KR102881521B1 - High-purity (hydrogen maximization) gasification production system for pyrolysis gas reforming of waste plastics containing large amounts of PVC using steam plasma gasification melt reforming Device - Google Patents

Abstract

The present invention comprises: an input device for receiving and compressing a material that is waste plastic waste including waste PVC; a transfer heating dryer that is configured to indirectly heat the material received from the input device with hot air; a melter that is configured to receive the material transferred from the transfer heating dryer and vertically transport it, melt it by indirect heating of the hot air and maintain it in a slurry state; a pyrolysis dechlorinator that is heated by hot air that indirectly heats the material transferred from the melter and steam that directly heats it, the flow of the hot air and the direction of transport of the material are the same, and is configured to separate and remove chlorine or hydrogen chloride in the material in a liquid state by high temperature heat; a pyrolysis gas generator that heats the material transferred from the pyrolysis dechlorinator to a temperature higher than the temperature of the pyrolysis dechlorinator and thermally decomposes it to separate a gas containing hydrogen; It is characterized by including a steam plasma gasification melting reforming device provided downstream of the pyrolysis gas generator, which gasifies and melts slags residual carbon and incombustible matter transferred from the pyrolysis gas generator, and removes polymer impurities including carbon or tar contained in the gas generated from the pyrolysis gas generator.
Accordingly, according to the present invention, the chlorine component contained in the combustible waste that can be utilized as waste fuel (combustible waste such as household, industrial, waste plastic, designated waste, or mixed waste plastic) made of combustible waste plastic including PVC is removed through thermal decomposition conditions with improved efficiency by maintaining atmospheric pressure and constant temperature conditions, and the purified high-purity synthesis gas after decomposing the impurities such as fixed carbon and tar formed in the thermal decomposition process through steam plasma gasification melting can be utilized as a monthly fuel for hydrogen production, etc., and the device can be made compact and the amount of hydrogen generated can be increased to produce a high value-added synthesis gas raw material.

Description

High-purity (hydrogen maximization) gasification production system for pyrolysis gas reforming of waste plastics containing large amounts of PVC using steam plasma gasification melt reforming device

The present invention relates to a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reformer, and more specifically, to a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reformer, which has an improved structure so that chlorine components in combustible waste that can be used as waste fuel (combustible waste such as household, industrial, waste plastic, designated waste, or mixed waste plastic) containing a large amount of PVC (when it contains 2 wt% or more and cannot be used as a renewable fuel) are efficiently removed by pyrolysis, and carbon generated (residual) by pyrolysis, etc. can further generate synthesis gas (CO) by utilizing a steam plasma gasification melting and reforming process, and polymer tar, etc. contained in low-temperature pyrolysis gas is completely decomposed, and at the same time, hydrogen (H ₂ ) production rate is increased and a high value-added synthesis gas raw material can be produced.

In all areas, including the way people live, industrial production, and the medical industry, unnecessary waste or waste is generated after productive activities.

There are various methods for handling this waste, including landfilling, where waste slowly stabilizes as it decomposes; incineration, which burns at high temperatures to reduce its volume and utilizes the heat generated; separating waste for reuse or recycling; and discharging waste and other waste into the ocean, some distance from land. Among these methods, ocean discharge is increasingly being banned internationally.

These days, the problem of waste plastic disposal is causing serious environmental pollution, but the method of converting waste plastic into fuel utilizes the heat and gas generated during the combustion process of waste plastic.

This energy conversion of waste plastics can replace fossil fuels and reduce the amount of methane gas generated from landfill waste, which can help address climate change due to the high global warming potential of methane gas (biogas) (21 times that of carbon dioxide). However, it also causes secondary global pollution such as carbon dioxide and fine dust.

Accordingly, in developed countries, efforts are actively being made to reduce greenhouse gases through waste-to-energy conversion, such as converting combustible waste into solid fuel (RDF, Refuse-derived Fuel) and organic waste into biogas.

In line with this trend, related technologies are being proposed domestically as well, and the inventor of the present invention has proposed numerous technologies in related fields, including references, and is currently making proposals in various fields.

A technology has also been proposed to generate electricity by utilizing the heat generated during the pyrolysis or incineration of combustible renewable fuels (including unsolidified and liquid) that can be utilized as organic waste fuels (e.g., biomass, household, industrial, and plastic waste). Most current methods utilize the heat generated during pyrolysis and other processes to produce steam, which is then used to power a steam turbine to generate electricity.

However, the conventional technology has the problem of generating a large amount of fine dust as well as various toxic gases including dioxin during the process of incinerating such combustible renewable fuel, which aggravates air pollution, and has low efficiency, which increases the amount of _CO2 generated per unit of electricity produced, thereby aggravating global warming.

Accordingly, the heat generated from the gas generated through gas combustion was recovered by first pyrolysis gasification to induce complete combustion during the combustion process and reused for steam power generation, etc.

And, in recent years, the technology has advanced to the point where it is highly desirable to produce clean raw materials (liquid, gas-gas) by pyrolyzing or gasifying combustible renewable fuels and recycle the raw materials, which is efficient and environmentally friendly.

However, these wastes or recycled fuels often contain large amounts of PVC, and the current standard for recycled fuel (SRF) is a maximum chlorine content of 2 wt%. Therefore, waste with a chlorine content exceeding 2 wt% cannot be reused as recycled fuel. The PVC must be removed to reduce the chlorine content to 2% or less. Furthermore, waste plastics containing large amounts of PVC pose significant challenges when used as gas or liquid raw materials, as they exacerbate environmental pollution and contribute to equipment corrosion.

Furthermore, recycled plastic fuels are diverse in type, composition, and additives, making their removal economically problematic. Therefore, it's best to effectively remove unnecessary components from recycled fuels before using them as clean fuels. To achieve this clean fuel use, effectively removing chlorine is crucial.

Current literature indicates that chlorine in waste PVC is separated from 180°C and above, and nearly all of it is separated into hydrogen chloride at around 350°C. Furthermore, at low temperatures, separation efficiency is very low, while at high temperatures, organic components are separated and discharged mixed with chlorine.

To address these issues and efficiently separate and discharge only the chlorine component at lower temperatures (below 300℃), it is desirable to incorporate several additional improvements to the pyrolysis device. Such a device effectively separates chlorine at lower temperatures, thereby increasing the economic value of recycled raw materials, minimizing environmental pollution, and enabling the use of inexpensive energy, thereby increasing economic value. Furthermore, it allows for the economical recycling of the generated high-concentration hydrogen chloride.

Meanwhile, it would be more desirable to efficiently decompose tar or fine fixed carbon generated during the process of pyrolysis and gasification of waste fuel into _H2 and CO or _CO2 , which are high-calorie gases (nitrogen is generated in gasification using air plasma or air, but is not generated at all when using oxygen or steam).

[References]

Patent Registration No. 10-0899185 (Published on May 26, 2009)

Patent Publication No. 10-2010-0019316 (published on February 18, 2010)

Patent Publication No. 10-2334096 (Published on December 3, 2021)

Patent Registration No. 10-1182485 (Published on September 12, 2012)

The purpose of the present invention is to provide a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming, which has a steam plasma gasification melting reforming device that removes chlorine components contained in combustible waste that can be utilized as waste fuel (combustible waste such as household, industrial, waste plastic, designated waste, or mixed waste plastic) made of combustible waste plastic including PVC through pyrolysis conditions with improved efficiency by maintaining atmospheric pressure and constant temperature conditions, and decomposes impurities such as fixed carbon and tar formed in the pyrolysis process through steam plasma gasification melting, and then uses the purified high-purity synthesis gas as a raw material for hydrogen production, etc., and which can compactize the device and increase the amount of hydrogen produced to produce a high-value-added synthesis gas raw material.

In addition, another object of the present invention is to provide a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reforming device capable of producing a purified synthetic gas clean raw material with high efficiency by producing hydrogen after waste fuel is pyrolyzed and gasified and then undergoing a process such as purification to be used in a gas engine or turbine.

In addition, another object of the present invention is to provide a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reforming device that can incorporate the advantages of a hot air circulation indirect heating pyrolysis furnace.

The purpose of the present invention is to provide a gasification system for separating and removing chlorine (hydrogen chloride) contained in PVC of waste plastic having a steam plasma gasification melting reformer, comprising: an input device for receiving and compressing a material which is waste plastic waste including waste PVC; a transfer heating dryer which is provided to indirectly heat the material received from the input device with hot air; a melter which is provided to receive the material transferred from the transfer heating dryer and vertically transport it, melt it by indirect heating of the hot air and maintain it in a slurry state; a pyrolysis dechlorinator which is provided to heat the material transferred from the melter by hot air which indirectly heats it and steam which directly heats it, and the flow of the hot air and the direction of transport of the material are the same so as to increase the residence time within a set temperature range of a dechlorination region and to efficiently separate and discharge chlorine and hydrogen chloride; a pyrolysis gas generator which heats the material transferred from the pyrolysis dechlorinator to a temperature higher than the temperature of the pyrolysis dechlorinator and thermally decomposes it to separate a gas containing hydrogen; This is achieved by a raw material production system characterized by including a steam plasma gasification melting reforming device provided downstream of the pyrolysis gas generator, which gasifies and melts slags residual carbon and incombustible matter transferred from the pyrolysis gas generator and removes polymer impurities including carbon or tar contained in the gas generated from the pyrolysis gas generator.

In addition, in the above steam plasma gasification melting reforming device, it is preferable that steam and plasma act to gasify carbon so that carbon is changed into water gas (main component H ₂ + CO) by dissociated water (2H ₂ + O ₂ ) at high temperature.

In addition, it is preferable that the steam has a temperature in the range of 200 to 500°C, and that the temperature by the arc energy supplied from the plasma has a temperature in the range of 3000 to 5000°C.

In addition, it is preferable that the steam plasma gasification melting reforming device includes a main body for receiving the transported incombustible matter and gas, a torch unit coupled to the main body so as to supply steam and plasma into the interior of the main body, and an input unit for guiding the incombustible matter generated from the pyrolysis gas generator into the main body.

In addition, the torch part includes a steam supply port for supplying steam and a plasma supply torch for supplying plasma, wherein the plasma supply torches are provided in multiple numbers and are spaced apart from the center of the main body at the same distance and are coupled to the main body, and it is preferable that the steam supply port is coupled to the main body so as to face the center of the main body.

In addition, it is preferable that the plasma supply torches are provided in multiple numbers, and include the steam supply port penetrating through the center of each plasma supply torch, or that the steam supply port is formed as an outer double pipe of each plasma supply torch.

In addition, the steam plasma gasification melting reforming device preferably includes a main body for receiving the transferred fixed carbon and non-combustible material, and a torch unit coupled to the main body so as to supply steam and plasma into the interior of the main body, and further includes a high-temperature liquid transfer pump for transferring liquid fuel generated from the pyrolysis gas generator to the main body.

Accordingly, according to the present invention, a high-purity synthesis gas can be produced by removing chlorine components contained in combustible waste that can be used as waste fuel (combustible waste such as household, industrial, waste plastic, designated waste, or mixed waste plastic) made of combustible waste plastic including PVC through improved pyrolysis conditions by maintaining atmospheric pressure and constant temperature conditions, and by decomposing impurities such as fixed carbon and tar formed in the pyrolysis process through steam plasma gasification melting, and using the purified high-purity synthesis gas as a raw material for hydrogen production, etc., and by compacting the device and increasing the amount of hydrogen produced, thereby producing a high-value-added synthesis gas raw material, a system for producing high-purity (hydrogen maximization) raw material by reforming pyrolysis gas of PVC-rich waste plastic can be provided.

In addition, a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reforming device capable of producing purified synthetic gas clean raw materials with high efficiency by producing hydrogen after waste fuel is pyrolyzed and gasified and then undergoing a process such as purification, which can be used in a gas engine or turbine, or can be used in a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reforming device capable of producing purified synthetic gas clean raw materials with stable quality with high efficiency by producing hydrogen.

In addition, a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming can be provided, which has a steam plasma gasification melting reforming device that can incorporate the advantages of a hot air circulation indirect heating pyrolysis furnace.

Figure 1 is a flow chart of a raw material production system according to one embodiment of the present invention;
Figure 2 is a conceptual diagram three-dimensionally arranging a part of the configuration of Figure 1.
Figure 3 is a cross-sectional view and a partially enlarged view of a pyrolysis dechlorinator.
Figure 4 is a cross-sectional view and a cross-sectional view of a thermal dechlorinator,
Figure 5 is a cross-sectional view and a partially enlarged view of a thermal dechlorinator according to another embodiment of the present invention.
Figure 6 is a graph of thermal decomposition characteristics by type of plastic.
Figure 7 is a plan view and cross-sectional view of a steam plasma gasification melting reforming device.
Figures 8a to 8c are cross-sectional views for explaining a method of supplying steam from a torch section.
Figure 9 is a conceptual diagram for explaining the operating process of steam plasma gasification melting.
Figure 10 is a flow chart for explaining the operation process of the raw material production system.
Figure 11 is a schematic flowchart for comparing the raw material production system according to the present invention with conventional technologies.

Hereinafter, a PVC-rich waste plastic pyrolysis gas reforming high-purity (hydrogen maximization) raw material production system (100, hereinafter referred to as “raw material production system”) having a steam plasma gasification melting reforming device according to one embodiment of the present invention will be described in detail with reference to FIGS. 1 to 11.

FIG. 1 is a flow chart of a raw material production system according to an embodiment of the present invention, FIG. 2 is a conceptual diagram three-dimensionally arranging a part of the configuration of FIG. 1, FIG. 3 is a cross-sectional view and a partially enlarged view of a pyrolysis dechlorinator, FIG. 4 is a cross-sectional view and a partially enlarged view of a pyrolysis dechlorinator, FIG. 5 is a cross-sectional view and a partially enlarged view of a pyrolysis dechlorinator according to another embodiment of the present invention, FIG. 6 is a graph of pyrolysis characteristics by type of plastic, FIG. 7 is a plan view and a cross-sectional view of a steam plasma gasification melting reforming device, FIGS. 8a to 8c are cross-sectional views for explaining a method of supplying steam from a torch unit, FIG. 9 is a conceptual explanatory diagram for explaining the operating process of steam plasma gas and melting, FIG. 10 is a flow chart for explaining the operating process of a raw material production system, and FIG. 11 is a schematic flow chart for comparing a raw material production system according to the present invention with conventional technologies.

The steam plasma gasification melting reforming device (200) described below can be applied to a pyrolysis process that gasifies, melts, and reforms residues containing fixed carbon generated in the process of pyrolyzing various types of combustible waste raw materials and impurities containing tar in the pyrolysis gas using steam plasma. Among these pyrolysis processes, a process of pyrolyzing chlorine (hydrogen chloride) contained in waste plastics that cannot be used as renewable fuel because they contain 2 wt% or more of PVC will be described below as an embodiment of the present invention.

Before describing the present invention in more detail, it should be noted that the present invention is susceptible to various modifications and various forms, and thus, embodiments (or examples) will be described in detail herein. However, this is not intended to limit the present invention to a specific disclosed form, but rather to encompass all modifications, equivalents, and alternatives falling within the spirit and scope of the present invention.

In each drawing, the same reference signs, especially the tens and units digits, or the tens, units digits, and alphabets, indicate parts having the same or similar functions, and unless otherwise specified, the parts indicated by each reference sign in the drawing are understood to be parts that comply with these standards.

In addition, in each drawing, the components are expressed in an exaggerated (or thick) or simplified (or thin) size or thickness for convenience of understanding, but the scope of protection of the present invention should not be interpreted as being limited by this.

The terminology used in this specification is only used to describe specific implementations (modes, aspects) (or examples) and is not intended to limit the present invention. The singular expressions include plural expressions unless the context clearly indicates otherwise. In this application, it should be understood that terms such as ~comprises~ or ~consists of~ specify that a feature, number, step, operation, component, part or combination thereof described in the specification is present, but do not exclude in advance the possibility of the presence or addition of one or more other features, numbers, steps, operations, components, parts or combinations thereof.

Unless otherwise defined, all terms used herein, including technical or scientific terms, have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. Terms defined in commonly used dictionaries should be interpreted as having a meaning consistent with their meaning in the context of the relevant technology, and will not be interpreted in an idealized or overly formal sense unless explicitly defined herein.

A chlorine separation and removal gasification system (1000) according to the present invention relates to the separation and removal gasification of chlorine (hydrogen chloride) contained in PVC of waste plastics having a steam plasma gasification melting reformer, and comprises: an input device (10) for receiving and compressing a material, which is waste plastic waste including waste PVC; a transfer heating dryer (110) configured to indirectly heat the material received from the input device (10) with hot air; a melter (120) configured to receive the material transferred from the transfer heating dryer (110) and vertically transport it, melt it by indirect heating of the hot air, and maintain it in a slurry state; a pyrolysis dechlorinator (130) configured to heat the material transferred from the melter (120) by hot air that indirectly heats it and steam that directly heats it, and the flow of the hot air and the transport direction of the material are the same, so as to increase the residence time within a set temperature range of a dechlorination region, and to efficiently separate and discharge chlorine and hydrogen chloride; It is preferable to include a pyrolysis gas generator (140) that heats the material transferred from the pyrolysis dechlorinator (130) to a temperature higher than that of the pyrolysis dechlorinator (130) to thermally decompose the material and separate a gas containing hydrogen; and a steam plasma gasification melting reforming device (200) provided downstream of the pyrolysis gas generator (140) that gasifies and melts slags residual carbon and incombustible matter transferred from the pyrolysis gas generator (140) and removes polymer impurities containing carbon or tar contained in the gas generated from the pyrolysis gas generator (140).

Hereinafter, for convenience, the material or raw material includes waste plastic containing waste PVC, and is a general term for what is transported or left inside the input device (10), the transfer drying heater (110), the pyrolysis dechlorinator (130), the pyrolysis gas generator (140), the steam plasma gasification melting reformer (200), etc. In addition, the material may include a solid or liquid form and may include bubbles contained in the liquid. In other words, the material includes waste, and among the waste, it also includes waste containing waste plastic.

The input device (10) preferably includes a hopper body (11) for receiving materials including waste plastic to be processed for transporting them to a subsequent process, and an extrusion means (13) of a screw type or a pneumatic or hydraulic pushing type (e.g., a pusher type) for pressurizing the materials received at the bottom of the hopper body (11) and transporting them to the subsequent process. If necessary, a configuration for discharging blockages, etc. in the extrusion means (13) may be further included, and the extrusion means (13) may rotate forward (forward) and backward (backward).

In the following configurations (20, 30, 110, 120, 130, 140), for convenience, the screw-type extrusion means or conveying means is driven by a driving means including a motor or reducer that is operated by an externally applied power source, and a description of such driving means is omitted below.

The transfer heating dryer (110) is connected to the rear end of the input device (10) and heats and dries the transferred material and transfers the material to the melter (120) connected to the rear end. It is composed of a long cylindrical drying heating body (111) capable of receiving and transferring the material, and a drying heating jacket (113) surrounding the drying heating body (111) so that hot air can pass through and transfer heat to the drying heating body (111). A rotating screw-type transfer means capable of transferring the material is provided inside the drying heating body (111).

The heat source supplied to the drying heating jacket (113) of the transfer heating dryer (110) is hot air that has passed through the pyrolysis gas generator (140) - melter (120), which heats the material at room temperature before it is transferred to the melter (120), and as the material is heated, moisture contained in the material is removed to heat and dry the material.

Meanwhile, as mentioned in the prior art, the present invention is to remove and separate chlorine (hydrogen chloride) present in waste PVC.

First, when looking at the thermal decomposition characteristics of waste synthetic resins, as shown in Fig. 6, unlike other waste plastics, in the case of PVC, thermal decomposition starts at a low temperature of 200℃ or lower, is completed at around 350℃ in the first stage, and is promoted in the second stage near 400℃.

In the case of PVC, it can be seen that chlorine is separated and emitted as hydrogen chloride at a low temperature of around 250℃, and this is expressed in the structural formula in [Table 1].

Looking at the “thermolysis characteristics of waste synthetic resin” graph in Figure 6, in the case of PVC, decomposition and removal of hydrogen chloride generally occur at 200 to 350°C, but there is a problem that the generation of other organic components is accelerated when the temperature exceeds 300 to 350°C.

Here, the fact that the decomposition temperature of hydrogen chloride in PVC is in the range of 200 to 350°C is not because the actual decomposition temperature is different, but because the internal conditions of the space where thermal decomposition occurs are not formed under the same conditions. In other words, if all treatment processes, processes, and machines are under the same conditions, the separation and discharge of hydrogen chloride can be achieved in a very narrow temperature range. In other words, if temperature is applied evenly to all parts instantaneously, chlorine (hydrogen chloride) formed in the same ring is decomposed simultaneously at a constant temperature. Therefore, it can be seen that forming the temperature conditions inside the thermal dechlorinator (130) evenly and maintaining the set residence time are very important factors.

division Polymer structural formula Before separation After separation

The melter (120) is configured to melt the material transferred from the transfer heating dryer (110) and is composed of a vertical type long cylindrical melting body (121) and a melting jacket (123) surrounding the melting body (121).

The melting body (121) is provided in a long cylindrical shape capable of receiving and transporting materials, and the melting jacket (123) is structured to surround the melting body (121) so that heat can be transferred to the melting body (121) as hot air passes through it. Inside the melting body (121), a rotating screw-type transport means capable of transporting materials is provided.

Hot air that has passed through the pyrolysis gas generator (140) - pyrolysis dechlorinator (130) is supplied to the melting jacket (123), and in order to keep the temperature of the pyrolysis dechlorinator (130) constant, it is preferable that some of the hot air pass through the bypass automatic damper (131) to bypass the pyrolysis dechlorinator (130). The control of the bypass automatic damper (139) can be controlled by a control unit (not shown) based on a temperature sensor that detects the temperature of the pyrolysis dechlorinator (130).

The material that stays and is transferred to the melting body (121) is heated and begins to melt by heat transfer from the melting jacket (123), and gases such as chlorine can be separated from the material. The separated gases such as chlorine are captured and discharged to a high-concentration hydrogen chloride treatment device (150).

The rotation speed of the transport means including the screw of the melting body (121) is lower than the rotation speed of the transport means including the screw inside the thermal decomposition dechlorinator (130) at the rear end, and the pitch of the transport means including the screw becomes increasingly smaller so that the material can be compressed and transported.

For example, the rotation speed of the transport means inside the melter (120) is preferably less than 10 rpm, and the rotation speed of the transport means inside the thermal decomposition dechlorinator (130) is preferably in the range of 100 to 300 rpm.

And it is preferable that the maintenance temperature in the melter (120) be in the range of 120 to 250 ℃.

In the melter (120), a cylindrical internal melting body (121) is vertically arranged so that the compressed material from the transfer heating dryer (110) can be transferred by a transfer means including a screw, and a melting jacket (123) is provided that surrounds the melting body (121) and allows high-temperature air to pass through.

Inside the melter (120), solid waste plastic and liquid material partially melted by high temperature exist together and can be transported downward by a transport means.

In this way, through the process of arranging the melter (120) between the transfer heating dryer (110) and the thermal dechlorination dechlorinator (130), the chlorine separation and removal gasification system (1000) according to the present invention can perform the dechlorination process at atmospheric pressure, unlike the conventional technology.

In addition, by vertically arranging the melter (120), the solid and liquid materials can be mixed with each other and easily and conveniently transported to the next process by rotation of the transport means along with its own weight.

The thermal dechlorination device (130) can liquefy previously dried, partially melted, and slurried material by heating and also remove and separate chlorine or hydrogen chloride bubbles contained in the liquid, thereby increasing the separation and removal efficiency of chlorine or hydrogen chloride.

The pyrolysis dechlorinator (130) has an overall long cylindrical structure, and is preferably composed of an inner dechlorination body (131) through which the material moves, and a dechlorination jacket (132) that surrounds the dechlorination body (131) and is spaced apart from the outside of the dechlorination body (131).

In addition, the pyrolysis dechlorinator (130) has a front end, which is an upstream region connected to the melter (120), and an expansion section (133) whose diameter is rapidly expanded immediately after passing the front end. As the high-temperature material transported in this expansion section (133) rapidly increases in volume, the material can expand, so that the bonding force between the material molecules is lowered, so that the molecules constituting the material can be separated more easily, and furthermore, chlorine (hydrogen chloride) decomposed in the liquid or slurry can be easily separated.

And as explained above, unlike in the melter (120), in the pyrolysis dechlorinator (130), the material transport speed is very fast, so the material can expand more rapidly in the expansion section (133).

In addition, hot air, which is high temperature air, is supplied to the dechlorination jacket (132) of the pyrolysis dechlorinator (130) to increase the temperature of the material, and the supplied hot air is supplied in the same direction as the direction in which the material is transported, so that the temperature of the material can be maintained within a set range. In addition, it is preferable that the transporting means provided inside the pyrolysis dechlorinator (130) to transport the material is provided as a paddle (134) or vane type rather than a screw type. Accordingly, in the pyrolysis dechlorinator (130) according to the present invention, the material can be turned over or stirred more effectively than in the screw type, so that the gas existing in the liquid can be separated very stably and efficiently.

Accordingly, according to the present invention, by maintaining the temperature inside the thermal decomposition dechlorinator (130) uniformly and simultaneously stirring, bubbles in the liquid can be very effectively separated and discharged from the liquid, thereby effectively removing gases such as chlorine.

On the other hand, a screw type (138) transfer means is provided in the upstream region where the transfer volume of the pyrolysis dechlorinator (130) is narrow, as shown in FIGS. 3 and 4.

And, by blowing superheated steam of about 300℃ into the pyrolysis dechlorinator (130) through the steam nozzle (135) toward the material transferred from the expansion tube (133), the decomposed chlorine (hydrogen chloride) can be easily and quickly removed (discharged).

The steam nozzle (135) is provided with a pitch set in the longitudinal direction of the expansion section (133), as illustrated in FIG. 4, and these steam nozzles (135) can supply superheated steam as a whole or in sections. For example, if the nozzle numbers from the beginning of the expansion section (133) are 1, 2, 3, 4, ..., 10, superheated steam can be supplied only from steam nozzles (135) of 1, 3, 5, 7, 9, etc., or only from even-numbered steam nozzles (135).

As shown in Fig. 4, the spraying direction of the steam nozzle (135) is opposite to the rotational direction of the rotation shaft, so that the lumped liquid material (mainly liquid and including a small amount of slurry) is further broken down and turned over by the steam sprayed by the steam nozzle (135), so that the stirring or breaking up of the material can be performed more actively. Accordingly, chlorine or hydrogen chloride existing as bubbles within the liquid can be more effectively separated and discharged, and removed from the material.

In addition, the nozzle through which the steam nozzle (135) is sprayed can be controlled by a control unit that controls and operates the system (not shown) so that it can be completely or partially sprayed as described above. In addition, the spraying time of the steam nozzle (135) can also be continuously or intermittently adjusted by the control unit. Of course, it is preferable that such control be performed based on the temperature detected by a temperature sensor (not shown).

It is preferable that the dechlorination jacket (132), which is the outer surface of the dechlorination body (131) of the pyrolysis dechlorinator (130), include a heat transfer member (136) including a plurality of heat fins so that the heat of the high-temperature gas supplied from the pyrolysis gas generator (140) can be effectively transferred to the inside of the dechlorination body (131). The plurality of heat transfer members (136) provided in the dechlorination jacket (132) can increase the heat transfer area and thus improve the heat transfer efficiency.

Meanwhile, in order to maintain the airtightness of the rotary shaft of the pyrolysis dechlorinator (130), a sealing member (137) is included. As shown in Fig. 4, the sealing member (137) is preferably provided with a housing that accommodates the gland packing so that a gas such as nitrogen can be injected to seal the rotary shaft and the dechlorinator body (131) and to seal any gas, including chlorine, that may leak to the outside.

Additionally, this confidentiality member (237) may include a spring as a means for pressurizing the grand packing as shown in FIG. 5.

These confidentiality members (137, 237) are particularly important for safety against external leakage of non-harmful gases such as chlorine or hydrogen chloride, and are preferably installed in drive parts including a rotating shaft of a transfer drying heater (110), a melter (120), a pyrolysis gas generator (140), etc., which have a drive part including a rotating shaft. In addition, if a gas leak is detected from the confidentiality members (137, 237), it is preferable to further include a purge member including a pipe or neutralization tank capable of purging the gas to the outside or a neutralization (decontamination) tank capable of capturing and neutralizing it.

In addition, unlike conventional pyrolysis decomposition devices, according to the present invention, there is a risk of explosion due to pyrolysis at high temperatures, gas generation, high-temperature steam supply, and residual external air during stop operation. In order to prevent such risks, as illustrated in Fig. 1, it is preferable to include an explosion-proof port (139) at the upper side of the melter (120) and the end of the pyrolysis dechlorinator (130) to discharge internal pressure to the outside when the pressure is higher than the set pressure to prevent explosion.

Accordingly, even if an explosion occurs due to explosive conditions inside the structure, the device can be protected and the safety of the operator can be ensured.

In conventional technology, bulk waste vinyl is fed into a pyrolysis furnace, and the dechlorination process is performed in a pyrolysis emulsification unit. In this process, the waste vinyl in bulk must be heated in the pyrolysis emulsification unit at a very high temperature, such as 450°C or higher. In this case, waste vinyl at room temperature must be rapidly raised to a high temperature of 450°C or higher to induce pyrolysis. This process of heating from room temperature to high temperature inevitably results in an uneven temperature distribution within the pyrolysis emulsification unit, as the temperature inside the unit rapidly increases from low to high.

Furthermore, most conventional pyrolysis emulsification devices utilize direct-heat burners, which heat the device using self-produced renewable oil or non-condensable gas as fuel. Direct-heat burner methods, rather than hot air circulation methods, have difficulty maintaining the temperature inside the reactor due to their heating characteristics, and the aforementioned localized heating within the reactor is very likely.

However, as in the present invention, the material that has been heated to a certain temperature and passed through the transfer heating dryer (110) and melter (120), which are pre-heating or separation processes before the pyrolysis dechlorinator (130), can be dechlorinated in the pyrolysis dechlorinator (130). Accordingly, in the present invention, the pyrolysis process is stable overall and can be performed at a lower temperature than the conventional technology, such as about 250 to 330°C (more preferably, 220 to 300°C). Due to this stable operation, the yield of pyrolysis regenerated oil can be maintained at about 75% or more, which is an increase compared to less than 50% in the conventional technology. In addition, unlike the conventional technology where a large amount of hydrogen chloride is contained in the product generated by pyrolysis, according to the present invention, only a very small amount of hydrogen chloride is present, so that the separation and removal efficiency of hydrogen chloride is improved, and the product generated by pyrolysis can be utilized as a high-quality raw material.

In addition, in the present invention, about 65% of the total energy is consumed for preheating, and the load of the thermal decomposition dechlorinator (130) can be reduced, so that the operating load of the thermal decomposition dechlorinator (130) is also reduced. In addition, compared to the prior art, the hydrochloric acid content in the thermal decomposition regenerated oil and non-condensable gas generated in the thermal decomposition dechlorinator (130) according to the present invention can be reduced, so that the effect of reducing the alkali treatment load of the product can also be obtained.

Figure 11 is a schematic comparison of the flow chart of the prior art described above and the technology according to the present invention.

The pyrolysis gas generator (140) applies heat and steam to the material that has passed through the pyrolysis dechlorinator (130) to separate the carbon and pyrolysis gas remaining in the material.

The pyrolysis gas generator (140) is composed of a cylindrical structure including a screw-type conveying means so that materials can be moved inside a combustion chamber (40) equipped with a heating burner (60) on one side that generates heat by mixing supplied fuel and air. That is, high-temperature steam is supplied inside the pyrolysis gas generator (140), and high-temperature hot air is formed in the external combustion chamber (40). In general, the temperature in the pyrolysis gas generator (140) is preferably about 450°C or higher (more preferably 450 to 550°C).

Here, it is preferable to further include a high-temperature liquid transfer pump (143) capable of transferring and spraying the molten liquid (since the plasma melting furnace melts metal or glass at high temperatures, it turns into slag and is called slag, but plastics turn into liquid when melted) formed by the high temperature in the pyrolysis gas generator (140) to the main body (203) of the steam plasma gasification melting reformer (200). That is, if the molten state that has already turned into a liquid is transferred to the steam plasma gasification melting reformer (200) by the liquid transfer pump (143) and the liquid is spray-heated and decomposed, there is an advantage in that heating energy can be saved by indirect heating in the pyrolysis gas generator (140) and the device can be made compact.

The hot air circulation fan (50) circulates the hot air generated in the combustion chamber (40) back to the combustion chamber (40) through the thermal dechlorination device (130) - melter (120) - transfer heating dryer (110). By this circulation, waste heat can be supplied to the combustion chamber (40), thereby increasing the thermal efficiency of the system.

The combustion air fan (70) has the function of supplying heated air of a certain temperature mixed with high combustion gas generated from the heating burner (60).

The high-concentration hydrogen chloride treatment device (150) has the function of capturing gas components containing chlorine or hydrogen chloride generated from the melter (120) and the thermal dechlorination dechlorinator (130), removing impurities and purifying them to produce high-concentration hydrogen chloride or neutralize them to produce chloride.

The present invention is characterized in that a steam plasma gasification melting reforming device (200) as shown in FIG. 1 and FIG. 7 to FIG. 8c is provided between a pyrolysis gas generator (140) and a pyrolysis gas purification device (160).

It is preferable that the steam plasma gasification melting reforming device (200) includes a main body (203) that receives the transferred incombustible matter and pyrolysis gas, a torch unit (210) coupled to the main body (203) so as to supply steam and plasma into the interior of the main body (203), and an inlet unit (205, 207) that guides the incombustible matter generated from the pyrolysis gas generator (140) to the main body (203).

The molten liquid from the pyrolysis gas generator (140) is transferred through a high-temperature liquid transfer pump (143) connected to the main body of the pyrolysis gas generator (140), and the remainder of the molten liquid and the non-combustible components are introduced into the main body (203) of the steam plasma gasification melting reformer (200) through an inlet (205, 207) connected to the downstream side of the pyrolysis gas generator (140) (see the solid line connecting ‘140’ and ‘203’ in FIG. 1), and the pyrolysis gas generated from the pyrolysis gas generator (140) is introduced into the main body (203) of the steam plasma gasification melting reformer (200) through a pipe line including a pipe (see the dashed line connecting ‘140’ and ‘203’ in FIG. 1), and mixed.

The molten slag and pyrolysis gas containing such non-combustible components are all introduced into the main body (203), and the non-combustible component material containing the molten slag that is not completely pyrolyzed by steam and plasma is pyrolyzed by steam and plasma, and tar, fixed carbon, etc. generated during pyrolysis or generated in the pyrolysis gas generator (140) can be reformed by steam and plasma.

Here, the injection of non-combustible material from the injection parts (205, 207) can be appropriately controlled according to the molten state or the ambient temperature inside the main body (203). For example, by detecting the height or temperature of the molten pool inside the main body (203), the operation of the first injection part (205) and the second injection part (207), which are multiple injection parts (205, 207, two in this embodiment, but can be multi-stage or single as needed), can be controlled by a control part (not shown) to adjust the injection amount to be injected into the main body (203). In addition, the pyrolysis gas generated from the pyrolysis gas generator (140) can also be introduced into the main body (203), for example, through a steam supply port (215) to which steam is supplied or through a supply line (not shown).

The present invention is characterized in that impurities such as carbon in the dust, finely floating tar components, and ash that are thermally decomposed are reformed into H ₂ and CO or CO ₂ in the steam plasma gasification melting reforming device (200). In the steam plasma gasification melting reforming device (200), moisture is dissociated using high-temperature steam and arc energy of plasma.

Carbon C(s) in the ash must come into contact with _O2 to be converted from solid to gas (CO), so injection of a gasification medium such as oxygen ( _O2 ) or air ( _N2 + _O2 ) is inevitable.

If air is injected, the amount of gas produced increases due to the nitrogen ( _N2 ) in the air, which contains a large amount of nitrogen, but the heat capacity of the gas is relatively low, which has the problem of lowering the gas quality. In addition, if pure oxygen ( _O2 ) is injected, the amount of gas produced due to nitrogen does not increase, but the hydrogen content in the generated gas is low, which has the disadvantage of low hydrogen production efficiency.

Accordingly, it can be seen that when dissociated water (2H ₂ + O ₂ ) is injected, the amount of gas generated is reduced and the hydrogen content is relatively increased, making it the best method for producing hydrogen.

However, if the moisture injection method is used to make dry coke into a slurry state by mixing more than 30 wt% as in the existing method, the heat content of the gas is relatively lowered due to the consumption of latent heat of vaporization of moisture, so the method of injecting the injected coke in a dry state (containing less than 5% moisture) is a desirable method for increasing hydrogen production.

By utilizing a steam plasma gasification melting reformer (200) that injects moisture in a dissociated state through high-temperature steam and plasma, the device can be compacted and the hydrogen content can be maximized.

To maximize hydrogen production, superheated steam is used as a plasma medium gas. However, if the steam temperature is too low, problems such as leakage of the plasma torch may occur due to condensation by the cooling water, so it is desirable to supply high-temperature superheated steam.

On the other hand, if the superheated steam is too high, other problems such as overheating and cooling of the torch may occur, so superheated steam of about 200 to 500°C can be used, but preferably it is in the range of 200 to 300°C, and more preferably it is in the range of 230 to 270°C.

And the temperature generated by the plasma torch is preferably in the range of 2000 to 5000℃, so the superheated steam supplied to the plasma is heated to an ultra-high temperature of about 2500℃ or higher by the arc energy, dissociated, separated into synthesis gas ( _H2 + _O2 ), and the separated gas is mixed with carbon (C) of waste fuel to change into water gas (main component _H2 + CO).

Figure 9 is a diagram illustrating the process described above.

At this time, it was confirmed through pilot experiments that the hydrogen component increased from a maximum of 14.85 V% (when using air) to 32.19 V% (when using pure oxygen) in the conventional technology to up to 56.84 V% (when using pure oxygen) in accordance with the present invention .

Here, the supply temperature of steam in the steam plasma gasification melting reforming device (200) is preferably in the range of 300 to 500°C, and the temperature formed by plasma is preferably in the range of 3,000 to 5,000°C. At this time, the ambient temperature inside the main body (203) is preferably about 1,300°C.

At this temperature or atmosphere, what is generated after thermal decomposition from the non-combustible material to be thermally decomposed in the steam plasma gasification melting reformer (200) is synthesis gas (containing hydrogen 80 V% or more) and tar component (1 mg/Nm ³ Below), carbon (0.01 wt%), etc. in the slag are included, and the residue is discharged as molten slag through the molten slag discharge unit (220).

In the steam plasma gasification melting reforming device (200), the target of reforming includes tar components and carbon in ash, and as a result of reforming, carbon and tar are gasified or decomposed.

And, as shown in FIG. 7 and FIG. 8a to FIG. 8c, it is preferable that the torch unit (210) include a steam supply port (215) through which steam is supplied and a plasma torch (213) through which plasma is generated.

There are several methods for supplying steam from the torch unit (210) to the main body (203), as shown in FIGS. 8a to 8c.

First, as shown in Fig. 8a, the plasma torch (213) is an example of a plurality of three (a plurality including one or two direct current or alternating current electrodes can be used). It is preferable that an electrode of the opposite polarity is installed at the lower part of the main body (203) to which the plasma torch (213) is coupled, that is, if the upper part is the ‘+’ pole in the case of alternating current, the lower part is the ‘-’ pole, and if the upper part is the ‘+’ pole in the case of three-phase power, the lower part is the ‘ground connection’ or the ‘common base’. One method is to couple the plasma torch (213) to the main body (203) at an equal distance from the center or central axis of the main body (203) and to couple the steam supply port (215) to the main body (203) so as to face the center of the main body (203).

And, the plasma torch (313) is given as an example of three in number, and as shown in FIG. 8b, a steam supply port (315) is formed as a double pipe on the outside of each plasma torch (313), and as shown in FIG. 8c, a steam supply port (415) is formed penetratingly in the center of each plasma torch (413), which are different methods. In the drawing numbers that are not described, if the tens and ones are the same, it is understood that it is the same as the configuration described above.

The pyrolysis gas reforming device (160) connected to the rear end of the steam plasma gasification melting reforming device (200) has the function of capturing, purifying, and reforming the gas components generated in the steam plasma gasification melting reforming device (200) to produce high-purity hydrogen. The hydrogen thus produced can be separated and extracted by a hydrogen extractor and used in the process or can be utilized as fuel for operating fuel cells, etc. That is, the produced gas does not contain chlorine or hydrogen chloride, so that the gas according to the present invention does not contain insoluble substances or impurities compared to the gas of the prior art, thereby improving usability and economic feasibility.

In the present invention, the high-concentration hydrogen chloride treatment device (150) and the thermal decomposition gas reforming device (160) are not the core contents of the invention, and the processes and treatment steps preceding them are important components, so a detailed description thereof is omitted below.

The unexplained reference number ‘138’ indicates a screw-type conveying means for conveying materials to the front end of the pyrolysis dechlorinator (130).

And although not shown, a hole may be formed along the length of the rotating shaft of the pyrolysis dechlorinator (130) to transfer heat to the material through hot air, steam, a heating wire, heat transfer oil, etc. through the formed hole. This heat transfer can maintain the temperature of the material more uniformly, thereby improving the efficiency of pyrolysis or dechlorination.

In addition, the heat transfer hole of the rotation shaft can also be provided in a transfer heating dryer (110), a melter (120), or a pyrolysis gas generator (140).

The operation process of the chlorine separation and removal gasification system having this configuration is specifically examined with reference to FIGS. 1 to 4 as follows.

First, when combustible waste plastic waste including waste PVC is fed into the feeding device (10), the material received in the hopper body (11) is pressurized by the extrusion means (13) at the bottom and fed to the transfer heating dryer (110).

The material of the drying heating body (111) is transferred to the melter (120) while maintaining a dried state by evaporating moisture, volatile impurities, etc. by the heat transferred by the hot air of the drying heating jacket (113) of the transfer heating dryer (110).

In the melter (120), the material is melted by the heat supplied by the hot air, and maintains a solid state and a liquid state (slurry state) and is transferred to the thermal decomposition dechlorinator (130) by a transfer means such as a screw.

The rotation speed of the transport means for transporting the material in the transport heating dryer (110) and melter (120) is very slow compared to the rotation speed of the transport means for transporting the material in the thermal decomposition dechlorinator (130).

The material transferred from the melter (120) is thermally decomposed by the material coming into contact with the steam supplied into the dechlorination body (131) in the pyrolysis dechlorinator (130) and by the material being heated by the hot air flowing along the dechlorination jacket (132). In particular, in the pyrolysis dechlorinator (130), unlike the prior art, chlorine and hydrogen chloride can be very effectively separated from the material at a set temperature and within an evenly distributed temperature range.

The gas separated from the melter (120) and the thermal dechlorinator (130) can be moved to the high-concentration hydrogen chloride treatment unit (150) to produce high-concentration recycled oil.

And, as shown in Fig. 2, the transfer heating dryer (110) is arranged horizontally and the melter (120) is arranged vertically, and the melter (120) in the vertical state and the thermal decomposition dechlorinator (130) in the horizontal state are arranged orthogonally to each other.

The material that has passed through the pyrolysis dechlorinator (130) can be moved to the pyrolysis gas purification device (160) by separating gas containing hydrogen in the pyrolysis gas generator (140) that can maintain a higher temperature by the hot air of the combustion chamber (40) and the steam supplied inside, thereby producing high-purity hydrogen.

And the residue that has not been thermally decomposed is fed into the main body (203) of the steam plasma gasification melting reforming device (200) combined with the torch unit (210) described above by an injector (205, 207) through a conveyor (not shown) as needed.

Additionally, the pyrolysis gas generated from the pyrolysis gas generator (140) is also introduced into the main body (203).

The introduced non-combustible material is melted again in a high-temperature atmosphere and gasified, and impurities such as tar and fixed carbon in the pyrolysis gas generated during the pyrolysis process inside the main body (203) and impurities including tar and fixed carbon in the pyrolysis gas introduced from the pyrolysis gas generator (140) can be reformed by steam and plasma supplied from the torch unit (210).

Here, in order to maintain the ambient temperature of the steam plasma gasification melting reformer (200) within a certain range, the power supply must be controlled and supplied by considering the amount of pyrolysis residue, which is the incombustible component, and the supply amount of pyrolysis generated gas. In addition, since the arc rod of the plasma torch (213) is consumable, it must be supplied in the amount consumed. In order to control this, since the amount of slag produced varies depending on the amount of the input residue, and the height of the molten metal varies depending on the amount of slag melted, it is preferable to detect this as a current or voltage fluctuation and control the power supply. Whether the current fluctuation or the voltage fluctuation is the target of detection is determined by the type of AC power supply that supplies three-phase power to the arc rods of the three plasma torches (213).

Meanwhile, the high temperature hot air generated in the combustion chamber (40) by being heated by the heating burner (60) can be discharged to the outside as needed through the pyrolysis gas generator (140) - pyrolysis dechlorinator (130) - melter (120) - transfer heating dryer (110), but most of it is circulated back to the combustion chamber (40) by the hot air circulation fan (50) so that the waste heat is recycled, thereby improving the thermal efficiency of the system.

And, as shown in the flow chart in Fig. 10, the synthesis gas having almost no tar and high hydrogen content that has passed through the steam plasma gasification melting reformer (200) is changed into a very high purity synthesis gas through mixing, cooling, dust collection, etc., and a WGS reactor (Water Gas Shift Reaction), etc., and hydrogen is separated from the synthesis gas, and the surplus gas can be used for power generation such as a lean burn engine.

Accordingly, according to the present invention, a high-purity synthesis gas can be produced by removing chlorine components contained in combustible waste that can be used as waste fuel (combustible waste such as household, industrial, waste plastic, designated waste, or mixed waste plastic) made of combustible waste plastic including PVC through improved pyrolysis conditions by maintaining atmospheric pressure and constant temperature conditions, and by decomposing impurities such as fixed carbon and tar formed in the pyrolysis process through steam plasma gasification melting, and using the purified high-purity synthesis gas as a raw material for hydrogen production, etc., and by compacting the device and increasing the amount of hydrogen produced, thereby producing a high-value-added synthesis gas raw material, a system for producing high-purity (hydrogen maximization) raw material by reforming pyrolysis gas of PVC-rich waste plastic can be provided.

In addition, a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reforming device capable of producing purified synthetic gas clean raw materials with high efficiency by producing hydrogen after waste fuel is pyrolyzed and gasified and then undergoing a process such as purification, which can be used in a gas engine or turbine, or can be used in a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming having a steam plasma gasification melting reforming device capable of producing purified synthetic gas clean raw materials with stable quality with high efficiency by producing hydrogen.

In addition, a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming can be provided, which has a steam plasma gasification melting reforming device that can incorporate the advantages of a hot air circulation indirect heating pyrolysis furnace.

Although one embodiment of the present invention has been illustrated and described herein, those skilled in the art will appreciate that modifications to the present embodiment can be made without departing from the principles or spirit of the invention. The scope of the invention is defined by the appended claims and their equivalents.

1000: Chlorine Separation Removal Gasification System
10: Feeder 11: Hopper body
13: Extrusion means 40: Combustion chamber
50: Hot air circulation fan 60: Heating burner
70: Combustion air fan 80: Explosion-proof hole
110: Transfer heating dryer 111: Drying heating main body
113: Dry heating jacket 120: Melter
121: melting body 123: melting vessel jacket
130: Thermal dechlorination device 131: Dechlorination body
132: Dechlorination jacket 133: Expansion pipe
134: Paddle 135: Steam nozzle
136: Heat transfer member 137: Sealing member
138: Dechlorination screw 139: Bypass automatic damper
140: Pyrolysis gas generator 143: Liquid transfer pump
150: High-concentration hydrogen chloride treatment unit 160: Pyrolysis gas purification unit
200, 300, 400: Steam plasma gasification melting reforming device
203: Main body 205, 207: First and second input sections
210: Torch section 213: Plasma torch
215: Steam supply port 220: Molten slag discharge port

Claims (7)

In a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming with a steam plasma gasification melting reforming device,
An input device that receives and compresses waste plastic waste including waste PVC;
A transfer heating dryer capable of indirectly heating the material received from the above input device with hot air;
A melter configured to receive the material transferred from the above-mentioned transfer heating dryer, transport it vertically, and melt it by indirect heating of hot air to maintain a slurry state;
A thermal dechlorination dechlorinator that is heated by hot air that indirectly heats the material transferred from the above melter and steam that directly heats it, and the flow of the hot air and the direction of transfer of the material are the same, thereby increasing the residence time within the set temperature range of the dechlorination area and enabling efficient separation and discharge of chlorine and hydrogen chloride;
A pyrolysis gas generator that heats the material transferred from the pyrolysis dechlorinator to a temperature higher than the temperature of the pyrolysis dechlorinator and pyrolyzes it to separate a gas containing hydrogen;
A steam plasma gasification melting reforming device provided downstream of the pyrolysis gas generator, which gasifies and melts slags residual carbon and incombustible matter transferred from the pyrolysis gas generator and removes polymer impurities including carbon or tar contained in the gas generated from the pyrolysis gas generator;
The above steam plasma gasification melting reforming device includes a main body for receiving transported incombustible matter and gas, a torch unit coupled to the main body for supplying steam and plasma into the interior of the main body, and an input unit for guiding incombustible matter generated from the pyrolysis gas generator into the main body.
The above torch part includes a steam supply port for supplying steam and a plasma supply torch for supplying plasma,
A raw material production system characterized in that the plasma supply torch is provided in plurality and is spaced apart from the center of the main body at an equal distance and coupled to the main body, and the steam supply port is coupled to the main body so as to face the center of the main body. In the first paragraph,
A raw material production system characterized in that in the above steam plasma gasification melting reforming device, steam and plasma are applied to gasify carbon, and carbon is changed into water gas (main component H ₂ + CO) by dissociated water (2H ₂ + O ₂ ) at high temperature. In the second paragraph,
A raw material production system characterized in that the steam has a temperature range of 200 to 500°C, and the temperature by the arc energy supplied from the plasma has a temperature range of 3000 to 5000°C. delete delete In a high-purity (hydrogen maximization) raw material production system for PVC-rich waste plastic pyrolysis gas reforming with a steam plasma gasification melting reforming device,
An input device that receives and compresses waste plastic waste including waste PVC;
A transfer heating dryer capable of indirectly heating the material received from the above input device with hot air;
A melter configured to receive the material transferred from the above-mentioned transfer heating dryer, transport it vertically, and melt it by indirect heating of hot air to maintain a slurry state;
A thermal dechlorination dechlorinator that is heated by hot air that indirectly heats the material transferred from the above melter and steam that directly heats it, and the flow of the hot air and the direction of transfer of the material are the same, thereby increasing the residence time within the set temperature range of the dechlorination area and enabling efficient separation and discharge of chlorine and hydrogen chloride;
A pyrolysis gas generator that heats the material transferred from the pyrolysis dechlorinator to a temperature higher than the temperature of the pyrolysis dechlorinator and pyrolyzes it to separate a gas containing hydrogen;
A steam plasma gasification melting reforming device provided downstream of the pyrolysis gas generator, which gasifies and melts slags residual carbon and incombustible matter transferred from the pyrolysis gas generator and removes polymer impurities including carbon or tar contained in the gas generated from the pyrolysis gas generator;
The above steam plasma gasification melting reforming device includes a main body for receiving transported incombustible matter and gas, a torch unit coupled to the main body for supplying steam and plasma into the interior of the main body, and an input unit for guiding incombustible matter generated from the pyrolysis gas generator into the main body.
The above torch part includes a steam supply port for supplying steam and a plasma supply torch for supplying plasma,
The above plasma supply torch is provided in multiples,
A raw material production system characterized in that the steam supply port is formed by a double pipe on the outside of each plasma supply torch or by including the steam supply port penetrating the center of each plasma supply torch. In claim 1 or claim 6,
A raw material production system characterized by further comprising a high-temperature liquid transport pump that transports liquid fuel generated in the pyrolysis gas generator to the main body.