FI20205131A1 - Method for processing plastic waste pyrolysis gas - Google Patents

Method for processing plastic waste pyrolysis gas Download PDF

Info

Publication number
FI20205131A1
FI20205131A1 FI20205131A FI20205131A FI20205131A1 FI 20205131 A1 FI20205131 A1 FI 20205131A1 FI 20205131 A FI20205131 A FI 20205131A FI 20205131 A FI20205131 A FI 20205131A FI 20205131 A1 FI20205131 A1 FI 20205131A1
Authority
FI
Finland
Prior art keywords
pyrolysis gas
plastic waste
waste pyrolysis
stream
temperature
Prior art date
Application number
FI20205131A
Other languages
Finnish (fi)
Swedish (sv)
Other versions
FI129233B (en
Inventor
Mikko Matilainen
Max Nyström
Antti Kurkijärvi
Hannu Lehtinen
Esa Korhonen
Original Assignee
Neste Oyj
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Neste Oyj filed Critical Neste Oyj
Priority to FI20205131A priority Critical patent/FI129233B/en
Publication of FI20205131A1 publication Critical patent/FI20205131A1/en
Application granted granted Critical
Publication of FI129233B publication Critical patent/FI129233B/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/062—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F19/00—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers
    • F28F19/008—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers by using scrapers
    • 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

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)

Abstract

The present invention relates to methods for processing plastic waste pyrolysis gas, in particular methods wherein clogging of the systems used in the method is avoided or at least alleviated.

Description

METHOD FOR PROCESSING PLASTIC WASTE PYROLYSIS GAS
FIELD The present invention relates to methods for processing plastic waste pyrolysis gas, in particular methods wherein clogging of the systems used in the method is avoided.
BACKGROUND Significant amount of waste plastic is produced around the world. For example municipal solid plastic waste comprises typically high-density polyethylene (HDPE), low- density polyethylene (LDPE), polypropylene (PP), polystyrene (PS), poly(vinyl chloride) (PVC), and poly(ethylene terephthalate) (PET). This is an abundant feedstock which could be utilized as an alternative refinery feed and a platform to new plastics and chemicals. However, solid plastic is not suitable feedstock as such, but it needs to be liquefied first. Yield and composition of the products are mainly influenced by plastic type and process conditions (Williams et al. Energy & Fuels, 1999, 13, 188-196). Processing of waste plastic is carried out in chemical recycling systems, and it relies on thermal, pyrolytic reactions to crack the long plastic polymers to shorter products, most of which are liquids. The gaseous product mixture from plastic pyrolysis is known to clog and foul surfaces, pipes and equipment. Partly this is because some of the reaction products are heavy, waxy components which deposit on surfaces, but also tar, char and more solid, coke type deposits are common. The waxy o components and tar are especially problematic on cooling surfaces of heat S exchangers used in condensing the reaction mixture, but coke can deposit S 25 anywhere in the equipment. These cause two main problems. Firstly, the deposits 5 act as an insulator reducing the heat transfer in the heat exchangers. Secondly, the E deposits will eventually clog the heat exchanger, preventing any flow through it. S Therefore, if traditional heat exchangers are used to condense the pyrolysis gas, o then the eguipment needs to be duplicated: while one is in operation, the other is O 30 under maintenance and cleaning. This is expensive and labor intensive. This problem has been solved before using direct contact condensers. However, spray condensers, for example, suffer from relatively low separation efficiency, and they offer no protection against coke deposits. Also, the liquid recycling used in these condensers necessitates a liquid holdup which has two main drawbacks. Firstly, it significantly increases the fire load of the apparatus as there is a reservoir of hot pyrolysis product mixture in the recycle loop. Secondly, the relatively long residence time of this liquid reservoir exposes the liquid to additional thermal reactions, potentially reducing the product quality and causing fouling of the equipment. Accordingly, there is still need for further methods for processing plastic waste pyrolysis gas wherein risk of clogging of the system used in the process is reduced.
SUMMARY The following presents a simplified summary in order to provide a basic understanding of some aspects of various embodiments of the invention. The summary is not an extensive overview of the invention. It is neither intended to identify key nor critical elements of the invention, nor to delineate the scope of the invention. The following summary merely presents some concepts of the invention in a simplified form as a prelude to a more detailed description of exemplifying embodiments of the invention. It was observed that when gaseous reaction mixture from plastic waste pyrolysis was admixed with cooled, condensed pyrolysis product, the highest boiling part of the pyrolysis gases condense smoothly from the admixture without clogging. N It was also observed that clogging of the plastic waste pyrolysis products could be N avoided by passing the gaseous pyrolysis product to a condensing means operating
QA <Q at lower temperature than the pyrolysis temperature, when any solidifying materials
NN © is wiped and/or scraped from inner walls of the condensing means.
I a a — 25 In accordance with the invention, there is provided a new method for processing
O D> plastic waste pyrolysis gas, the method comprising
O S a) providing
N o a plastic waste pyrolysis gas stream wherein temperature of the plastic waste pyrolysis gas stream is 300-650 °C, preferably 450- 500 °C and o a hydrocarbonaceous liquid stream wherein temperature of the hydrocarbonaceous liquid stream is below temperature of the plastic waste pyrolysis gas stream, b) admixing, preferably in an ejecting means, the plastic pyrolysis gas stream and the hydrocarbonaceous liquid stream to form an admixture, c) ejecting, preferably through a spray nozzle, the admixture to a chamber to produce a condensed fraction and a gaseous fraction, and d) separating the gaseous fraction and the condensed fraction to yield a first liquid product stream and a gaseous product stream. In accordance with the invention, there is provided also another new method for processing plastic waste pyrolysis gas, the method comprising a) providing a plastic waste pyrolysis gas stream wherein temperature of the plastic waste pyrolysis gas stream is 300-650 °C, preferably 450-500 °C, b) transferring the plastic waste pyrolysis gas stream to a condensing means, wherein temperature in the condensing means is below temperature of the plastic waste pyrolysis gas stream of step a) to produce a condensed fraction and a gaseous fraction of the plastic waste pyrolysis gas, c) continuously wiping and/or scraping inner surfaces of the condensing means, and S d) separating the gaseous fraction and the condensed fraction to yield a first O liquid product stream and a gaseous product stream. S 25 A number of exemplifying and non-limiting embodiments of the invention are 5 described in accompanied dependent claims. E: Various exemplifying and non-limiting embodiments of the invention and to methods ™ of operation, together with additional objects and advantages thereof, are best 3 understood from the following description of specific exemplifying embodiments N 30 when read in connection with the accompanying figures.
The verbs “to comprise” and “to include” are used in this document as open limitations that neither exclude nor require the existence of also unrecited features.
The features recited in depending claims are mutually freely combinable unless otherwise explicitly stated. Furthermore, it is to be understood that the use of "a" or "an", i.e. a singular form, throughout this document does not exclude a plurality.
BRIEF DESCRIPTION OF FIGURES The exemplifying and non-limiting embodiments of the invention and their advantages are explained in greater detail below with reference to the accompanying figures, in which figure 1 show an exemplary non-limiting system suitable for processing plastic waste pyrolysis gas according to an embodiment of the present invention, and figure 2 shows another exemplary non-limiting system suitable for processing plastic waste pyrolysis gas according to another embodiment of the present invention.
DESCRIPTION The present invention is related to processing plastic waste pyrolysis gas such that clogging of a system used in the method is avoided or at least alleviated.
Figure 1 shows an exemplary system 100 suitable for use in a method according to an embodiment of the present invention. According to this embodiment the method comprises co-introducing plastic waste pyrolysis gas stream (A) and hydrocarbonaceous liquid stream (B) to an ejecting means 101 to form an admixture (C). Temperature of the plastic waste pyrolysis gas stream is typically 300-650 °C, N 20 preferably 450-500 °C. Temperature of the hydrocarbonaceous liquid stream is N below temperature of the plastic waste pyrolysis gas stream, typically 100-300 °C, 7 preferably 175-225 °C. An exemplary temperature of the hydrocarbonaceous liquid 7 stream is 200 °C. The proper admixing will ensure a thorough contact between the E two phases and cooling of the reaction gases so that the highest boiling part of the O 25 reaction gases condense.
5 < After mixing, the admixture is directed, preferably through a spray nozzle 102 to a chamber 103 wherein liquids and gases separate, and a condensed, liquid fraction
(D1) and a gaseous fraction (E1) are formed.
The chamber comprises outlets for gases and liquids.
Accordingly, as the gaseous pyrolysis reaction mixture is mixed thoroughly with the cooler hydrocarbonaceous liquid before it enters the chamber, a good contact 5 between the liquid phase and the gaseous phase is achieved.
This results in improved, more ideal condensing behavior and more ideal separation.
Also, since the admixing is carried out in an ejecting means though a nozzle, the flow rate is high enough to keep the ejecting means free from fouling, while still possessing the same advantages as other direct contact condensers.
An exemplary device comprising ejecting means, nozzle and a chamber is an ejector venturi scrubber.
Mass ratio of the liquid and gas in the admixture should be high enough to avoid too strong cooling.
The mass ratio is typically 1-100, preferably 5-25. An exemplary mass ratio is 12. When the admixture ejected through the nozzle to the chamber, a liquid phase and a gaseous phase is formed, and the liquid fraction and the gaseous fraction are separated to yield the first liquid product stream (D1) and a gaseous product stream (E1) According to a preferable embodiment a first part (D1a) of the first liquid product stream is recirculated, e.g. pumped back from chamber 103 to the ejecting means 101 via a line 104, and a second part (D1b) of the first liquid product stream is taken S out from the process to a collecting means 105 as a “heavy product”. Yield and O composition of the heavy product is mainly dependent on the nature of the waste N plastic, the pyrolysis conditions and the condensing temperature.
S In order to avoid blockages, the line 104 and thus also the first part of the first liguid E 25 products stream therein is preferably kept at temperatures above 100 °C more n preferably between 150 °C and 250 °C.
The desired temperature range can be 3 obtained by insulating the line and/or using one or more heating means.
An N exemplary temperature of the first part of the first liquid product stream is 200 °C.
According to a preferable embodiment the gaseous fraction, i.e. the gaseous product stream (E1) is directed from the chamber 103 via a line 106 to a condensing means 107. The condensing means is typically a traditional heat exchanger. According to an exemplary embodiment, temperature of the gaseous product stream is decreased in the condensing means 107 to 10-50 °C, preferably to 20-40 °C. The cooling produces condensed liquid and non-condensable gases. No fouling or clogging is expected within the line 106 and in the condensing means 107 as the majority of the heavy components have been removed. The condensed liquid (D2) is separated from the non-condensable gases (E2) to yield a second liquid product stream, i.e. a light product. It can be transferred to a collecting means such as a tank 108. Yield and composition of the light product is dependent on the nature of the waste plastic, the pyrolysis conditions and the condensation temperatures. The non-condensable gases may be directed to combustion or to one or more further collecting means.
According to the embodiment shown in figure 1, the method comprises co- introducing plastic waste pyrolysis gas stream and a hydrocarbonaceous liquid stream to an ejecting means. In order to initiate the process, the system is filled with a seed liquid. The seed liquid is typically condensed plastic waste pyrolysis gas from an earlier process. Alternatively, another hydrocarbonaceous liquid composition — with similar properties can be used. The aim is to verify that the system includes enough hydrocarbonaceous liguid material to be admixed with the plastic waste pyrolysis gas stream in the ejecting means in the beginning of the process.
N Figure 2 shows an exemplary system 200 suitable for use in a method according to N another embodiment of the present invention. According to the embodiment shown 3 25 in the figure, a plastic waste pyrolysis gas stream (A) is transferred a condensing I means 201. Temperature of the plastic waste pyrolysis gas stream is typically 300- E 650 *C, preferably 450-500 *C. Temperature of the condensing means is below the O temperature of the plastic waste pyrolysis gas stream. Exemplary temperature of S the condensing means is 100-300 °C, preferably 175-225 °C.
N According to this embodiment the condensing means comprises wiping means and/or scraping means 202 adapted to wipe and/or scrape mechanically the inner surfaces of the condensing means 201. Exemplary suitable condensing means are wiped film condensers and scraped surface heat exchangers.
These condensing means are basically jacketed tanks, with a rotor inside which continuously wipes, and scrapes any solidifying material from the walls of the condensing means.
This prevents the formation of thick deposits on the condenser walls and thus prevents clogging of the apparatus.
The condensing means 201 is operating at temperature which is lower than the temperature of the plastic waste pyrolysis gas stream.
Accordingly, the heaviest parts of the pyrolysis gas are condensed, and a heavy component depleted gaseous fraction is produced.
Separation of the condensed fraction and the gaseous fraction yields the first liquid product stream (D1) and a gaseous product stream (E1). The first liquid product stream (D1) i.e. the heavy fraction may be transferred via line 203 to a collecting means 204 as a heavy product.
In order to avoid blockages, the line 203 is preferably kept at temperatures above 100 °C more preferably between 150°C and 250 °C.
The desired temperature range can be obtained by insulating the line and/or using one or more heating means.
According to a preferable embodiment the gaseous product stream is directed via line 205 to a second condensing means 206. This condensing means is typically a traditional heat exchanger.
According to an exemplary embodiment, temperature of the gaseous fraction is decreased in the condensing means 206 to 10-50 °C, preferably 20-40 °C.
The cooling produces condensed liquid and non-condensable gases.
No fouling or clogging is expected within the line 205 and in the condensing N means 206 as the majority of the heavy components have been removed.
After S cooling, the condensed liquid is separated from the non-condensable gases (E2) to S 25 yield a second liquid product stream (D2). It can be transferred in a collecting means = such as a tank 207 as a light product.
The non-condensable gases may be directed 5 to combustion or to one or more further collecting means.
Yield and composition of 3 the light product is dependent mainly on the nature of the waste plastic, the pyrolysis S conditions and the condensing temperatures.
The non-condensable gases may be directed to combustion or to one or more further collecting means.
Experimental The process was simulated with Aspen plus software. The pyrolysis gas was modelled using pseudo components, which were estimated using experimentally measured distillation curve and density from crude plastics pyrolysis oil. The used density was 809.8 kg/m?, and true boiling point (TBP) distillation curve is presented in table 1. Table 1 recovered mass (%) temperature (C°)
O QA O
N <Q
NN
O = a Additionally, the amount and composition of light ends were estimated from 0 10 literature (Williams et al., Energy & Fuels, 1999, 13, 188-196; Williams et al, S Recources, Concervation and Recycling, 2007, 51, 754-769). Mass ratio of lights N and pseudo components was 0.27, and the composition of the lights is presented in table 2.
Table 2 The thermodynamic model used in the simulations was Braun K-10, and it was assumed that there was one ideal separation stage in the ejecting means.
Stream of plastic waste pyrolysis gas, having a pressure of 95 kPa(a), a temperature of 500 °C, an average mol weight 69.2 g/mol and a mass flow of 20 kg/h exited the reactor.
o The pyrolysis gas is allowed to enter a venturi ejector, where it is contacted with
QA a recirculated — hydrocarbonaceous liquid stream. Mass ratio of the S 10 — hydrocarbonaceous liquid and the plastic waste pyrolysis gas was approximately 5 100. The venturi ejector sprays the admixture into a separation chamber, and the E condensed heavy hydrocarbons were pumped through a tube-and-shell heat — exchanger. This heat exchanger is adjusted so that the temperature of the resulting
O o admixture was from 100 to 300 °C. After the heat exchanger the liquid heavy O 15 hydrocarbons were split and partly recirculated back to venturi ejector and partly bled out and collected.
The non-condensed gases exited the separation tank through a demister and were directed to a heat exchanger. The output temperature of the process side of this heat exchanger was 40 °C. Condensed light hydrocarbons and non-condensables were fed to a separation tank, from where non-condensables were fanned out and directed to incineration, and the liquid was collected. The results from three simulation cases are presented in the tables 3-5. Table 3 Admixture Product flows (wt-% of pyrolysis gas) temperature (°C) heavy product light product Uncondensables Table 4 Admixture TBP distillation curve (°C) temperature (°C) Heavy product Light product
O QA S
O o 10
QA O N
Table 5 Admixture Average molar weight of gas (g/mol) temperature (°C) . Between Pyrolysis gases Uncondensables condensers The specific examples provided in the description given above should not be construed as limiting the scope and/or the applicability of the appended claims.
O QA O N
N <Q
NN O
I = 0
LO O QA O N

Claims (5)

What is claimed is
1. A method for processing plastic waste pyrolysis gas, the method comprising a) providing a plastic waste pyrolysis gas stream wherein temperature of the plastic waste pyrolysis gas stream is 300-650 °C, preferably 450-500 °C, b) transferring the plastic waste pyrolysis gas stream to a condensing means (202), wherein temperature in the condensing means is below temperature of the plastic waste pyrolysis gas stream of step a) to produce a condensed fraction and a gaseous fraction of the plastic waste pyrolysis gas, c) continuously wiping and/or scraping inner surfaces of the condensing means, and d) separating the gaseous fraction and the condensed fraction to yield a first liquid product stream and a gaseous product stream.
2. The method according to claim 1 wherein temperature of the condensing means is 100-300 °C, preferably 175-225 °C.
3. The method according to claim 1 or 2 comprising collecting the first liquid product stream.
4. The method according to any one of claims 1 to 3 comprising cooling the gaseous product stream of step d) to 10-50 °C, preferably to 20-40 °C to yield a second liquid product stream and a gaseous stream.
5. The method according to claim 4 comprising collecting the second liquid product stream.
O
QA
O
N
N <Q
NN
O
I a a 0
LO
O
QA
O
N
FI20205131A 2019-06-10 2019-06-10 Method for processing plastic waste pyrolysis gas FI129233B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
FI20205131A FI129233B (en) 2019-06-10 2019-06-10 Method for processing plastic waste pyrolysis gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FI20205131A FI129233B (en) 2019-06-10 2019-06-10 Method for processing plastic waste pyrolysis gas

Publications (2)

Publication Number Publication Date
FI20205131A1 true FI20205131A1 (en) 2020-12-11
FI129233B FI129233B (en) 2021-09-30

Family

ID=74551380

Family Applications (1)

Application Number Title Priority Date Filing Date
FI20205131A FI129233B (en) 2019-06-10 2019-06-10 Method for processing plastic waste pyrolysis gas

Country Status (1)

Country Link
FI (1) FI129233B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2022250829A1 (en) * 2021-05-28 2022-12-01 Eastman Chemical Company Mixed liquified pyrolysis gas with recycled content

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2022250829A1 (en) * 2021-05-28 2022-12-01 Eastman Chemical Company Mixed liquified pyrolysis gas with recycled content

Also Published As

Publication number Publication date
FI129233B (en) 2021-09-30

Similar Documents

Publication Publication Date Title
FI128804B (en) Method for processing plastic waste pyrolysis gas
US7847136B2 (en) Device and method for recovering fractional hydrocarbons from recycled plastic fractions and/or oily residues
US7560019B2 (en) System and method for extending the range of hydrocarbon feeds in gas crackers
US8025774B2 (en) Controlling tar by quenching cracked effluent from a liquid fed gas cracker
EP1934307B1 (en) Method for processing hydrocarbon pyrolysis effluent
KR102381741B1 (en) A sequential cracking process
EP1707614A1 (en) Thermal or catalytic cracking process for hydrocarbon feedstocks and corresponding system
CA2558347A1 (en) Device and method for recovering fractional hydrocarbons from reclaimed plastic materials and/or from oily residues
RU2504575C2 (en) Method and apparatus for separating coal tar from suspended-phase hydrocracked vacuum gas oil and composition thereof
CN116997602A (en) Extraction solvent for plastic derived synthetic raw materials
FI129233B (en) Method for processing plastic waste pyrolysis gas
WO2022020152A1 (en) Methods for plastic waste recycle using slurry
NL2033861B1 (en) System and Process for Degassing of Pyrolysis Plastics
WO2020190168A1 (en) Method of hydrocarbon pyrolysis and device for implementing same
US20230332051A1 (en) Integrated mixed plastic pyrolysis with heavy oil product thermal cracking
AU2023254034A1 (en) Integrated mixed plastic pyrolysis with heavy oil product thermal cracking
WO2024218310A2 (en) Advanced chemical recycling of mixed and pure waste plastics within a molten metal reactor

Legal Events

Date Code Title Description
FG Patent granted

Ref document number: 129233

Country of ref document: FI

Kind code of ref document: B