WO1994011465A1 - Method for direct disposal of plastic waste by chemical recycling in a partial oxidation process - Google Patents

Method for direct disposal of plastic waste by chemical recycling in a partial oxidation process Download PDF

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Publication number
WO1994011465A1
WO1994011465A1 PCT/NO1993/000164 NO9300164W WO9411465A1 WO 1994011465 A1 WO1994011465 A1 WO 1994011465A1 NO 9300164 W NO9300164 W NO 9300164W WO 9411465 A1 WO9411465 A1 WO 9411465A1
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WO
WIPO (PCT)
Prior art keywords
ash
carbon
plastic waste
chemical recycling
soot
Prior art date
Application number
PCT/NO1993/000164
Other languages
French (fr)
Inventor
Wolfgang Kowallik
Hans Jürgen MAAZ
Werner Soyez
Original Assignee
Norsk Hydro A.S
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Filing date
Publication date
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Publication of WO1994011465A1 publication Critical patent/WO1994011465A1/en

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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72Other features
    • C10J3/82Gas withdrawal means
    • C10J3/84Gas withdrawal means with means for removing dust or tar from the gas
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913Carbonaceous raw material
    • C10J2300/0946Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0959Oxygen
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0973Water
    • C10J2300/0976Water as steam
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/169Integration of gasification processes with another plant or parts within the plant with water treatments
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846Partial oxidation, i.e. injection of air or oxygen only
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861Heat exchange between at least two process streams
    • C10J2300/1884Heat exchange between at least two process streams with one stream being synthesis gas
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency
    • Y02P20/129Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/141Feedstock
    • Y02P20/143Feedstock the feedstock being recycled material, e.g. plastics

Definitions

  • the present invention relates to direct disposal of plastic wast by means of a method for chemical recycling of plastic material using the material as feed stock for petrochemical processes More specificly the invention concerns recycling of plastic wast as feed stock into the reactor unit of a partial oxidatio process operating at high temperatures and pressures in th presence of oxygen and with steam as a moderating agent.
  • Th partial oxidation process comprises gasification, waste hea recovery and carbon removal in a scrubber unit during formatio of soot water slurry containing the unburned carbon and ash.
  • recycled plastic waste is proposed to be used as feedstock fo hydrocarbon gasification processes making synthesis gas hydrogen and carbon monoxide. After purification of such a ra gas, which will be heavily loaded with impurities, it may be use as a raw material and feed for the production of basic chemical such as ammonia and ethanol.
  • the temperature of the flui feedstock is between 50-150°C and the viscosity at least 300°cSt preferably 500°cSt and the pressure in the reactor is 15-35 bar
  • the viscosity of the oil/plastic mixture depends on the amoun and type of plastics and the initial viscosity of the base oil Accordingly, for avoiding that the viscosity of the mixture get too high, any increase in plastic waste concentration must b balanced by a less viscous - more expensive base oil. Viscosit below 250-300°cSt is usually desired.
  • the main object of the present invention was to provide a metho for chemical recycling of plastic waste where the above drawback are eliminated.
  • Partial oxidation processes for hydrocarbon feedstocks were developed and commercialized during the 1950's.
  • the best know processes such as the Shell gasification process and the Texac gasification process, have been utilized in a number of commer cial plants.
  • the unburned carbon from the gasifier will be made int a carbon slurry, an aqueous suspension containing soot and significant amount of ash, depending on the feedstock, which ha to be further processed and recycled.
  • the soot/ash slurry from the carbon separation step will at leas contain 0.5-3% unburned carbon and 0.1-2% ash.
  • the ash may contain appreciable amounts of Ni, Fe and V as well as Cl pigments and other inorganic substances used in the productio of plastic materials.
  • Such recirculation is avoided with an improved filtration step the soot/water slurry from the carbon/ash removal step i initially passing through a sedimentation step after flocculatin agents have been added to the solution.
  • Filtration is carried ou at low temperatures below 80-75°C and preferably between 20-60" while confining the soot water slurry containing impurities fro the plastic material combustion between movable filter belt exerting a constant line pressure until the filtercake contains less than 80% water and is no longer soapy or pasty but i tranferred into flakes or agglomerates which are easily separate and well suited for subsequent transport and processing.
  • Oil and plastic material are directl fed to the gasification reactor without any chemical or therma pretreatment breaking down the molecular chains.
  • the oil feedstock may comprice various types of waste residue and oil, like highly aromatic oils, PCB and other waste product from petrochemical industries which to day are disposed of b high temperature incineration.
  • Fig. 1 shows a general flow sheet of the gasification process comprising application of oil/plastic feedstock.
  • Plastic waste material 15 and oil 12 are directly fed into th reactor 13 of the gasification unit. Gasification and partia oxidation is carried out at 40-60 bar and at a temperature o 1300-1500°C in the presence of oxygen 16 using steam 17 as moderating agent. After passing through a waste heat recover unit 14 the gases are passed through a carbon removal step 1 i which unburned carbon and ash are removed in a water wash. The resulting soot/ash water slurry emerging from the carbon/as separation stage 1 is initially passed through a cooler 2 t lower the temperature from approximately 95°C to 20-60°C.
  • the slurry is then passed to a soot slurry tank 3 and thereafte through a mixer 4 to administer flocculation agents from a sourc 5.
  • Two flocculants are used, one positively charged polyelectro lyte sold under the trade mark Praestol 611BC (cationic) and on negatively charged polyelectrolyte sold under the trade mar Praestol 2440 (anionic) , both being in the form of whit polyacrylamide granulates.
  • the ratio between the two types o flocculants can be varied within wide limits, but shoul preferably be in the range of 1-5 : 0.5-2 cationic : anioni flocculant.
  • the total amount of flocculants added was adjusted to betwee 60-100 ppm and the ratio of cationic : anion polyelectrolyte wa 1.5 : 1.
  • the flocculants were added to the slurry in the form o a 0.1-0.3% solution in water.
  • the resulting product 9 could be handled and further processe without any problems.
  • the proportion of oil and recyclin plastics can be varied within wide limits and the upper limit of plastics can be 40-50% (by weight) or higher.
  • the conten of impurities in the plastic waste is less critical than in know recycle processes. Even chlorine containing plastic materia (PVC) can be tolerated to a certain extent. Due to the hig temperatures, any type of organic chlorine compound will b desintegrated.
  • the resulting hydrochloric acid is disposed o within the process according to the invention by neutralization.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)
  • Processing Of Solid Wastes (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)

Abstract

The invention relates to a method for the chemical recycling of plastic waste materials by means of an improved partial oxidation, gasification process comprising gasification, waste heat recovery and carbon removal in a scrubber unit during formation of a soot water slurry containing the unburned carbon and ash. The plastic waste material and oil feedstock are fed directly into the reactor together. Unburned carbon and ash are separated and removed completely from the gasification process thereby establishing a continuous once-through partial oxidation without the need to recirculate carbon/ash residue. The soot/water slurry resulting from the carbon removal step is filtered to form a filtercake containing at least 20 % dry matter, said filtercake being processed into a reclaimable ash. Two types of polyelectrolytic flocculating agents are added to the soot slurry prior to filtration, one being cationic and the other anionic. The flocculants are added in a total amount of 60-100 ppm and at a ratio of cationic: anionic polyelectrolyte of 1-5 : 0.5-2.

Description

s
Method for direct disposal of plastic waste by chemical recycling in a partial oxidation process
The present invention relates to direct disposal of plastic wast by means of a method for chemical recycling of plastic material using the material as feed stock for petrochemical processes More specificly the invention concerns recycling of plastic wast as feed stock into the reactor unit of a partial oxidatio process operating at high temperatures and pressures in th presence of oxygen and with steam as a moderating agent. Th partial oxidation process comprises gasification, waste hea recovery and carbon removal in a scrubber unit during formatio of soot water slurry containing the unburned carbon and ash.
So far recycling development activities have mainly bee concentrated on remelting and reusing of the plastics i competition with virgin plastic material. However, the handlin and reprocessing costs for such uses are very high and th resulting plastic materials cannot compete with virgin plasti materials. A more recent trend of development takes recyclin back upstream of chemical processes. The material is the reprocessed at or before the polymerization stage, to regenerat hydrocarbon feedstock. However, economic viability is hard t achieve also by such routes, so that the necessity to brea through the cost barriers is also growing for such recyclin routes. It has therefore been proposed to develop a feedstock preparatio unit which can be added to the front of an existing, commercia oil processing plant or petrochemical production plant. Th recycled plastic materials are then reprocessed by a chemical o thermal treatment to depolymerize the long chain molecules an to make a liquid feed suitable to be processed in a petrochemica plant.
Furthermore, and according to EP patent application 0.474.62 recycled plastic waste is proposed to be used as feedstock fo hydrocarbon gasification processes making synthesis gas hydrogen and carbon monoxide. After purification of such a ra gas, which will be heavily loaded with impurities, it may be use as a raw material and feed for the production of basic chemical such as ammonia and ethanol.
It is a prerequisite for a successful operation that the plasti waste is gasified under high pressure and that such process ca be carried out continuously. According to the above paten application heavy oil residue is heated to 150-250°C and i transported to an extruder/mixer where it is intimately mixe with plastic granules or particles, which has already been wette by the oil. This results in the preparation of a fluid mixtur which is kept under a pressure which is higher than the existin pressure in a subsequent reactor. The plastics granule/oi mixture is pressed through a die and into the reactor in th presence of steam and oxygen and gasified into synthesis gas.
At the introduction into the reactor the temperature of the flui feedstock is between 50-150°C and the viscosity at least 300°cSt preferably 500°cSt and the pressure in the reactor is 15-35 bar
However, such method is not applicable for use in a continuous partial oxidation gasification process. There is given n solution to the problem of handling the unburned carbon/ash residue which will be of substantial proportions. According t present process design, the unburned carbon is to be recovere and continuously recycled to the feed. But with the recirculatio of a carbon/ash residue resulting from the gasification o substantial amounts of plastic waste, the contamination of th feedstock will be so high that the process will ultimately com to a stop unless a large bleed is applied.
Furthermore, the extra step involved with use of an extruder mixer as described in the above EP-patent application represent an undesired addition and complication for a partial oxidatio plant.
The viscosity of the oil/plastic mixture depends on the amoun and type of plastics and the initial viscosity of the base oil Accordingly, for avoiding that the viscosity of the mixture get too high, any increase in plastic waste concentration must b balanced by a less viscous - more expensive base oil. Viscosit below 250-300°cSt is usually desired.
The idea to reduce the impact of plastics on fuel viscosity b thermal treatment has also been proposed. According to previou experiences those operations cause severe fouling of the hea exchangers.
The main object of the present invention was to provide a metho for chemical recycling of plastic waste where the above drawback are eliminated. Primarily it is an object of the presen invention to provide a continuous once-through productio process, thereby eliminating the need for recirculation of th unburned carbon/ash residue. This will give greater versatilit regarding the permissible contaminants which can be allowed t pass through the reactor. Furthermore, it is an object of the invention to provide process where the feedstock comprising recycled plastic waste ca be passed directly into the reactor without running int viscosity problems and resulting economic disadvantages.
Finally it is an object of the present invention to provide once-through continuous gasification process for recycled plasti waste, eliminating costly and time-consuming plastic handling an pretreatment by devicing a more direct route allowing the plasti material to be used directly without any special pretreatment.
During performance of simulated tests with mixtures of heavy oi and plastic (polyolefin) in solutions under conditions whic prevail within a partial oxidation gasification reactor, it wa found that the viscosity increased dramatically with plasti material concentrations from about 10% and higher. When th concentration was increased from 15-22% (by weight) , th viscosity increased by a factor of 40.
Thus it will not be feasible to introduce highly concentrate solutions of polymer waste into a gasification reactor withou exceeding the max. viscosity for proper atomization.
Partial oxidation processes for hydrocarbon feedstocks wer developed and commercialized during the 1950's. The best know processes, such as the Shell gasification process and the Texac gasification process, have been utilized in a number of commer cial plants.
Gasification processes utilizing recycled plastics and othe hydrocarbon feedstock normally comprise three principal steps:
- gasification, in which the feedstock is converted into ra synthesis gas in the presence of oxygen and a moderating agent - waste heat recovery in which high pressure steam is generat from the hot gases leaving the reactor, and
- carbon removal, in which residual carbon contained in t reactor outlet gas, is removed in a mul istep water wash.
Hereby the unburned carbon from the gasifier will be made int a carbon slurry, an aqueous suspension containing soot and significant amount of ash, depending on the feedstock, which ha to be further processed and recycled.
A serious drawback of such processes is already that a certai percentage of the feedstock is not gasified and remains in th form of soot mixed with appreciable amounts of ash.
The soot/ash slurry from the carbon separation step will at leas contain 0.5-3% unburned carbon and 0.1-2% ash. The ash ma contain appreciable amounts of Ni, Fe and V as well as Cl pigments and other inorganic substances used in the productio of plastic materials.
Without recirculation of unburned carbon and ash the overal efficiency of the gasification process is improved and the amoun of contaminants in the feedstock may be appreciably increase because there is no gradual build up of impurities due t recirculation of such matter.
Such recirculation is avoided with an improved filtration step the soot/water slurry from the carbon/ash removal step i initially passing through a sedimentation step after flocculatin agents have been added to the solution. Filtration is carried ou at low temperatures below 80-75°C and preferably between 20-60" while confining the soot water slurry containing impurities fro the plastic material combustion between movable filter belt exerting a constant line pressure until the filtercake contains less than 80% water and is no longer soapy or pasty but i tranferred into flakes or agglomerates which are easily separate and well suited for subsequent transport and processing.
Now according to the present invention there is provided a metho for chemical recycling of plastic waste by means of the abov once-through process route. Oil and plastic material are directl fed to the gasification reactor without any chemical or therma pretreatment breaking down the molecular chains.
The oil feedstock may comprice various types of waste residue and oil, like highly aromatic oils, PCB and other waste product from petrochemical industries which to day are disposed of b high temperature incineration.
Seperate feed of oil and plastic materials directly to th reactor burner avoids the above mentioned problems which wil arise when oil and plastic materials are mixed.
Essential features of the invention are as defined in th accompanying claims 1-6 and further important aspects will als be apparent from the detailed description of the invention below
Fig. 1 shows a general flow sheet of the gasification process comprising application of oil/plastic feedstock.
Plastic waste material 15 and oil 12 are directly fed into th reactor 13 of the gasification unit. Gasification and partia oxidation is carried out at 40-60 bar and at a temperature o 1300-1500°C in the presence of oxygen 16 using steam 17 as moderating agent. After passing through a waste heat recover unit 14 the gases are passed through a carbon removal step 1 i which unburned carbon and ash are removed in a water wash. The resulting soot/ash water slurry emerging from the carbon/as separation stage 1 is initially passed through a cooler 2 t lower the temperature from approximately 95°C to 20-60°C.
The slurry is then passed to a soot slurry tank 3 and thereafte through a mixer 4 to administer flocculation agents from a sourc 5. Two flocculants are used, one positively charged polyelectro lyte sold under the trade mark Praestol 611BC (cationic) and on negatively charged polyelectrolyte sold under the trade mar Praestol 2440 (anionic) , both being in the form of whit polyacrylamide granulates. The ratio between the two types o flocculants can be varied within wide limits, but shoul preferably be in the range of 1-5 : 0.5-2 cationic : anioni flocculant.
The total amount of flocculants added was adjusted to betwee 60-100 ppm and the ratio of cationic : anion polyelectrolyte wa 1.5 : 1. The flocculants were added to the slurry in the form o a 0.1-0.3% solution in water.
Initially the slurry was dewatered while passing a sedimentatio tank 6. Thereafter it was passed through the filter unit 7 wher it was pressed between two vertically moving filterbands an finally compressed by means of rollers pressing the filterband together to exert a constant pressure until the water content o the filtercake was reduced to <80%. Filtrate from the filtratio stage 7 was returned to the soot separation unit 1 by means o a pump and pipe 10.
Thereafter the filtercake was released on to a movable conveyo belt in the form of dry flakes or plates with an averag thickness of approx. 2 mm and fed into the combustion unit 8 The resulting product 9 could be handled and further processe without any problems. The proportion of oil and recyclin plastics can be varied within wide limits and the upper limit of plastics can be 40-50% (by weight) or higher. Also the conten of impurities in the plastic waste is less critical than in know recycle processes. Even chlorine containing plastic materia (PVC) can be tolerated to a certain extent. Due to the hig temperatures, any type of organic chlorine compound will b desintegrated. The resulting hydrochloric acid is disposed o within the process according to the invention by neutralization.

Claims

Claims
Method for the chemical recycling of plastic waste materials by means of an improved partial oxidation, gasification process comprising gasification, waste heat recovery and carbon removal in a scrubber unit during formation of a soot water slurry containing the unburned carbon and ash, c h a r a c t e r i z e d i n t h a t the plastic waste material and oil feedstock are fed directly into the reactor and that unburned carbon and ash are seperated from the formed gases and removed from the gasification process, thereby establishing a continuous once-through partial oxidation without the need to recirculate carbon/ash residue.
Method for chemical recycling of plastic waste according to claim 1, c h a r a c t e r i z e d i n t h a t plastic waste material in liquid form and oil feed¬ stock are fed as two separate streems to the reactor burner.
Method for chemical recycling of plastic waste according to claim 1, c h a r a c t e r i z e d i n t h a t the soot/water slurry resulting from the carbon removal step comprising filtration to form a filter¬ cake containing at least 20% dry matter, said filtercake being processed into a reclaimable ash, containing insignificant amounts of carbon.
4. Method for chemical recycling according to claim 1, c h a r a c t e r i z e d i n t h a t two types of polyelectrolytic flocculating agents are added to the soot slurry prior to filtration, one being cationic and the other an anionic poly¬ electrolyte.
5. Method for chemical recycling according to claim 1, c h a r a c t e r i z e d i n t h a t the slurry is cooled to a temperature below 80"C and then filtered until the moisture content is reduced to below 80% by weight.
6. Method for chemical recycling according to claim 1, c h a r a c t e r i z e d i n t h a t the flocculants are added in a total amount of 60- 100 ppm and that at a ratio of cationic : anionic polyelectrolyte is kept at 1-5 : 0.5-2.
PCT/NO1993/000164 1992-11-11 1993-11-09 Method for direct disposal of plastic waste by chemical recycling in a partial oxidation process WO1994011465A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO924337 1992-11-11
NO924337A NO176669C (en) 1992-11-11 1992-11-11 Process for the direct disposal of plastic waste by chemical recycling in a process for partial oxidation of hydrocarbons

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WO1994011465A1 true WO1994011465A1 (en) 1994-05-26

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CA (1) CA2149145C (en)
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WO (1) WO1994011465A1 (en)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008056311A1 (en) * 2008-11-07 2010-05-12 Apk Aluminium Und Kunststoffe Ag Process for separating individual valuable substances from mixed, in particular comminuted plastic waste
CN113185257A (en) * 2021-03-31 2021-07-30 太原理工大学 Solid waste regeneration foamed ceramic material for heat insulation wall and preparation method thereof

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0474626A2 (en) * 1990-09-05 1992-03-11 OMV Aktiengesellschaft Process for charging continuously a mixture of solids and liquid to be gasified
EP0567449A1 (en) * 1992-04-22 1993-10-27 ÖMV Aktiengesellschaft Process for thermal transformation of organic substances into gases

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0474626A2 (en) * 1990-09-05 1992-03-11 OMV Aktiengesellschaft Process for charging continuously a mixture of solids and liquid to be gasified
EP0567449A1 (en) * 1992-04-22 1993-10-27 ÖMV Aktiengesellschaft Process for thermal transformation of organic substances into gases

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NO176669C (en) 1995-05-10
CA2149145A1 (en) 1994-05-26
CN1092097A (en) 1994-09-14
CA2149145C (en) 2004-04-13
NO924337D0 (en) 1992-11-11
NO176669B (en) 1995-01-30
NO924337L (en) 1994-05-13

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