EP4048454A1 - Dispositif de correction de front d'onde de réfraction - Google Patents

Dispositif de correction de front d'onde de réfraction

Info

Publication number
EP4048454A1
EP4048454A1 EP20812399.2A EP20812399A EP4048454A1 EP 4048454 A1 EP4048454 A1 EP 4048454A1 EP 20812399 A EP20812399 A EP 20812399A EP 4048454 A1 EP4048454 A1 EP 4048454A1
Authority
EP
European Patent Office
Prior art keywords
combustor
boiler
plant
carbon dioxide
steam
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP20812399.2A
Other languages
German (de)
English (en)
Inventor
Caglar Ataman
Kaustubh BANERJEE
Pouya RAJAEIPOUR
Hans Zappe
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Rockfuel Innovations Ltd
Original Assignee
Rockfuel Innovations Ltd
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 Rockfuel Innovations Ltd filed Critical Rockfuel Innovations Ltd
Publication of EP4048454A1 publication Critical patent/EP4048454A1/fr
Pending legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • B09B3/45—Steam treatment, e.g. supercritical water gasification or oxidation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/14—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with steam or water
    • 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
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/12—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of plastics, e.g. rubber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/10—Supplementary heating arrangements using auxiliary fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/28—Plastics or rubber like materials
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste

Definitions

  • This invention relates to a system and method for the processing of polymeric waste. Furthermore, the invention relates to the carbon neutral and efficient processing of such waste.
  • the invention may be utilised in the formation of carbon neutral fuels for transport, domestic and commercial use, and the formation of useful carbon neutral or greenhouse neutral gases.
  • the invention may be utilised in the production of carbon neutral products.
  • system is used herein to mean an arrangement of apparatus and, while some of the component parts of the apparatus are conventional and/or known per se, the particular assemblage is novel and wholly inventive.
  • carbon neutral is used herein to mean that the amount of carbon dioxide produced during the process is balanced or offset by the subsequent absorption or capture of an equivalent or even greater quantity of carbon dioxide by calcium oxide produced by the process or by a subsidiary plant incorporated in the apparatus of the process.
  • polymeric should be interpreted as “synthetic” polymer-based material.
  • the invention is concerned primarily with plastic polymeric waste, and therefore a particular emphasis is placed on the processing of waste plastics and the invention is discussed in this context. It is of course feasible that the system and method as described herein could be applicable to the carbon neutral processing of other types of polymeric waste and the scope of the present invention is intended to cover such instances.
  • plastic can be recycled. There are basically two types of plastic: carbon chain and heterochain; heterochain plastic cannot easily be recycled, if at all. Even where possible, plastic products can only be recycled a few times (sometimes only two or three times) before they lose their original properties and become non-recyclable. The problem is exacerbated by the fact that often recyclable and non-recyclable plastics are not segregated at all. The cost and effort required to sort and segregate recyclable from non-recyclable plastic is high, typically resulting in recyclable plastic being transferred to landfill.
  • Waste plastic is extremely harmful to marine life. According to the documentary series “The Blue Planet”, evidence has been found, even in the remote waters of Antarctica, of plastic killing and harming seabirds. With increasing concerns as to the devastating and potentially catastrophic effect of waste plastic in the environment, there is a need to find solutions to eradicate or significantly reduce the harmful effects of waste plastic.
  • Plastic is formed from natural materials, including natural gas and crude oil and the burning thereof inevitably produces a vast amount of heat energy, which could be utilised. Plastic contains the same amount of energy per pound as premium fuel.
  • a significant drawback with such combustion is the creation of harmful dioxins, as well as carbon dioxide.
  • Efficient incinerators can largely address the issue by preventing the exposure of dioxins. This does not however address the inevitable production of carbon dioxide.
  • the environmental impact of carbon dioxide has been a growing concern and the need to reduce such emissions increasingly prevalent.
  • scientists devoting their lives to, and specialising in, climate science warn us that climate change is the largest of all threats that could bring about the extinction of humankind.
  • climate change is one of the very largest risks to our continued existence as a species. It is incumbent upon all, including innovators and all those involved in the protection of new ideas to try to do all that we can to encourage solutions that will help in the fight against climate change for the sake of all humanity.
  • Catalysts effectively to convert carbon dioxide into carbon monoxide and oxygen or hydrogen have been identified. Such catalysts have been shown to provide highly effective results, but the process requires large amounts of energy, making such conversion inefficient in practice.
  • a system for the processing of polymeric waste comprising:
  • processing plant operatively connected to the combustor to receive heat energy therefrom, the processing plant being arranged thereby to heat additional polymeric waste to produce a synthesis gas, without combustion; wherein the system optionally further comprises:
  • a boiler having an inlet for the introduction of water and an outlet for the release of steam, the boiler being operatively connected to the combustor to receive heat energy therefrom and to heat the water to produce steam and being operatively connected to the processing plant to transfer steam thereto.
  • a method of processing polymeric waste comprising:
  • the method optionally comprises:
  • a system for the processing of polymeric waste comprising:
  • a boiler having an inlet for the introduction of water and an outlet for the release of steam, the boiler being operatively connected to the combustor to receive heat energy therefrom and to heat the water to produce steam;
  • a method of processing polymeric waste comprising:
  • a system for the processing of polymeric waste comprising:
  • a boiler having an inlet for the introduction of water and an outlet for the release of steam, the boiler being operatively connected to the combustor to receive heat energy therefrom and to heat the water to produce steam;
  • a processing plant operatively connected to the combustor to receive heat energy therefrom and operatively connected to the boiler to receive steam therefrom, the processing plant being arranged thereby to heat additional polymeric waste to produce a synthesis gas, without combustion.
  • a method of processing polymeric waste comprising:
  • Such apparatus may include a pyrolysis plant, and/or a gasification plant. Additionally, the processing plant may further comprise a Fischer Tropsch plant to convert synthesis gas into a synthesis fuel. Pyrolysis of polymeric waste in the processing plant may directly produce diesel or fuel oil.
  • the combustor preferably further comprises a carbon dioxide regeneration arrangement configured to remove and re introduce carbon dioxide back into the combustor.
  • a carbon dioxide regeneration arrangement configured to remove and re introduce carbon dioxide back into the combustor.
  • This serves to produce a limited or controlled oxygen environment and thus can facilitate a “slow burn” which will result in the production of more char.
  • the heat in the combustor and the regeneration arrangement may thereby serve to facilitate the conversion of carbon dioxide (a greenhouse gas) into carbon monoxide (a greenhouse neutral gas).
  • Carbon monoxide is not considered a greenhouse gas because it does not absorb enough terrestrial thermal infra-red energy to fall within the definition.
  • carbon monoxide is an indirect greenhouse gas because it can indirectly increase the global warming potential of greenhouse gasses. The specific reactions incurred in the process are well known to those in the art.
  • the carbon monoxide produced could either be sold as a valuable calorific gas or utilised in further reactions (such as a water gas shift reaction) for the production of fuels for vehicles.
  • further reactions such as a water gas shift reaction
  • a strictly carbon neutral system is required then there is the option, in the system herein described, not to produce carbon monoxide from the combustor and any balance of carbon dioxide produced by the combustor may be directed elsewhere for further processing as discussed in more detail later.
  • the system includes a boiler for converting water to steam, the boiler having an inlet for the introduction of water and an outlet for steam.
  • the system further comprises a limekiln having an inlet for the introduction of limestone, a heater for heating limestone contained therein and an outlet for the release of calcium oxide and carbon dioxide, wherein the heater of the limekiln is in communication with the boiler outlet and is heated thereby.
  • Calcination of limestone by heating releases carbon dioxide and produces calcium oxide (referred to hereinafter as quicklime).
  • Quicklime produced by the heating of limestone may be collected from the limekiln and used to absorb carbon dioxide from the atmosphere. Such quicklime could be used in vehicle exhaust filters or along motorways or other areas of high carbon dioxide pollution in order to absorb the carbon dioxide.
  • the heater of the limekiln may be in communication with the boiler outlet so that steam from the boiler is supplied directly to the heater to facilitate the heating of limestone within the limekiln.
  • the heater of the limekiln may be in communication with the boiler outlet indirectly by way of other apparatus so that energy from the steam is supplied to the heater to facilitate the heating of limestone within the limekiln. In this way a portion of the steam output from the boiler may be used to generate electricity.
  • the heater of the limekiln may be an electrical resistance heating element powered by electricity.
  • the system may comprise a turbine-driven generator set connected to the boiler and means to direct steam from the boiler to the turbine of the generator set for the production of electricity for supply to the heater of the limekiln (where an electrical resistance heating element is provided) or elsewhere within the system. If the steam produced by the boiler is less than 900°C, this arrangement is particularly advantageous as it allows the limekiln to be supplied with sufficient heat for the calcination of limestone.
  • the heater of the limekiln is capable of receiving steam directly from the boiler and also comprises an electrical heating element to provide additional heat within the limekiln.
  • the steam produced by the boiler is less than 900°C
  • a portion of the steam produced by the boiler may be supplied directly to the heater to facilitate the heating of limestone within the limekiln with the remainder of the steam being directed to the turbine for the production of electricity to power the electrical heating element further to heat the limestone within the limekiln and to power the limekiln.
  • This excess can be sequestrated or used in making fuels or other processes on the basis that a proportional amount of calcium oxide produced by the process can be used in marine projects where twice the amount of carbon dioxide can be absorbed than the carbon dioxide produced by the systems of the present invention.
  • this excess carbon dioxide can be processed in the plant described herein to make the whole process carbon neutral if that is what is required.
  • the system of the present invention may further comprise an electrolysis plant arranged to receive excess carbon dioxide produced by the system and to convert the carbon dioxide into carbon and oxygen by electrolysis.
  • the splitting of carbon dioxide into carbon and oxygen is energy intensive, but by utilising energy derived from elsewhere in the system, the process may become viable.
  • the electrolysis plant and/or the chemical processing unit may be powered by electricity produced by the system.
  • the electrolysis plant and/or chemical processing unit may be operatively connected to the combustor to receive excess carbon dioxide produced by the burning of polymeric waste.
  • the electrolysis plant and/or chemical processing unit may be operatively connected to the limekiln to receive excess carbon dioxide and/or heat produced by the calcination of limestone.
  • the electrolysis plant and or chemical processing unit may be operatively connected to the turbine and/or the boiler to receive electricity or steam produced thereby to facilitate the conversion process.
  • the electrolysis plant and/or chemical processing unit may also be operatively connected to the processing plant to receive excess heat therefrom. Heat reclamation from the limekiln and the processing plant can therefore be used to assist the conversion process in the electrolysis plant and/or the chemical processing unit.
  • Additional processes being established include methods for combining carbon dioxide with a microorganism which extracts the carbon therefrom.
  • the carbon can then be processed with hydrogen and oxygen to produce a synthetic PHA-based biopolymer material which is formed into capsules and can subsequently be melted and formed into desired shapes.
  • the system and method of the present invention may be used to produce a fully carbon neutral and/or greenhouse neutral fuel in conjunction with the rest of the process.
  • the systems and methods of the present invention preferably serve to produce fuels, elements and compounds which are carbon neutral.
  • the system and process of the present invention may be utilised to supply this demand, in addition to the production of carbon neutral products.
  • excess carbon dioxide remaining following the production of carbon neutral fuel, by the system of the present invention may undergo co-electrolysis with other elements or compounds, such as water or glycerol.
  • other elements or compounds such as water or glycerol.
  • the system and methods of the present invention provide a choice. If complete carbon neutrality is desired this can be achieved.
  • the desired result is carbon neutral fuels and gasses with less of a concern being placed on the processing of greenhouse neutral gas formed as a minority by-product, then this can also be achieved; this is preferable to drilling and mining for fossil fuels which are neither greenhouse gas neutral nor carbon neutral.
  • the primary function of the system and process of the present invention is to facilitate the processing of waste plastic in a carbon neutral manner. As discussed above, the process may also be applicable to the low carbon processing of waste plastic rather than total neutrality. It is also feasible that additional waste products can benefit from processing by the system of the present invention.
  • One possible example of this is the waste residue which results from oil refining, namely petroleum coke (petcoke). Petcoke is an extremely damaging carbon polluting fuel which, at present, is exported from around the world to countries such as India and China, where it is burned for fuel. This combustion is one of the worst carbon polluters in the world.
  • the system of the present invention could additionally be utilised to transform petcoke into carbon monoxide which is a valuable calorific greenhouse neutral gas.
  • the system and process of the present invention allow conversion of plastic, along with the products of the combustion thereof, into carbon neutral fuel or gas, or into greenhouse gas neutral fuel or gas.
  • the present invention does not relate solely to the use of plastic feedstock as the fuel for the process, but it also relates to the production of carbon neutral and greenhouse gas neutral fuels and gases.
  • the entire purpose of the overall concept of the present invention is therefore to provide a whole cycle carbon neutral or greenhouse gas neutral product without the need for any ancillary offset or often questionable sequestration schemes.
  • FIG. 1 is a simplified diagram of the system for processing polymeric waste, which operates in accordance with the method of this invention
  • Figure 2 is a diagrammatic axial section through one embodiment of rotary kiln for the production of carbon dioxide from limestone;
  • Figure 3 is a diagrammatic axial section through an alternative embodiment of rotary kiln for the production of carbon dioxide from limestone;
  • Figure 4 is a diagrammatic axial section through yet another embodiment of kiln for the production of carbon dioxide from limestone; and Figure 5 is a diagrammatic axial view through the combustor and boiler of the system of Figure 1 .
  • the system 10 includes a combustor 11 which comprises burners 12 for burning waste plastic.
  • the combustor 11 includes an inlet 13 for the introduction of the plastic therein and a plurality of outlets.
  • One outlet 14 is provided to direct noxious particulates and other non-desired gases to a scrubber 14.
  • Another outlet 16 allows carbon monoxide 63 to be emitted and collected; carbon monoxide produced by the process can be sold as a valuable calorific gas or utilised in further reactions (such as a water gas shift reaction) for the production of fuels for vehicles.
  • the combustor 11 also includes a carbon dioxide regeneration arrangement 17 configured to re introduce carbon dioxide back into the combustor 11 .
  • the burning of polymeric waste in the combustor 11 produces carbon dioxide and the combustor 11 includes an outlet 18 to direct the carbon dioxide 50 away for further processing. Separation means (not shown) are provided to isolate the various gases following combustion and to direct these to the correct outlet. Such means are known in the art and are not discussed further here.
  • the system 10 also includes a processing plant 21.
  • the processing plant 21 is in close proximity with and is connected to the combustor 11 by an insulated pipe 22 to allow heat energy generated by the burning of plastic from within the combustor 11 to pass to the processing plant 21 .
  • the processing plant 21 includes an inlet 23 for the introduction of additional plastic waste and, in the particular embodiment shown, comprises a pyrolysis plant.
  • the processing plant 21 may alternatively comprise a gasification plant or other apparatus designed to heat material to facilitate decomposition, without combustion.
  • the processing plant 21 has an outlet 24 for synthetic gas (syngas) produced by the heating of waste plastics therein.
  • Synthetic gas (synfuel) produced by the heating of waste plastics therein.
  • Carbon dioxide produced by the combustor 11 may be transported by an insulated pipe (not shown) to the processing plant 21 and used to purge oxygen in the plant 21 in order further to facilitate to production of syngas.
  • Synthetic fuel (synfuel) may be obtained from the resultant syngas using common methods, as will be appreciated by those skilled in the art. This synthetic fuel can be used to replace fossil fuels.
  • the processing plant 21 also includes an outlet 25 for waste and gasses which are passed to an additional scrubber 15 and an additional outlet 26 for excess heat to be expelled from the plant 21 and utilised elsewhere, as described in more detail below.
  • the system 10 includes a boiler 29 having a water inlet 30 and two steam outlets 31 , 32.
  • the boiler 29 receives heat from the combustor 11 to convert water into steam.
  • a turbine-driven generator set 33 is arranged to receive a portion of the steam from one of the boiler outlets 32 and is configured to generate electricity 34 for supply elsewhere in the system 10.
  • a limekiln 37 is provided for the production of carbon dioxide from limestone. Calcination of limestone by heating releases carbon dioxide and produces calcium oxide (referred to hereinafter as quicklime).
  • the limekiln 37 is in communication with the boiler steam outlet 32 to provide heat to the inner chamber 38 of the limekiln 37 for the heating of the limestone and is also connected to the turbine generator set 33 to receive power therefrom, as discussed in more detail below.
  • the limekiln 37 is provided with an inlet 39 for the introduction of limestone, a heater 40 for heating the limestone, an outlet 41 for the release of carbon dioxide and an outlet 42 for the release of quicklime.
  • Quicklime produced by the heating of limestone may be collected from the limekiln 37 and used to absorb carbon dioxide from the atmosphere.
  • the calcining of limestone produces carbon dioxide.
  • the limekiln outlet 41 is configured to direct the carbon dioxide 50 away for further processing.
  • Excess carbon dioxide 50 produced by the system 10 can be processed in various ways. As shown in Figure 1 , the system 10 includes an electrolysis plant 45 arranged to receive excess carbon dioxide produced by the combustor 11 and by the limekiln 37 and to convert the carbon dioxide 50 into carbon and oxygen by electrolysis.
  • an electrolysis plant 45 arranged to receive excess carbon dioxide produced by the combustor 11 and by the limekiln 37 and to convert the carbon dioxide 50 into carbon and oxygen by electrolysis.
  • the system 10 also includes a chemical processing unit 46 arranged to receive excess carbon dioxide 50 produced by the combustor 11 and the limekiln 37 and to convert the carbon dioxide 50 to carbon monoxide and oxygen or carbon monoxide and hydrogen.
  • a chemical processing unit 46 arranged to receive excess carbon dioxide 50 produced by the combustor 11 and the limekiln 37 and to convert the carbon dioxide 50 to carbon monoxide and oxygen or carbon monoxide and hydrogen.
  • the electrolysis plant 45 and the chemical processing unit 46 are powered by electricity 34 produced by the turbine-driven generator set 33. Either or both of these processes can be utilised to process excess carbon dioxide 50.
  • the system 10 also includes a plastic product processing plant 47. Additionally, or alternatively, excess carbon dioxide 50 can be processed in the plastic processing plant 47 to produce carbon-based products, using known methods.
  • Residual heat 48 which has been drawn from the limekiln 37 and from the processing plant 21 and any excess steam 49 produced by the boiler 29 may also be transferred to one or more of the electrolysis plant 45, the chemical processing plant 46 or the plastic product processing plant 47 to provide additional heat and/or steam for the further processing of carbon dioxide 50 produced by the combustor 11 and by operation of the limekiln 37.
  • the combustor 11 has a base 52 on which is rotatably mounted a platform 53.
  • a motor 54 is provided within the base 52 drivingly connected to the platform 53 to cause the intermittent rotation thereof, one third of a revolution at a time, to allow the performance of a batch process.
  • the platform 53 supports a partition wall 55 which divides the inner space above the platform 53 into three compartments 56 bound by the outer peripheral wall of the combustor 11 .
  • the partition wall 55 is of a suitable reinforced material capable of withstanding the high temperatures likely to be encountered during operation of the apparatus.
  • the compartments 56 are configured to rotate sequentially into three distinct sections, an introduction section 57, a combustion section 58 and a gas processing section 59.
  • the boiler 29 is located in the apparatus above the partition wall 55 and includes the water inlet 30.
  • the volume within the apparatus and above the boiler is divided by a further partition wall 64 such that steam generated by the boiler 29 leaves the apparatus through the two steam outlets 31 , 32, having the functionality described hereinafter.
  • the introduction section 57 contains the inlet 13 for the introduction of waste plastic to the compartment 56 for the time being aligned with that inlet
  • the burners 12 are located at the upper end of the combustion section 58 and are arranged to burn content in the compartment 56 for the time being therebelow, or primarily therebelow, in the course of rotation of the platform 53.
  • the boiler 29 being above the burners 12 facilitates the transfer of heat from the combustion to the boiler 29, thereby to heat water in the boiler 29.
  • the burning of the plastic produces energy, in the form of heat, and carbon dioxide rich gasses.
  • the compartments 56 rotate from the plastic introduction section 57 to the combustion section 58.
  • a duct 66 passes through the boiler 29 and communicates with the combustion section 58, to transfer to the space above the boiler but separated from the steam, the combustion gasses to remove any noxious particulates and other non-desired gases. Those leave the apparatus and pass to the scrubber
  • the remaining gasses from the scrubber (primarily carbon dioxide 50) are passed through an inlet 60 into the gas processing section 59 and also the combustion section 58 of the combustor 11.
  • An outlet 16 for carbon monoxide is provided through the apparatus wall in the gas processing section 59.
  • the transfer of combustion gasses through the scrubber and back into the combustion section 58 enables carbon dioxide to be recirculated and thus facilitates a controlled slow burn of plastic waste.
  • the burning of plastics in an oxygen-controlled environment produces a carbon dioxide and carbon monoxide mix.
  • the production of further carbon monoxide from this mix in this third gas processing section 59 is facilitated by the burnt plastic residue that will exist in this section 59.
  • Separation means are provided to isolate the various gases following combustion and to direct these to the correct outlet. Such means are known in the art and are not discussed further here.
  • the carbon monoxide 63 leaves the apparatus through outlet 16 and the carbon dioxide 50 passes out of outlet 18 for further processing.
  • Carbon monoxide 63 produced by the process can be sold as a valuable calorific gas or utilised in further reactions (such as a water gas shift reaction) for the production of fuels for vehicles.
  • the burning of plastics does not generally produce a large quantity of char but the regeneration of carbon dioxide 50 into the gas processing section 59 serves to produce a limited or controlled oxygen environment which will result in the production of more carbon monoxide 63 as carbon dioxide mixes with the burnt plastic residue in that environment in section 59 as above. Excess carbon dioxide can however be processed further as explained hereinbefore.
  • an additional process may be included to increase the amount of char and carbonate material in order to form greater quantities of carbon monoxide and less carbon dioxide.
  • Such a process may involve the introduction of petcoke 51 to the gas processing section 59.
  • the mix of carbon dioxide 50 and carbon monoxide 63 from the combustion section 58 will pass over the char and petcoke mix to form more carbon monoxide.
  • the apparatus may be configured to enable residue and char from the processing plant 21 to be introduced into the gas processing section 59.
  • Such apparatus may be arranged to deposit the material into the top of the gas processing section 59 by a sealed hopper (not shown) contemporaneously with the injection of the combustion gases therein.
  • the hopper may be purged of oxygen before the material is deposited.
  • the carbon dioxide 50 and carbon monoxide 63 gasses may be directed from the scrubber 14 through an insulted pipe to an independent chamber 62 which also communicates with the processing plant 21 and is configured to receive the residue and char remaining after the processing (for example, pyrolysis) in the plant 21 is complete. This will result in more carbon monoxide 63 being produced. Petcoke 51 could also be added to this independent chamber 62 to result in the production of even more carbon monoxide 63. These processes utilise the material remaining in the processing plant 21 and this ensure that this material is not wasted. Any residuary carbon dioxide and carbon monoxide gas mix may then return to the gas processing section 59 of the combustor 11 or be independently processed to separate any carbon dioxide 50 from the heavy carbon monoxide biased mix.
  • the limekiln 37 comprises a generally cylindrical vessel 67 having an inner chamber 38 mounted coaxially therein.
  • the vessel 67 is supported on three pairs of horizontally-spaced rollers 68 with the vessel axis inclined at a small angle to the horizontal.
  • At least one roller 68 of each pair includes a motor (not shown) to effect rotation of the vessel 67.
  • the inlet 39 for the introduction of limestone is provided at the raised end of the limekiln 37, that inlet 39 being provided with a gate valve 69.
  • a stationary inlet duct 70 also provided with a gate valve 71 is arranged so that on rotation of the vessel 67, the inlet 39 will come into register with the duct 70 when the inlet 39 is uppermost. When in register and both gate valves 69, 71 are opened, limestone may pass from the duct 70 to the inlet 39 and so into the vessel 67.
  • the outlet pipe 41 is provided at the raised end of the kiln 37 for carbon dioxide generated within the vessel 67.
  • a gas-type rotary joint (not shown) is arranged between the vessel 67 and the pipe 41 and a valve (also not shown) is disposed within the pipe 41 to control the release of carbon dioxide.
  • the inner chamber 38 of the limekiln 37 is formed from stainless steel reinforced as necessary to withstand the tumbling of the limestone within the vessel 67.
  • the heater 40 is a resistive heating element disposed within the chamber 38 and electricity supply cables are connected to that element and are provided with electrical, thermal and mechanical insulation to allow the supply of electricity 34 to the element through an external control unit (not shown).
  • the turbine and generator set 33 is arranged to receive steam from the boiler outlet 32 and is connected to the control unit so that the heater 40 may be powered from the set to raise the temperature within the limekiln sufficiently to cause calcination of the limestone.
  • an automatically-operating one-way gate at the steam entrance of the rotary kiln serves to prevent steam exiting the limekiln 37 through the inlet 39, in the event of a blowback.
  • FIG. 4 An alternative form of kiln 43 is shown in Figure 4.
  • This kiln comprises a generally cylindrical stationary casing 77 having a furnace 78 housed therein.
  • the furnace 78 includes a rotatable annular outer vessel 79 formed by coaxial inner and outer cylindrical walls 82, 81.
  • a reaction chamber 82 is defined between the inner cylindrical wall 82 and the outer cylindrical wall 81 and is arranged to receive limestone to be calcined.
  • the casing 77 includes an annular gas containment area 83 and insulation 84 is provided between the containment area 83 and the furnace 78.
  • the casing 77 and outer vessel 79 may be constructed of a conventional refractory material, reinforced as necessary, in a manner well known to those skilled in the art, but further use may be made of the specialist materials, as hereinbefore discussed (or other materials) if particular longevity is required for specific furnaces.
  • the furnace 78 has, at one end (the first end 85), an inlet 86 for the introduction of limestone, that inlet 86 being provided with a mechanical feed system 87, which will be explained in more detail below.
  • the outer vessel 79 of the furnace 78 is horizontally positioned such that the other end of the furnace (the second end 88) is at the same height as the first end 85 and includes a distal protrusion 89 for the introduction of limestone into the reaction chamber 82.
  • the inner cylindrical wall 80 defines an inner chamber 90.
  • Heating means 91 is disposed within the inner chamber 90.
  • the heating means 91 is an electrical resistance heating element arranged to be supplied with electricity 34 derived from the turbine generator set 33.
  • the heating element 91 extends in an annular or a half annular configuration and is located against the bottom half of the furnace, against the inner cylindrical wall 80. In practice, limestone will gather in the lower half of the outer vessel 79 as it is conveyed along the reaction chamber 82.
  • the heating element 91 extends along the length of the outer vessel 79 in order to maximise heat transfer.
  • the electrical resistance heating element 91 is electrically powered to raise the temperature within the furnace 11 .
  • Electricity supply cables 92 are connected to that element and are provided with electrical, thermal and mechanical insulation to allow the supply of electricity 34 to the element.
  • the element 91 is connected to the turbine generator set 33 to receive power therefrom.
  • the apparatus includes a curved blade 93 within the reaction chamber 82 arranged to channel limestone introduced into the reaction chamber 82 toward and along the inner cylindrical wall 80.
  • the curved blade 93 is mounted to both the inner and outer cylindrical walls 80, 81 .
  • the blade 93 extends the full axial length of the outer vessel 79, including along the distal protrusion 89 thereof and is curved to define a spiral shape along the length of the reaction chamber 82; this arrangement provides a defined path for the limestone.
  • the presence of the blade 93 ensures that limestone is conveyed along the path in measured amounts.
  • the processing of the limestone is thereby carried out in a uniform fashion facilitating full and even processing.
  • the blade 93 is also curved transversely to define a concave surface for the channelling of limestone towards the heating element. The spacing between adjacent turns in the spiral blade 93 is uniform as too is the pitch of the blade.
  • a plurality of outlets 94 in the form of gas valves, are provided, equidistantly spaced around the outer cylindrical wall 81 of the outer vessel 79, for the release of carbon dioxide. Alternatively, or additionally, these could be gas permeable membranes.
  • the gas valves are defined in the outer cylindrical wall 81 of the outer vessel 79 and openings 95 are provided in the insulation 84 to allow carbon dioxide to escape from the reaction chamber 82 to the containment area 83 of the casing 77.
  • a fan 96 is provided adjacent the containment area 83 of the casing 77 to assist the drawing away of carbon dioxide from the vessel 79.
  • FIG. 1 shows a further embodiment which combines the heater arrangements of the embodiments of both Figures 2 and 3.
  • the heater 40 comprises a resistive heating element connected to an electricity supply cable and additionally steam from the outlet of the boiler 32 is passed directly to the inner chamber 38 to provide heat to the limekiln.
  • Such an arrangement may be used to ensure that sufficient heat may be supplied to the limekiln 37 for the heating of limestone therein and also to power actual operation of the limekiln 37.
  • a door 75 which, when the inlet 39 is in register with the inlet duct 70, comes into register with an outlet duct 76, to enable the removal of quicklime produced by the calcination of limestone within the kiln.
  • Carbon dioxide produced by the combustion of synfuel, formed by the processing plant 21 can be absorbed by quicklime expelled from the limekiln 37. As such, synfuel produced by the processing plant 21 can be considered carbon neutral.
  • the present invention employs combustion to address the problems associated with polymeric waste but does so in an environmentally and efficient way.
  • the invention makes use of the energy produced during combustion to facilitate processing of excess carbon dioxide, which would otherwise be emitted as a by-product, into useful carbon neutral or greenhouse neutral gases or into carbon neutral products.
  • the system and process of the present invention thus serves to address the problems associated with processing of waste plastics.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Sustainable Development (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Treating Waste Gases (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention concerne un système et un procédé destinés au traitement de déchets polymères, et en particulier au traitement neutre en carbone et efficace de ces déchets. Le système (10) comprend une chambre de combustion (11) conçue pour brûler des déchets polymères et une installation de traitement (21) reliée fonctionnellement à la chambre de combustion (11) pour recevoir de l'énergie thermique de cette dernière. L'installation de traitement (21) est conçue pour ainsi chauffer des déchets polymères supplémentaires, sans combustion, de façon à produire un gaz de synthèse, ou un combustible synthétique, ou de l'huile combustible. Le système (10) comprend par ailleurs éventuellement une chaudière (29), comportant une entrée (30) permettant l'introduction d'eau et une sortie (31, 32) permettant la libération de vapeur, la chaudière (29) étant fonctionnellement reliée à la chambre de combustion (11) de façon à en recevoir de l'énergie thermique et à chauffer l'eau pour produire de la vapeur et étant reliée fonctionnellement à l'installation de traitement (21) de façon à lui transférer la vapeur. Le système (10) peut en outre comprendre un four à chaux (37) comportant une entrée (39) permettant l'introduction de calcaire, un élément de chauffe (40) destiné à chauffer le calcaire contenu en son sein, et une sortie (41, 42) prévue pour la libération de dioxyde de carbone et d'oxyde de calcium, l'élément de chauffe (40) du four à chaux (37) étant en communication avec la sortie de chaudière (32) et étant chauffé directement ou indirectement par de la vapeur provenant de cette dernière. Le procédé de traitement de déchets polymères selon la présente invention utilise le système (10). Le système et le procédé selon la présente invention permettent la conversion de plastique, conjointement avec les produits de sa combustion, en combustible ou en gaz carbo-neutre, ou en combustible ou en gaz ne produisant pas d'émissions nettes de gaz à effet de serre.
EP20812399.2A 2019-10-22 2020-10-21 Dispositif de correction de front d'onde de réfraction Pending EP4048454A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB1915286.7A GB2588414B (en) 2019-10-22 2019-10-22 Processing of polymeric waste
PCT/GB2020/052640 WO2021079105A1 (fr) 2019-10-22 2020-10-21 Système et procédé de traitement de déchets polymères

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EP4048454A1 true EP4048454A1 (fr) 2022-08-31

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Publication number Priority date Publication date Assignee Title
US4919686A (en) * 1986-10-14 1990-04-24 Co-Gen Power Corporation Process for the pyrolytic production of synthetic gas
US7500997B2 (en) * 2002-02-05 2009-03-10 The Regents Of The University Of California Steam pyrolysis as a process to enhance the hydro-gasification of carbonaceous materials
KR100787958B1 (ko) * 2004-09-25 2007-12-31 구재완 폐합성 고분자화합물의 연속식 열분해 시스템

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GB201915286D0 (en) 2019-12-04
GB2588414B (en) 2024-04-03
GB2588414A (en) 2021-04-28

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