process for recovery of tank bottom wastes |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20180717 |
|
| WD01 | Invention patent application deemed withdrawn after publication |