CN108026452A - Method for mixed waste plastic to be converted into liquid fuel and wax by catalytic cracking - Google Patents
Method for mixed waste plastic to be converted into liquid fuel and wax by catalytic cracking Download PDFInfo
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- CN108026452A CN108026452A CN201680051577.2A CN201680051577A CN108026452A CN 108026452 A CN108026452 A CN 108026452A CN 201680051577 A CN201680051577 A CN 201680051577A CN 108026452 A CN108026452 A CN 108026452A
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- catalyst
- waste plastic
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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
- 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
- C10G11/04—Oxides
- C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
-
- 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
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
-
- 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
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
Abstract
The present invention relates to a kind of method for being used to mixed waste plastic be converted into liquid fuel and wax by catalytic cracking.This method comprises the following steps：Mixed waste plastic and the catalyst comprising zeolite catalyst are introduced in reactor；At least a portion mixed waste plastic is allowed to be converted into liquid fuel and wax in the reactor；And the product stream containing the liquid fuel and wax is removed from the reactor.
Description
This application claims the priority of European application number 15201127.6, which carried on December 18th, 2015
Hand over, be for all purposes incorporated herein the full content of the application by quoting mode.
The present invention relates to a kind of method for being used to mixed waste plastic be converted into liquid fuel and wax by catalytic cracking.Should
Method comprises the following steps：Mixed waste plastic and the catalyst comprising zeolite catalyst are introduced in reactor；In the reaction
At least a portion mixed waste plastic is allowed to be converted into liquid fuel and wax in device；And removed from the reactor containing described
The product stream of liquid fuel and wax.
In view of importance day of the polymer as the substitute of conventional structure material (such as glass, metal, paper and timber)
Benefit increase, the needs being aware of for saving non-renewable resources (such as oil) and the garbage loading embeading available for waste product disposal hold
The decrement of amount, in recent years, considerable concern are directed to recycling, regenerate, recycle or recycling in some way waste plastics
The problem of.
Pyrolysis or catalytic cracking waste plastics has been proposed being converted into heavy polymer with much lower molecule
The volatile compound of amount.Depending on used method, volatile compound can be used as fuel oil or fuel oil supplement
The opposite higher boiling liquid hydrocarbon of agent, or light boiling point as gasoline-type fuel or as other chemicals is to mid-boiling point hydro carbons.
The catalytic cracking of mixed waste plastic is method well known to those skilled in the art.For example, US 5,216,149 is disclosed
It is a kind of to be used to allow to decompose urging for given polymer in the presence of other polymers (decomposing without substantive) by identifying
Agent and temperature conditionss come control the pyrolysis of the complex waste stream of plastics with by this circulation turn to useful high value monomer or its
The method of his chemicals.
K.-H.Lee, et al. in Polymer Degradation and Stability [depolymerization and stability]
The mixture of discarded high density polyethylene (HDPE) and polystyrene is disclosed in 84 (2004) 123-127 through used FCC catalyst
Liquid-phase catalysis degraded.The influence of the mixed proportion of polyethylene and polystyrene is have studied, and ladies and gentlemen author has found reactant
The increase of middle polystyrene content shows in the products therefrom increase of gas and oil ratio and kerosene, diesel oil and wax ratio subtracts
It is few.However, at the same time, the ratio of aromatic components is sharply increased to 70% in product liquid, and more even polystyrene content
For only about 40%.This is found in K.-H.Lee in 93 (2008) 1284- of Polymer Degradation and Stability
It is proved in 1289 publication, wherein the polystyrene content obtained is 40%, or even 90% aromatic hydrocarbons.It is catalyzed using 20g
Agent/200g plastics carry out the experiment reported by K.-H.Lee.
Although for some applications, increasing the ratio of the gasoline obtained from the catalytic cracking of waste plastics, it may be advantageous,
But a high proportion of aromatic compound is probably undesirable, such as the toxicity due to such compound.In addition, should for other
With, for example, commercially to the increasing demand of diesel oil in the case of, the ratio for increasing diesel oil and wax is favourable.Cause
This, it is desirable to provide a kind of method for catalytic cracking waste plastics, wherein obtained gasoline and diesel oil distillate can be customized
Ratio, the ratio without undesirably increasing obtained aromatic compound.
The present invention the inventors discovered that, pass through selection in mixed waste plastic certain ratio polystyrene and polyene
Hydrocarbon and increase the ratio of the catalyst containing zeolite catalyst and waste plastics in the reactor, can unexpectedly solve
This problem and other problems as described below.
Present invention is accordingly directed to a kind of side for being used to mixed waste plastic be converted into liquid fuel and wax by catalytic cracking
Method, this method include：
Mixed waste plastic and the catalyst comprising zeolite catalyst are introduced in reactor；
At least a portion mixed waste plastic is allowed to be converted into liquid fuel and wax in the reactor；And
The product stream containing the liquid fuel and wax is removed from the reactor,
It is characterized in that, the mixed waste plastic contain by weight from 2% to 50% polystyrene and by weight from
50% to 98% polyolefin, is each based on the gross weight of polystyrene and polyolefin in the mixed waste plastic, and its feature
It is, the weight ratio of the catalyst reactor and mixed waste plastic is higher than 1: 10.
In the catalytic cracking of plastics, some cuts of chemical compound are obtained.It typically, there are containing having less than 5
The gas fraction of the lightweight chemical compound of a carbon atom.Gasoline fraction contains the change with low boiling point (such as less than 216 DEG C)
Compound.The cut includes the compound with 5 to 11 carbon atoms.Kerosene and diesel oil distillate have higher boiling point (such as 216
DEG C to 359 DEG C).The cut usually contains the compound with 12 to 21 carbon atoms.Generally will even more high boiling cut
It is named as wax (heavy-cycle oil or HCO).In all cuts, these compounds are hydrocarbon, optionally include hetero atom (such as N, O
Deng)." liquid fuel " in the sense of the present invention therefore it is such as gasoline and diesel oil fuel, it is valuable it is also possible to be used as other
Chemicals or solvent." wax " specifies such hydrocarbon, these hydrocarbon are under room temperature (23 DEG C) for solid and with generally greater than 45 DEG C
Softening point.
Plastics are mainly made of specific polymer, and plastics are usually named by the specific polymer.Preferably, mould
Material containing its gross weight by weight more than 25%, preferably by weight more than 40% and more preferably exceed by weight
50% particular polymers.Other components in plastics are such as additives, as filler, reinforcing agent, processing aid, plasticizer,
Pigment, light stabilizer, lubricant, anti-impact modifier, antistatic additive, ink, antioxidant etc..It is more than in general, plastics include
A kind of additive.
The plastics used in the method for the invention are polyolefin and polystyrene, such as high density polyethylene (HDPE) (HDPE),
Low density polyethylene (LDPE) (LDPE), polypropylene (PP) and polystyrene (PS).The mixing being mainly made of polyolefin and polystyrene
Plastics are preferable.In this context " main composition " should be understood so that in mixed plastic polyolefin and polystyrene
Concentration be by weight higher than 50%, more preferably by weight of from more than 75%, be each based on the gross weights of dry-mixing plastics.
The mixed plastic can be made of polyolefin and polystyrene.The gross weight of dry-mixing plastics is preferably based on, the mixed plastic
Containing being less than 99.5% by weight, 99% polyolefin and polystyrene are more preferably less than by weight.
Other plastics (such as polyvinyl chloride, polyvinylidene chloride, polyethylene terephthalate, polyurethane (PU), third
Alkene nitrile-butadiene-styrene (ABS), nylon and fluorinated polymer etc.) it is not ideal.If present in waste plastics, then they
It is preferred that with the gross weight of dry waste plastics by weight less than 50%, preferably by weight less than 30%, more preferably by weight
Less than 20%, a small amount of presence even more preferably by weight less than 10%.The gross weight of dry waste plastics is preferably based on, is appointed
Why not the independent content of too desired plastics is by weight less than 5%, is more preferably less than 2% by weight.
Preferably, these plastic wastes starting materials include one or more thermoplastic polymers and substantially free of heat
Solidity polymer.15wt% is less than for composition substantially free of the content for being intended to indicate that thermosetting polymer in this respect,
Preferably less than 10wt% and even more preferably less than 5wt%.
In general, waste plastics contains other undesirable components, i.e. foreign material, such as paper, glass, stone, metal etc..
In the context of the present invention, no matter when refer to waste plastics weight or mixed waste plastic in polystyrene and poly-
The weight of alkene, the weight are directed to the weight of dry plastics, are mixed without any foreign material with plastics.However, the weight
Including any component in the plastic, such as additive described above.
The present invention's the inventors discovered that when using catalyst comprising zeolite catalyst, higher than 1：10 it is anti-
Answer in device under the weight ratio of catalyst and mixed waste plastic, polystyrene is added in polyolefin plastics unexpectedly to production
Product distribution, which has, to be significantly affected.With by K.-H.Lee (referring to bibliography cited above) report on the contrary, ladies and gentlemen inventor
It was found that the polystyrene of more height ratio causes the bavin of higher amount in the product stream that is obtained from reactor in mixed waste plastic
Oil and wax.Therefore, method of the invention allows on the relatively high selectivity to diesel oil and wax and the relatively low choosing to gas and gasoline
Select the selectivity for sexually revising product.Such as find when, there are during 15% polystyrene, wax yield is even in mixed waste plastic
Double.
Furthermore, it was found that in the method for the invention, it is (special relative to the increase of saturated compounds concentration and unsaturated compound
It is not aromatic compound) reduction of concentration, diesel quality improved.This be the discovery that it is especially unexpected because adding
Plus polystyrene (polymer based on aromatic hydrocarbons) should result in the unsaturated compound of higher amount and particularly aromatic series
Compound.Meanwhile the gasoline fraction also obtained keeps its high-quality on research octane number (RON) (RON) and motor octane number (MON)
Amount is horizontal.
It was found that the gross weight based on polystyrene in mixed waste plastic and polyolefin, if mixed waste plastic contains by weight
The polystyrene from 2% to 50% is counted, preferably by weight from 2% to 40%, more preferably by weight from 2% to 30%, and
And even more preferably by weight from 2% to 20% polystyrene, then realize above advantage.Most preferably, it is useless based on mixing
The gross weight of polystyrene and polyolefin in plastics, mixed waste plastic contain by weight from 2% to 15%, such as by weight
From 5% to 15% polystyrene.
The method of the present invention is further characterized in that the weight ratio of catalyst reactor and mixed waste plastic is higher than 1: 10.It is excellent
Selection of land, the weight ratio of catalyst and mixed waste plastic is higher than 1: 9 in the reactor, and more preferably above 1: 8, more preferably above
1: 7, more preferably above 1: 6, more preferably above 1: 5, more preferably above 1: 4, and even more preferably higher than 1: 3,
Such as higher than 1: 2.The weight ratio of particularly preferred catalyst in the reactor and mixed waste plastic is about 1: 1.5.
The weight ratio of catalyst and mixed waste plastic can be less than 10: 1 in the reactor, be preferably lower than 7: 1.Therefore,
In the reactor the weight ratio of catalyst and mixed waste plastic can be for example from 1: 9 to 10: 1, preferably from 1: 8 to 10: 1,
It is preferred that from 1: 7 to 10: 1, preferably from 1: 6 to 10: 1, preferably from 1: 5 to 10: 1, preferably from 1: 4 to 10: 1, preferably from 1: 3 to 10
: 1, and even more preferably from 1: 2 to 10: 1 or in the range of 1: 2 to 7: 1.
The catalyst used in the method for the invention includes zeolite catalyst.In one embodiment, the catalyst
Mainly zeolite catalyst.In a further embodiment, which is made of zeolite catalyst.In the 3rd embodiment
In, which includes other catalyst in addition, particularly amorphous type catalyst.
The embodiment that wherein catalyst is mainly zeolite catalyst is preferable.In this context, term is " main
Ground " defines the catalyst for the mixture for being zeolite catalyst and Non-zeolite catalysts (such as amorphous type catalyst),
But the wherein gross weight based on catalyst, the catalyst include the zeolite catalyst by weight more than 50%.Preferably, should
Catalyst, which includes, is more than 60%, more preferably more than 70%, is still more preferably greater than 80% and most preferably more than 90%
Zeolite catalyst.The catalyst can include the mixed of single zeolite catalyst or two or more zeolite catalysts
Compound.
As catalyst, all types of FCC catalysts can be used.FCC catalyst is for those skilled in the art
It is well known.For example, zeolite catalyst can be selected from well known by persons skilled in the art and commercially available crystalline microporous zeolite.Boiling
The preferred embodiment of stone-type catalyst is described in WO 2010/135273, its content is incorporated herein by quoting mode.Properly
The instantiation of zeolite catalyst include but not limited to：ZSM-5、ZSM-11、ZSM-22、ZSM-23、ZSM-35、ZSM-
48th, ZSM-50, TS-1, TS-2, SSZ-46, MCM-22, MCM-49, FU-9, PSH-3, ITQ-1, EU-1, NU-10, silicone zeolite-
1st, silicone zeolite -2, borosilicate zeolite-C, borosilicate zeolite-D, BCA and its mixture.
If the catalyst additionally comprises amorphous type catalyst, i.e., this can include silica, aluminium oxide, kaolinite
Soil or its mixture.Silica (especially in the form of sand) is well known for FCC catalytic applications.Preferable nothing
Setting type catalyst includes by weight at least 60%, preferably by weight at least 70% and even more preferably by weight extremely
The few 80% oxidized compound (such as silica (SiO based on silicon2), kaolin etc.) silica equivalent.
The catalyst can be fresh catalyst, equilibrium catalyst (such as used catalyst) or its mixture.
Mixed waste plastic and catalyst comprising zeolite catalyst can be subsequently or simultaneously introduced in reactor.This
Outside, by mixed waste plastic and catalyst in increments comprising zeolite catalyst or can be introduced continuously into reactor.
Technical staff knows the suitable instrument and equipment for carrying out the method according to the invention, and by based on his
Professional experiences select suitable system, so further extensive details need not be provided herein.It is not intended, however, that by theoretical beam
Tie up, stirring reactor, rotary kiln, bubble flow can be included effective for some examples for the reactor technology for carrying out the present invention
Fluidized bed reactor and circulating fluid bed reactor lifter or drop device.Rotary kiln is cylindrical vessel, is slightly slanted in level
Face, the rotary kiln are slowly rotated around its axis.Pending material is dosed to the upper end of cylinder.As kiln rotates, material
Moved down progressively towards lower end, and a certain amount of stirring and mixing may be undergone.In bubbling fluidized bed reactor, fluid
(gas or liquid) is with sufficiently high speed by catalyst granules so that it is fluid one that catalyst, which suspends and appears as it,
Sample.In recirculating fluidized bed (also known as transmitting reactor), catalyst and fluid are flowed with high speed cocurrent.Usually by whirlwind point
The fluid of downstream processes can be undergone by being used for the separation from the solid for be recycled to reactor from device system.These reactors can be with
It is the upstream for lifter, or flowing down for drop device.
Preferably, they are introduced continuously into.In one embodiment, whole process continuously carries out.
In the reactor, in the presence of a catalyst, at least one of mixed waste plastic be converted into liquid fuel and
Wax.This conversion preferably at elevated temperatures, such as higher than 350 DEG C, is preferably higher than 400 DEG C, more preferably above 410 DEG C
Lower generation.Compatibly, the conversion is in the range of higher than 410 DEG C to 500 DEG C, more preferably from 420 DEG C to 450 DEG C (such as
About 425 DEG C) at a temperature of occur.
The Gao Chong of catalyst in the reactor and mixed waste plastic is explained in greater detail referring now to following instance and attached drawing
The influence than polystyrene content in lower mixed waste plastic is measured, attached drawing is shown below：
Fig. 1 is influence of the polystyrene loading capacity to selectivity,
Fig. 2 is influence of the polystyrene loading capacity to the quality of diesel oil distillate, and
Fig. 3 is influence of the polystyrene loading capacity to the quality of gasoline fraction.
Following instance is carried out according to following general experimental arrangement：
In each catalysis operation under half point batch mode, by 30g plastics (high density polyethylene (HDPE) (HDPE) and variable
Polystyrene (PS)) and the catalyst of limited amount be loaded into reactor.Reactor is closed, and by reactor in 20 minutes
200 DEG C are heated to from room temperature, and is purged at the same time with 150mL/min nitrogen flows.When internal temperature reaches the fusing point of plastics, open
Begin to stir and be slowly increase until 690rpm.Keep the temperature at 200 DEG C and continue 25-30 minutes.During the heating process,
The nitrogen come out from reactor is not collected.
After first pre-treatment step, reaction temperature is raised the temperature to the rate of heat addition of 10 DEG C/min, and open
Begin to collect gas and nitrogen in corresponding gas sampling bag.When internal temperature reaches reaction temperature, the circulation of gaseous products
It is replaced by another pair glass trap and corresponding gas sampling bag.This was considered as zero reaction time.
Within the selected period, liquid and gaseous products are collected respectively and taken in a pair of of glass trap and its relevant gas
In sample bag.At the end of experiment, reactor is cooled to room temperature.During this cooling step, liquids and gases are also have collected.
Reaction product is divided into 3 groups：I) gas, ii) liquid hydrocarbon and iii) (waxy compound, be accumulated in catalyst to residue
On ash content and coke).The quantitative of gas is completed by using gas chromatography (GC) of the nitrogen as internal standard compound, and liquid with
Residue is quantitatively completed by weight.
Simulation distillation (SIM-DIS) GC methods allow to determine that the different fractions in fluid sample (are evaporated according to selected
Point), detailed hydrocarbon analysis (DHA) GC methods allow the gasoline fraction (C5-C11 of the definite sample finally taken out：Boiling point ＜
216.1℃；It includes the C5-C11 in C5-C6 and fluid sample in gaseous sample) in PIONA (alkane, different alkane
Hydrocarbon, alkene, cycloalkane, aromatic hydrocarbons) component, and GCxGC allows the diesel oil distillate (C12- of the definite fluid sample finally taken out
C21；216.1 DEG C of 359 DEG C of ＜ BP ＜) in saturate (not being the whole of aromatic hydrocarbons), single aromatic, two aromatic hydrocarbons and three aromatic hydrocarbons.
If the disclosure content of any patent, patent application and the publication that are incorporated herein by quoting mode with
Mutually conflict is to the degree that term may be caused not know for the explanation of the application, then this explanation should be preferential.
Example 1
Follow general program described above and carry out the experiment.In this example, raw material are that pure HDPE (is labeled as
100HDPE).Reaction temperature is arranged on 425 DEG C.In this example, using 20g zeolite catalyst (catalyst：Put down by FCC
Weigh the used FCC catalyst that catalyst Co., Ltd (FCC Equilibrium Catalyst, Inc.) provides).Catalyst
It is equal to 20/30 with the weight ratio of plastics.
Example 2
Follow general program described above and carry out the experiment.In this example, raw material be containing 95wt.%HDPE and
The mixture (being labeled as 95HDPE-5PS) of 5wt.%PS.Reaction temperature is arranged on 425 DEG C.In this example, used
20g zeolite catalyst (catalyst：The used FCC catalyst provided by FCC equilibrium catalysts Co., Ltd).Catalyst
It is equal to 20/30 with the weight ratio of plastics.
Example 3
Follow general program described above and carry out the experiment.In this example, raw material be containing 90wt.%HDPE and
The mixture (being labeled as 90HDPE-10PS) of 10wt.%PS.Reaction temperature is arranged on 425 DEG C.In this example, using 20g
Zeolite catalyst (catalyst：The used FCC catalyst provided by FCC equilibrium catalysts Co., Ltd).Catalyst and modeling
The weight ratio of material is equal to 20/30.
Example 4
Follow general program described above and carry out the experiment.In this example, raw material be containing 85wt.%HDPE and
The mixture (being labeled as 85HDPE-15PS) of 15wt.%PS.Reaction temperature is arranged on 425 DEG C.In this example, using 20g
Zeolite catalyst (catalyst：The used FCC catalyst provided by FCC equilibrium catalysts Co., Ltd).Catalyst and modeling
The weight ratio of material is equal to 20/30.
Influence of the polystyrene loading capacity to the selectivity of this method is shown in Fig. 1.It is obvious that to gas and gasoline
Selectivity is reduced with the increase of polystyrene loading capacity, and to the selectivity increase of diesel oil and wax.
However, it is opposite with the expection of technical staff and with described in the prior art on the contrary, method of the invention carries
The diesel oil distillate that the even aromatic compound of decrement is included under low polystyrene loading capacity is supplied to be particularly.This effect is shown
In Fig. 2, it is aromatic that Fig. 2 provides (S) of saturation in the diesel oil distillate depending on the acquisition of polystyrene loading capacity, list
(MA), the amount of two aromatic (DA), three aromatic (TA) and how aromatic (PA) compound.
Fig. 3 shows polystyrene loading capacity to gasoline fraction (P：Alkane, I：Isoparaffin, O：Alkene, N：Cycloalkanes
Hydrocarbon, A：Aromatic hydrocarbons, U：Do not identify) quality influence.In addition Fig. 3 shows the gasoline obtained with different polystyrene loading capacities
The RON and MON of cut.
Fig. 1,2 and 3 are additionally provided with the conversion ratio (X) of the mixed waste plastic in each operation.
Claims (14)
1. a kind of method for mixed waste plastic to be converted into liquid fuel and wax by catalytic cracking, this method includes：
Mixed waste plastic and the catalyst comprising zeolite catalyst are introduced in reactor；
At least a portion mixed waste plastic is allowed to be converted into liquid fuel and wax in the reactor；And
The product stream containing the liquid fuel and wax is removed from the reactor,
It is characterized in that, the mixed waste plastic contain by weight from 2% to 50% polystyrene and by weight from 50%
To 98% polyolefin, the gross weight of polystyrene and polyolefin in the mixed waste plastic is each based on, and it is characterized in that,
The weight ratio of the catalyst reactor and mixed waste plastic is higher than 1: 10.
2. according to the method described in claim 1, wherein based on the gross weight of polystyrene and polyolefin in the mixed waste plastic,
The mixed waste plastic contains by weight from 2% to 40%, preferably by weight from 2% to 30%, more preferably by weight from
2% to 20% polystyrene.
3. method according to claim 1 or 2, wherein the weight ratio of catalyst and mixed waste plastic is high in the reactor
In 1: 8,1: 5, more preferably above 1: 3 are preferably higher than.
4. according to any method of the preceding claims, wherein catalyst and mixed waste plastic in the reactor
Weight ratio is less than 10: 1, is preferably lower than 7: 1.
5. according to any method of the preceding claims, wherein the catalyst is mainly zeolite catalyst.
6. method according to any one of claim 1 to 4, the wherein catalyst are made of zeolite catalyst.
7. method according to any one of claim 1 to 5, the wherein catalyst are additionally catalyzed comprising amorphous type
Agent.
8. according to the method described in claim 7, wherein the amorphous type catalyst include silica, aluminium oxide, kaolin,
Or its mixture.
9. according to any method of the preceding claims, wherein the catalyst be fresh catalyst, equilibrium catalyst,
Or its mixture.
10. according to any method of the preceding claims, wherein at least a portion mixes useless modeling in the reactor
Material is converted into liquid fuel and the temperature residing for wax is higher than 350 DEG C, 410 DEG C is preferably higher than, more preferably higher than 410 DEG C
To in the range of 500 DEG C, even more preferably still in the range of from 420 DEG C to 450 DEG C.
11. according to any method of the preceding claims, wherein the gross weight based on the mixed waste plastic, the mixing
Waste plastics includes the polystyrene and polyolefin by weight more than 50%.
12. according to any method of the preceding claims, this method is carried out continuously.
13. according to any method of the preceding claims, wherein the waste plastics is selected from post-consumer plastic waste, does not conform to rule
Lattice plastics and industrial waste plastics.
14. according to any method of the preceding claims, the wherein waste plastics is substantially free of thermosetting polymer.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP15201127.6 | 2015-12-18 | ||
| EP15201127 | 2015-12-18 | ||
| PCT/EP2016/081302 WO2017103013A1 (en) | 2015-12-18 | 2016-12-15 | Process for converting mixed waste plastic into liquid fuels and waxes by catalytic cracking |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108026452A true CN108026452A (en) | 2018-05-11 |
Family
ID=55068789
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201680051577.2A Pending CN108026452A (en) | 2015-12-18 | 2016-12-15 | Method for mixed waste plastic to be converted into liquid fuel and wax by catalytic cracking |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US20180362857A1 (en) |
| EP (1) | EP3390576A1 (en) |
| CN (1) | CN108026452A (en) |
| WO (1) | WO2017103013A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114867824A (en) * | 2019-12-23 | 2022-08-05 | 雪佛龙美国公司 | Recycle economics for converting plastic waste to polypropylene by refinery FCC and alkylation units |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3653687A1 (en) * | 2018-11-19 | 2020-05-20 | Ecole Polytechnique Federale De Lausanne (EPFL) EPFL-TTO | Direct conversion of plastic materials into methane and liquid fuels |
| CN115322803B (en) * | 2022-08-17 | 2024-03-22 | 华东理工大学 | Method for preparing high-added-value hydrocarbon under moderate condition of waste plastic |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5481052A (en) * | 1992-04-22 | 1996-01-02 | Bp Chemicals Limited | Polymer cracking |
| DE19822568A1 (en) * | 1998-05-20 | 1999-11-25 | Sebastian Hein | Treatment of plastic waste by pyrolysis |
| CN103357431A (en) * | 2012-03-30 | 2013-10-23 | 中国科学院大连化学物理研究所 | Catalyst for process of producing vehicle fuel through pyrolysis of waste plastic, as well as preparation method and application thereof |
| WO2014040634A1 (en) * | 2012-09-14 | 2014-03-20 | Outotec Oyj | Method and apparatus for recycling plastic wastes |
| WO2015128033A1 (en) * | 2014-02-25 | 2015-09-03 | Saudi Basic Industries Corporation | Process for converting mixed waste plastic (mwp) into valuable petrochemicals |
-
2016
- 2016-12-15 US US16/062,713 patent/US20180362857A1/en not_active Abandoned
- 2016-12-15 WO PCT/EP2016/081302 patent/WO2017103013A1/en active Application Filing
- 2016-12-15 CN CN201680051577.2A patent/CN108026452A/en active Pending
- 2016-12-15 EP EP16819860.4A patent/EP3390576A1/en not_active Withdrawn
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|---|---|---|---|---|
| US5481052A (en) * | 1992-04-22 | 1996-01-02 | Bp Chemicals Limited | Polymer cracking |
| DE19822568A1 (en) * | 1998-05-20 | 1999-11-25 | Sebastian Hein | Treatment of plastic waste by pyrolysis |
| CN103357431A (en) * | 2012-03-30 | 2013-10-23 | 中国科学院大连化学物理研究所 | Catalyst for process of producing vehicle fuel through pyrolysis of waste plastic, as well as preparation method and application thereof |
| WO2014040634A1 (en) * | 2012-09-14 | 2014-03-20 | Outotec Oyj | Method and apparatus for recycling plastic wastes |
| WO2015128033A1 (en) * | 2014-02-25 | 2015-09-03 | Saudi Basic Industries Corporation | Process for converting mixed waste plastic (mwp) into valuable petrochemicals |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114867824A (en) * | 2019-12-23 | 2022-08-05 | 雪佛龙美国公司 | Recycle economics for converting plastic waste to polypropylene by refinery FCC and alkylation units |
| CN114867824B (en) * | 2019-12-23 | 2024-03-01 | 雪佛龙美国公司 | Recycling economy for converting plastic waste to polypropylene by refinery FCC and alkylation units |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2017103013A1 (en) | 2017-06-22 |
| US20180362857A1 (en) | 2018-12-20 |
| EP3390576A1 (en) | 2018-10-24 |
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