KR102636642B1 - Apparatus for forming cement by using shells and plastic waste and cement forming method using the same - Google Patents

Abstract

The present invention includes a raw material tank in which waste plastic raw materials are stored; A bubble fluidized bed gasification furnace in which raw materials are supplied from the raw material tank through the raw material input unit, steam flows in from the bottom and the fluidized medium flows inside, thereby forming a bubble fluidized layer, and the raw materials are gasified to produce produced gas inside; Char contained in the fluidized medium and the produced gas is transferred from the bubble fluidized bed gasifier, air is additionally supplied, the fluidized medium is heated by burning the char, and the heated fluidized medium is heated. A high-speed fluidized bed combustion furnace transferred to the bubble fluidized bed gasifier; a produced gas cyclone that is in communication with the bubble fluidized bed gasifier and separates fine particles from the produced gas discharged from the bubble fluidized bed gasifier, re-introduces the fine particles into the bubble fluidized bed gasifier, and discharges the remainder; It is connected between the upper part of the high-speed fluidized bed combustion furnace and the upper part of the bubble fluidized bed gasifier, and after separating the fluidized medium from the exhaust gas, the exhaust gas is discharged and the fluidized medium is separately supplied to the bubble fluidized bed gasifier and the raw material input section. gas cyclone; and a shell processing unit that generates cement by heating the shell using the generated gas and exhaust gas. It relates to a cement manufacturing device using shells and waste plastic and a cement manufacturing method using the same.

Description

Cement manufacturing device using shells and waste plastic and cement production method using the same {Apparatus for forming cement by using shells and plastic waste and cement forming method using the same}

The present invention relates to a cement production device using shells and waste plastics and a cement production method using the same. More specifically, the present invention relates to a cement production device that heat-treats shells to produce cement, and the gas generated by heat-treating waste plastics is used as a heat source. It relates to a cement manufacturing device used and a cement production method using the same.

As the quality of life improves worldwide after industrialization, the amount of waste generated is increasing. Previously, these wastes were disposed of by incineration or landfill, but air pollution due to harmful components generated during incineration is serious, soil and groundwater contamination through landfilling is increasing, and recently, due to a shortage of landfills, wastes can be considered as eco-friendly. There is a need to develop technology to process it in an efficient and safe way.

Shell refers to the shells of freshwater and marine species such as abalone, clams, oysters, corals, mussels, and whelks. The main ingredient is calcium carbonate (CaCO ₃ ). Due to the current system and cost issues, these shells are currently classified as industrial waste and disposed of. In particular, in the case of oyster shells, about 180,000 tons are generated annually, and various attempts have been made to utilize them as resources.

For example, oyster shells are crushed and used as raw materials for fertilizers, feed, and cosmetics, but the amount of oyster shells recycled in this way is extremely small. Considering the environmental problems caused by shells and the reality of recycling, the shells, which are marine and fishery waste, are used as raw materials for fertilizers, feed, and cosmetics. Research is required to develop realistic new treatment methods and use it as a recycled resource.

Meanwhile, plastic is light, hard, and easy to manufacture into various shapes, so it is a material widely used in various industries today. However, as the use of plastic products increases, the amount of plastic waste generated is rapidly increasing every year. Recently, more than 10 million tons are generated in Korea alone, and research on methods of processing plastic waste is being conducted from various angles.

Plastic waste can be disposed of through methods such as landfill, incineration, and recycling. Incineration of plastic waste has the advantage of recycling the heat energy generated by incineration, but it emits toxic gases that are fatal to the human body and the environment. And there is a non-economic problem.

Registered Patent No. 10-1993734 (registered on June 21, 2019)

The present invention seeks to provide a cement manufacturing device that produces cement by heat treating shells using gas generated by heat treating waste plastic as a heat source and a cement production method using the same.

A cement manufacturing apparatus using shells and waste plastic according to an embodiment of the present invention for achieving the above-described object includes a raw material tank in which waste plastic raw materials are stored; A bubble fluidized bed gasification furnace in which raw materials are supplied from the raw material tank through the raw material input unit, steam flows in from the bottom and the fluidized medium flows inside, thereby forming a bubble fluidized layer, and the raw materials are gasified to produce produced gas inside; Char contained in the fluidized medium and the produced gas is transferred from the bubble fluidized bed gasifier, air is additionally supplied, the fluidized medium is heated by burning the char, and the heated fluidized medium is heated. A high-speed fluidized bed combustion furnace transferred to the bubble fluidized bed gasifier; a produced gas cyclone that is in communication with the bubble fluidized bed gasifier and separates fine particles from the produced gas discharged from the bubble fluidized bed gasifier, re-introduces the fine particles into the bubble fluidized bed gasifier, and discharges the remainder; It is connected between the upper part of the high-speed fluidized bed combustion furnace and the upper part of the bubble fluidized bed gasifier, and after separating the fluidized medium from the exhaust gas, the exhaust gas is discharged and the fluidized medium is separately supplied to the bubble fluidized bed gasifier and the raw material input section. gas cyclone; and a shell processing unit that generates cement by heating the shell using the generated gas and exhaust gas.

Inside the bubble fluidized bed gasifier, a center rod positioned vertically along the center of the bubble fluidized bed gasifier; and a spiral wing that moves the generated gas and steam in a swirling flow along the central rod.

The shell processing unit includes a shell preheating unit 510 that preheats the shell; A preliminary decomposition furnace 520 for heating and partially calcining the shell supplied from the shell preheating unit 510; a main cracking furnace (530) for producing cement by heating the mixture supplied from the preliminary cracking furnace (520); and a cooling unit 540 that cools the cement supplied from the main decomposition furnace 530.

Exhaust gas discharged from the exhaust gas cyclone may be used as a heat source for the preliminary cracking furnace 520, and produced gas discharged from the produced gas cyclone may be used as a heat source for the main cracking furnace 530.

The raw material input unit includes a raw material input pipe through which raw materials are introduced from the raw material tank into the bubble fluidized bed gasifier; A transfer screw that rotates inside the raw material input pipe and transfers the raw material; and a discharge pipe for discharging gas containing chlorine compounds generated inside the raw material input pipe.

Another embodiment of the present invention includes a cement manufacturing method using shells and waste plastics, where waste plastic raw materials are supplied and burned in a double fluidized bed reactor including a bubble fluidized bed gasifier and a high-speed fluidized bed combustion furnace. A waste plastic combustion step of generating product gas and generating exhaust gas in a high-speed fluidized bed combustion furnace; and a cement production step of manufacturing cement through a preheating step of heating the shell, which is a raw material, a preliminary decomposition step, and a main decomposition step, and a cooling step of cooling the cooled object to be heated.

In addition, it is preferable that exhaust gas is used as a heat source in the preliminary decomposition step and produced gas is used as a heat source in the main decomposition step.

The waste plastic combustion step includes supplying waste plastic raw materials, steam, and heated fluid medium to a bubble fluidized bed gasifier to decompose the waste plastic raw materials; Reheating the fluidized medium by supplying and burning the fluidized medium discharged from the bubble fluidized bed gasifier and char generated by decomposition of waste plastic raw materials to a high-speed fluidized bed combustion furnace; Filtering fine particles contained in the product gas generated in the bubble fluidized bed gasification furnace through a product gas cyclone and discharging the gaseous components; and separating the components discharged from the high-speed fluidized bed combustion furnace through an exhaust gas cyclone, transferring the fluidized medium to the bubble fluidized bed gasification furnace, and discharging the remaining exhaust gas.

The cement manufacturing step includes supplying and preheating shell, which is a raw material, to a shell preheating unit including a plurality of cyclones arranged up and down; Supplying preheated shells and exhaust gas to a preliminary decomposition furnace to first heat the preheated shells; Supplying primary heated shells and produced gas to the main decomposition furnace, burning the produced gas, and secondary heating the primarily heated shells to produce cement; and cooling the cement.

The cement manufacturing device of the present invention manufactures cement from shells and uses gas generated in the process of gasifying waste plastics as a heat source, so that shells and waste plastics, which are classified as waste, can be recycled, thereby reducing the costs incurred in waste disposal. Save money and prevent environmental pollution.

In addition, since gas generated by gasifying and recycling waste plastic is used as a heat source for heat treating shells, the cost of using general fuels such as natural gas, oil, and coal can be reduced.

In addition, HCl generated when gasifying waste plastics containing PVC can be effectively reduced, and waste plastic raw materials can be more effectively supplied to the reactor regardless of the phase of the waste plastic raw materials.

Figure 1 is a diagram showing a cement manufacturing apparatus using shells and waste plastic according to an embodiment of the present invention.
Figures 2 and 3 are diagrams showing an embodiment of a bubble fluidized bed gasification furnace.
Figure 4 is a diagram showing another embodiment of a bubble fluidized bed gasification furnace.
Figure 5 is a diagram showing a modified example of the cross-sectional shape of the unit wing constituting the spiral wing according to Figure 4.
FIG. 6 is a view viewed from direction a of FIG. 4.
FIG. 7 is a diagram illustrating an example in which the cross section of the unit blade constituting the spiral blade of FIG. 4 has a pseudo-trapezoidal shape.
FIG. 8 is a diagram illustrating an example of the cross-sectional shape of a unit wing constituting the spiral wing of FIG. 4.
Figure 9 is a diagram showing the fluid flow inside the bubble fluidized bed gasification furnace of Figure 4.
FIG. 10 is a diagram illustrating an embodiment of a unit blade constituting the spiral blade of FIG. 4.
Figure 11 is a diagram schematically showing a double fluidized bed reactor according to another embodiment of the present invention.
Figure 12 is a diagram schematically showing a double fluidized bed reactor according to another embodiment of the present invention.
Figure 13 schematically shows the shape of the hole in the perforated plate when the spiral blade is formed in the shape of a perforated plate.

Before explaining in detail the preferred embodiments of the present invention below, the terms and words used in the specification and claims should not be construed as limited to their ordinary or dictionary meanings, but should be interpreted as meanings consistent with the technical idea of the present invention. Please note that it should be interpreted as a concept.

Throughout this specification, when a part “includes” a certain element, this means that it may further include other elements rather than excluding other elements, unless specifically stated to the contrary.

The present invention will be described in detail with reference to embodiments of the present invention and drawings. These examples are merely presented as examples to explain the present invention in more detail, and it will be apparent to those skilled in the art that the scope of the present invention is not limited by these examples. .

Each step may be performed in a different order than the specified order unless the context clearly indicates a specific order. That is, each step may be performed in the same order as specified, may be performed substantially simultaneously, or may be performed in the opposite order.

Below, we will look at embodiments of the present invention. However, the scope of the present invention is not limited to the preferred embodiments below, and those skilled in the art can implement various modifications of the contents described in this specification within the scope of the present invention.

The present invention relates to a cement production device using shells and waste plastics and a cement production method using the same.

Figure 1 relates to a cement manufacturing device (hereinafter referred to as 'cement manufacturing device') using shells and waste plastic according to an embodiment of the present invention.

The cement manufacturing apparatus according to an embodiment of the present invention includes a shell processing unit 500 that receives shells as a raw material and heat-treats them to produce cement, and a double fluidized bed reactor that supplies heat to the shell processing unit 500. The raw material of the shell processing unit 500 is shell, and the raw material of the double fluidized bed reactor is waste plastic.

First, the double fluidized bed reactor includes a bubble fluidized bed gasifier 100, a high-speed fluidized bed combustion furnace 200, and a raw material tank 300, and raw materials are transferred from the raw material tank 300 to the bubble fluidized bed gasifier 100. When this happens, the raw material is thermally decomposed in the bubble fluidized bed gasifier 100 to generate product gas 10, and the high-speed fluidized bed combustion furnace 200 produces the fluidized medium and the product gas 10 from the bubble fluidized bed gasifier 100. Char is supplied and the fluidized medium is heated by burning the char, and then transferred back to the bubble fluidized bed gasifier (100) to transfer heat to the bubble fluidized bed gasifier (100).

The raw material tank 300 is a unit in which waste plastic containing PVC, a raw material, is stored. The raw materials stored in the raw material tank 300 can be supplied to the bubble fluidized bed gasification furnace 100 through the raw material input unit 160. .

The raw material input unit 160 is a raw material input pipe 161 through which raw materials are introduced from the raw material tank 300 to the bubble fluidized bed gasifier 100, and a transfer screw that rotates inside the raw material input pipe 161 and transfers the raw materials. (162) and a discharge pipe (163) for discharging chlorine compounds such as HCl generated inside the raw material input pipe (161).

The bubble fluidized bed gasification furnace 100 is a unit that generates product gas 10 by receiving raw materials from the raw material tank 300 and thermally decomposing them, wherein not only useful substances such as H ₂ , CO, and CH ₄ but also tar (tar) ) and char are created together. The tar generated here is removed through thermal decomposition inside the bubble fluidized bed gasifier 100, and the char is transferred to the high-speed fluidized bed combustion furnace 200 and used as combustion fuel for heating the fluidized medium.

The produced gas 10 discharged from the bubble fluidized bed gasification furnace 100 not only contains useful gas components such as H ₂ , CO, and CH ₄ , but also contains fine particles such as tar and fluidized medium pulverized particles. These fine particles are separated through the produced gas cyclone 140 in communication with the bubble fluidized bed gasifier 100 and flow back into the bubble fluidized bed gasifier 100, and the remaining produced gas 10 with the fine particles removed Can be supplied to the main decomposition furnace 530 of the shell processing unit 500.

The produced gas 10 discharged from the produced gas cyclone 140 may vary depending on the type of fluid medium. It contains approximately 40 to 70 vol% hydrogen and can be used as a hydrogen raw material. The fluid medium is olivine. or calcium oxide (CaO) may be used.

The high-speed fluidized bed combustion furnace 200 is a unit that receives the fluidizing medium and char from the bubble fluidized bed gasification furnace 100 and heats the fluidizing medium by burning the char. The fluidized medium heated in the high-speed fluidized bed combustion furnace 200 and the exhaust gas 20 generated during the combustion process are separated through the exhaust gas cyclone 210.

The fluidized medium heated in the high-speed fluidized bed combustion furnace 200 is separated through the exhaust gas cyclone 210, and the fluidized medium separated from the exhaust gas cyclone 210 is discharged through the exhaust gas cyclone connection pipe 220.

The exhaust gas cyclone connection pipe 220 is connected to the first fluid medium supply pipe 230 and the second fluid medium supply pipe 240.

The exhaust gas cyclone connector 220 may be provided with a valve 221, and the heated flow is separately supplied to the first fluid medium supply pipe 230 and the second fluid medium supply pipe 240 by the valve 221. The amount of medium can be adjusted.

The first fluidized medium supply pipe 230 is provided to supply the heated fluidized medium back to the bubble fluidized bed gasifier 100, and the fluidized medium supplied to the bubble fluidized bed gasifier 100 is ( 100) can function as a heat source.

The second fluid medium supply pipe 240 is connected to the raw material input pipe 161, and can supply heated fluid medium to the raw material input pipe 161. The heated fluid medium supplied to the raw material input pipe 161 heats the raw material supplied from the raw material tank 300 and is mixed with the heated and liquefied raw material to form a sludge-like mixture, thereby facilitating the transfer of the raw material. You can do it.

Specifically, the front end of the raw material input unit 160 is connected to the raw material tank 300, and the rear end is connected to the bubble fluidized bed gasification furnace 100 maintained at a temperature of about 450 ° C. or higher, so that the raw material tank 300 The solid waste plastic raw material containing PVC supplied through maintains a solid form at the front end of the raw material input unit 160, but becomes liquefied at the rear end of the raw material input unit 160 due to the influence of the bubble fluidized bed gasification furnace 100. Supply through the transfer screw 162 is not smooth or difficult.

In addition, chlorine compounds such as HCl are generated at this time, which can cause corrosion of parts within the device or cause safety issues in the workplace.

Accordingly, in the present invention, a part of the fluidized medium heated in the high-speed fluidized bed combustion furnace 200 is supplied to the raw material input pipe 161, the solid waste plastic raw material is mixed with the fluidized medium to liquefy, and the fluidized medium and the raw material are mixed together. By transferring, the fluid medium performs a carrier function of moving the liquefied raw material, thereby solving the problem of poor transport of the liquefied raw material.

At this time, the fluid medium may be supplied in a range of about 5 to 10 times the volumetric flow rate of the raw material supplied from the raw material tank 300. If the volumetric flow rate of the fluid medium is less than 5 times the volumetric flow rate of the raw material, there is a problem in which the liquefied raw material is not transported smoothly, and if it exceeds 10 times, the temperature of the raw material input section 160 is unnecessarily increased and bubbles are formed. Since the content of the fluidized medium resupplied as the heat source of the fluidized bed gasification furnace 100 is excessively reduced, the efficiency of heat supply through the fluidized medium is significantly reduced, so the heated fluidic medium is supplied to the raw material input pipe 161 at the above-mentioned volume ratio. It is desirable.

In addition, by supplying a part of the fluid medium heated in the high-speed fluidized bed combustion furnace 200 to the raw material input pipe 161, the temperature of the raw material input pipe 161 is maintained at about 300 ° C. or higher from the front end to the rear end. The raw material is liquefied and gaseous chlorine compounds such as HCl are generated. Since the chlorine compounds generated here are discharged through the discharge pipe 163, corrosion problems in the reactor caused by chlorine compounds and reduced workplace safety can be prevented.

In this way, the raw materials supplied through the raw material input unit 160 are gasified by a gasification system consisting of a series of sequential devices including a bubble fluidized bed gasifier 100 and a high-speed fluidized bed combustion furnace 200.

The bubble fluidized bed gasifier 100 is a part that pyrolyzes and gasifies raw materials. Steam 30, an oxidizing agent, is injected into the lower part of the bubble fluidized bed gasifier 100 to form a bubble fluidized bed 120, and the raw materials are pyrolyzed and gasified. It changes into produced gas (10).

Inside the bubble fluidized bed gasifier (100), a center rod (130) is fixedly installed on the upper side of the bubble fluidized bed (120) along the center of the bubble fluidized bed gasifier (100) in a vertical direction, and a screw is installed around the center rod (130). It is preferable that the wing-shaped spiral blades 110 are combined so that the fluid moves in a swirling flow inside the bubble fluidized bed gasifier 100.

At this time, preferably, the spiral wing 110 may be formed in the shape of a perforated plate with a plurality of holes. In this case, the fluid medium falls to the bottom of the hole formed in the spiral blade 110 and may come into contact with steam and generated gas rising in a swirling flow along the spiral blade 110. Therefore, the contact efficiency between the fluid medium and the steam and generated gas is maximized, so the reforming efficiency of tar can be significantly improved.

In this way, when the spiral wing 110 is formed in the shape of a perforated plate, the shape of the hole may have a shape such as a circle, oval, or polygon, or a letter, pattern, or pattern, and the shape of the hole is not limited to this. No (see Figure 13).

The maximum diameter or maximum side length of these holes may be 5 to 20 mm.

When observed from one side, the spiral wings 110 may be formed to have 2 to 6 rows, and when the number of rows is less than one row, reactants such as raw materials and fluid media move from the top to the bottom and move from the bottom to the top. The frequency of contact and reaction efficiency of the gas decreases, which reduces the production efficiency of the produced gas 10 and the removal efficiency of tar. If it exceeds 6 rows, the space between each row becomes narrow, so that the As the pressure loss of gas rising while rotating increases, problems with the smooth flow of gas may occur.

Meanwhile, char and fluidized medium are transferred from the lower part of the bubble fluidized bed gasifier 100 to the high-speed fluidized bed combustion furnace 200. Air flows in from the bottom of the high-speed fluidized bed combustion furnace 200 to burn char, and the high-speed fluidized bed combustion furnace 200 is operated with a very high speed fluidized bed (fast bed). The fluidized medium transferred to the high-speed fluidized bed combustion furnace (200) was at 450 to 780°C at the bottom of the bubble fluidized bed gasification furnace (100), but is heated to 920 to 950°C as it passes through the high-speed fluidized bed combustion furnace (200) and acts as a high-temperature heat source. It is reintroduced into the bubble fluidized bed gasifier (100).

At this time, additional external fuel may be supplied to the high-speed fluidized bed combustion furnace 200 as needed, and the produced gas 10 discharged through the produced gas cyclone 140 may be used as the external fuel.

The gas that has passed through the high-speed fluidized bed combustion furnace 200 is separated from the fluidized medium and the ash by the exhaust gas cyclone 210 connected to the upper part of the high-speed fluidized bed combustion furnace 200, and the exhaust gas 20 generated by the combustion process is the exhaust gas. It is discharged through the cyclone (210).

The temperature of the exhaust gas 20 is 920 to 950°C, and it is supplied to the preliminary decomposition furnace 520 through an exhaust gas supply line 521, which will be described later, and can be used as a heat source for the preliminary decomposition furnace 520.

At the same time, the fluidized medium that has changed to a high temperature in the high-speed fluidized bed combustion furnace 200 passes through the exhaust gas cyclone 210, and a portion is transferred to the upper part of the bubble fluidized bed gasifier 100 for the gasification reaction of the bubble fluidized bed gasifier 100. It is used as a heat source, and the remaining part is supplied to the raw material input pipe 161 and functions as a carrier to facilitate the transfer of raw materials from the raw material input pipe 161.

As described above, the shell processing unit 500 is a device that produces cement by heat treating shell, which is a raw material, using gas generated in a double fluidized bed reactor, that is, product gas 10 and exhaust gas 20, as a heat source.

The shells used as raw materials can be shells of abalones, clams, oysters, corals, mussels, and whelks that exist in freshwater and marine life, but oyster shells are preferably used.

The shell processing unit 500 includes a shell preheating unit 510 that preheats the shell, which is a raw material; A preliminary decomposition furnace 520 that first heats and partially calcifies the shells supplied from the shell preheating unit 510; A main cracking furnace (530) that produces cement by heating the mixture supplied from the preliminary cracking furnace (520); and a cooling unit 540 that cools the cement supplied from the main decomposition furnace 530.

The shell preheating unit 510 includes a plurality of cyclones 511 arranged up and down, and is shown in the drawing as including five cyclones 511a, 511b, 511c, 511d, and 511e.

The shell, which is a raw material, is input into the cyclone 511a disposed at the top, and moves from the cyclone 511 disposed at the top to the cyclone 511 disposed at the bottom. At this time, it is preferable that the shell is washed to remove foreign substances and then introduced into the cyclone 511.

The raw material introduced into the upper part of each cyclone 511 rotates inside the cyclone 511 and moves to the bottom and flows into the next cyclone 511, and at the lower part of the cyclone 511, the high temperature discharged from the preliminary decomposition furnace 520 The gas moves from the bottom to the top of each cyclone 511 and is mixed with the raw material moving to the bottom to preheat the raw material.

At this time, the raw material rotates inside each cyclone 511 and moves to the next cyclone 511 through the lower discharge line 513 of the cyclone 511. At the same time, the heated gas present inside each cyclone 511 moves to the next cyclone 511 through the communication port 514 at the top of the cyclone 511, and at this time, the gas disposed at the top through the communication port 514 Some of the raw materials of the cyclone 511 may move.

In addition, in the drawing, the communication port 514 through which the heated gas moves each cyclone 511 sequentially connects each cyclone 511, and the discharge line 513 through which the raw material moves is connected to the communication port 514. It is shown to be connected, but this is an example, and the arrangement of the communication port 514 and the discharge line 513 is not necessarily limited to this. For example, the discharge line 513, like the communication port 514, is connected to each cyclone. (511) may be arranged to connect sequentially.

The cyclone 511a disposed at the top may be equipped with an exhaust means 512 for discharging gas whose temperature has been lowered by preheating the raw materials.

The preliminary decomposition furnace 520 receives preheated raw materials supplied from the cyclone 511e disposed at the lowest part, first heats them, and partially calcifies them. In the preliminary decomposition furnace 520, part of the calcium carbonate (CaCO ₃ ) contained in the shell is decomposed into carbon dioxide (CO ₂ ) and calcium oxide (CaO), and the carbon dioxide is decomposed into shell preheating unit 510 in the preliminary decomposition furnace 520. ), and the mixture containing calcium oxide and undecomposed calcium carbonate moves to the main decomposition furnace (530).

At this time, the exhaust gas 20 separated and discharged through the exhaust gas cyclone 210 of the double fluidized bed reactor is supplied to the preliminary decomposition furnace 520. At this time, the temperature of the exhaust gas 20 is in the range of 920 to 950 ° C. The interior of the preliminary decomposition furnace 520 is heated by the gas 20, so that calcium carbonate can be preheated and decomposed.

In addition, the exhaust gas 20 contains inorganic substances such as Ca, Si, Fe, Mg, etc. contained in worn fluids and waste plastic raw materials, and can be used as a raw material for cement.

The main cracking furnace 530 heats a mixture containing calcium carbonate and calcium oxide supplied from the preliminary cracking furnace 520. Accordingly, most of the calcium carbonate or the calcium carbonate supplied to the main decomposition furnace 530 is completely calcined to produce a mixture containing calcium oxide, that is, cement.

The main cracking furnace 530 has a cylindrical body arranged horizontally, the inlet of the main cracking furnace 530 is placed higher than the outlet, and the mixture supplied to the inlet of the main cracking furnace 530 is rotated about the central axis. Move it toward the exit.

At this time, on the outlet side of the main cracking furnace 530, the produced gas 10 discharged from the produced gas cyclone 140 of the double fluidized bed reactor is supplied and burned through the produced gas supply line 531. Thus, high-temperature gas having a temperature range of approximately 1300 to 1600° C. is supplied into the main decomposition furnace 530.

The high-temperature gas supplied from the outlet direction of the main cracking furnace 530 moves toward the entrance of the main cracking furnace 530 and calcifies the mixture inside the main cracking furnace 530, especially calcium carbonate. At this time, part of the mixture may melt due to the high temperature gas. The high-temperature gas moving toward the entrance of the main cracking furnace 530 moves to the preliminary cracking furnace 520, mixes with the gas components inside the preliminary cracking furnace 520, and moves to the shell processing unit 500 to produce raw materials. It can be calcined and preheated.

Meanwhile, the cement discharged from the main decomposition furnace 530 can be cooled through the cooling unit 540 and obtained as a solid in the form of powder or granules. In the cooling unit 540, cement can be cooled using various heat transfer media such as water and air, but preferably an air cooling method using cold wind can be applied.

Figures 2 and 3 are diagrams showing an example of the bubble fluidized bed gasifier 100, and are shown with part of the bubble fluidized bed gasifier 100 omitted.

As previously described, a center rod 130 is fixedly installed inside the bubble fluidized bed gasifier 100 in a vertical direction along the center of the bubble fluidized bed gasifier 100, and a screw blade is provided around the center rod 130. The shaped spiral wings 110 are combined.

The helical blade 110 can increase the frequency of contact between the produced gas 10 and the flowing medium, and the contact reaction between the tar contained in the produced gas 10 and the flowing medium increases.

A plurality of openings 115 may be formed in the spiral wing 110. The openings 115 are formed in plural numbers at intervals in the vertical direction, and part or all of the fuel and fluid medium falls under the spiral blade 110 through the openings 115, so that the steam and produced gas rising upward Efficient contact is easily achieved.

In order to maximize the contact between the fuel and fluid medium moving from the top to the bottom and the steam and generated gas moving from the bottom to the top, one end is in contact with the bottom of the opening 115 of the spiral blade 110 and A guide plate 116 is further provided that is coupled and includes a downwardly inclined surface extending in a direction opposite to the downwardly inclined direction of the spiral blade 110, so that the flow medium escaping through the opening 115 slopes down along the guide plate 116. It is composed of:

With this configuration, the flowing medium is prevented from escaping through the opening 115 too quickly, while the generated gas and steam rise around the guide plate 116, thereby lengthening the contact time.

The guide plate 116 is configured to rise upward from the portion in contact with the bottom of the opening 115 among the spiral wings 110 and then bend to go down. This configuration allows the flow medium coming down the spiral wing 110 to become more stable. This is to allow people to exit through the opening 115 and go down the information board 116.

Figure 4 is a diagram showing another embodiment of the bubble fluidized bed gasifier 100, and is shown with a part of the bubble fluidized bed gasifier 100 omitted.

As described above, inside the bubble fluidized bed gasifier 100, a center rod 130 is fixedly installed vertically along the center of the bubble fluidized bed gasifier 100, and the center rod ( Spiral wings 110 in the form of screw wings are coupled to the circumference of 130).

At this time, the spiral blade 110 in the form of a screw blade may be formed in a spiral shape by having a plurality of unit blades 111 radially coupled to the central rod 130, spaced apart from each other, and arranged in steps.

Therefore, macroscopically, the flow medium rotates and descends along the spiral blade 110 by the screw-shaped spiral blade 110, and the gas component including the generated gas 10 and steam 30 flows through the spiral blade 110. ) and moves upward. At the same time, microscopically, the reactant falls into the separation area, which is the empty space between each discontinuously disposed unit blade 111, so that it more frequently and effectively contacts the gas component moving upward while circling, producing gas 10. The generation efficiency and tar removal efficiency are significantly improved.

In other words, this spiral-shaped stepped arrangement increases the frequency with which the fluid medium comes into contact with the synthesis gas, and the tar contained in the synthesis gas is decomposed and reformed, which can significantly reduce the tar concentration in the synthesis gas. The short-circuit phenomenon in which gas escapes without contacting the fluid medium is prevented, thereby increasing the efficiency of tar removal from synthesis gas.

At this time, the cross section of the unit wing 111 perpendicular to the plane formed by the central axis of the central rod 130 and the longitudinal axis of the unit wing 111 is polygonal, and has a rectangular shape as shown in FIG. 4. It may have a shape such as a trapezoid (FIG. 5(a)), a triangle (FIG. 5(b)), a pentagon (FIG. 5(c)), etc., as shown in FIG. 5. It is also possible to form other polygons.

FIG. 6 is a top-view diagram of the bubble fluidized bed gasifier 100 observed from the direction a of FIG. 4, in which the two adjacent unit blades 111 of the spiral blade 110 overlap in some areas and are viewed from the top. When viewed, it appears as if there is no empty space between the unit blades 111, but in reality, since the unit blades 111 are positioned discontinuously, a spaced space, which is an empty space, exists between each unit blade 111.

Figure 7 shows a spiral wing 110 according to an example in which the unit wing 111 has a trapezoidal cross-section.

The cross section of the unit wings 111 is formed in a polygonal shape as described above, and it is more preferable that the separation area, which is an empty space between each unit wing 111, is formed in a shape that narrows from the top to the bottom.

Referring to the enlarged view of FIG. 7, when the distance (d1) between the uppermost ends of each unit wing (111a, 111b) adjacent to the separation area is formed to be larger than the distance (d2) between the lowermost ends, the gas component is separated from the separation area. Since the reverse flow phenomenon rising through the flow is prevented, it is preferable that d1 is formed larger than d2.

In particular, d1 can be formed to have a value 2 to 7 times that of d2, and if the distance ratio between d1 and d2 is outside this range, the reaction efficiency is improved by delaying the fall of the flowing medium falling through the separation area. Since is insignificant, d1 and d2 are preferably formed to have the above-mentioned ratio.

In addition, since the diameter of the flowing medium falling into the separation area is about 04 to 0.8 mm, the minimum width of the separation area between the two adjacent unit blades 111a and 111b is required to prevent fouling by the flowing medium. It is preferably formed in the range of 5 to 25 mm.

In particular, the width of the separation area is preferably formed to be tapered from the top to the bottom of each unit blade (111a, 111b). In this case, the fluid flow of the flowing medium falling through the separation area becomes smooth, and the gas component Through this spaced area, rising backflow phenomenon and subsequent fouling phenomenon can be prevented.

FIG. 8 is a diagram showing an example of the cross-sectional shape of the unit blade 111 constituting the spiral blade 110 of FIG. 4, where the unit blade 111 is formed at a predetermined angle with respect to the longitudinal axis of the unit blade 111. (θ) It may be arranged in a rotated state to have an inclined shape with respect to the floor surface, and the predetermined angle (θ) may be 40 to 80 degrees.

As the unit blades 111 are arranged in this way, the two surfaces extending from one edge located at the top of the unit blades 111 are formed to slope downward in different directions, and accordingly, they rotate and descend along the spiral blades 110. Since the flowing medium moves along the two downwardly sloping sides, the reactants are prevented from falling too quickly through the separation area, thereby extending the contact time between the reactants and the product gas (10) and steam (30), thereby improving reaction efficiency. You can get the effect.

Meanwhile, FIG. 9 is a diagram schematically showing the fluid flow of gas components including the fluidizing medium, product gas 10, steam 30, etc., when the unit blade 111 has a pseudo-trapezoidal cross-section. .

As shown in FIG. 9, some of the fluid medium stays in the separation area between each unit blade 111 and reacts by contacting the gas component in the upper area, and some reactants pass through the separation area and fall, contacting the gas component. react. In this way, as the frequency of contact between the fluid medium and the gas component significantly increases, the generation efficiency of the generated gas 10 and the efficiency of tar removal can be significantly improved.

Figure 10 is a diagram showing an embodiment of the unit blade 111 constituting the spiral blade 110 of the present invention. The unit blade 111 has at least one lower edge of the unit blade 111. A downwardly sloping extension 113 may be formed.

When the extension part 113 is formed in this way, the fluid medium moves along the extension part 113, so the fouling phenomenon in which the reactant cannot fall to the bottom of the separation area due to surface tension and the separation area is closed can be prevented. In addition, reaction efficiency can be improved by delaying the falling time of the fluid medium and increasing the contact time between the fluid medium and the steam 30 and the generated gas 10.

As an example, the extension portion 113 may be installed in all of the unit wings 111, or may be installed in only some of the unit wings 111, or may be installed in plural units in one unit wing 111. . It is preferable that the extension portion 113 is installed to have a regular pattern, but it can also be installed irregularly, and its shape or number is not particularly limited as long as it does not close the spaced area while allowing the flowing medium to fall downward. It can be.

Figure 11 is a diagram schematically showing a double fluidized bed reactor according to another embodiment of the present invention.

The double fluidized bed reactor according to this embodiment is spaced apart from the raw material input pipe 161 of the raw material input section 160 of the double fluidized bed reactor described with reference to FIG. 1 by a predetermined distance, and is formed to surround the raw material input pipe 161. Includes pipe 164. That is, the raw material input pipe 161 and the external pipe 164 have a double pipe shape in which the raw material input pipe 161 is disposed inside the external pipe 164.

At this time, the heat transfer medium 50 flows in the space S formed between the outer periphery of the raw material input pipe 161 and the inner periphery of the external pipe 164, thereby additionally heating the raw material input pipe 161. Therefore, liquefaction of the raw material supplied along the raw material input pipe 161 and generation of chlorine compounds can be accelerated, and thus chlorine compounds can be removed more efficiently.

The heat transfer medium 50 circulates through the space S and the heat exchanger 400, and the heat transfer medium 50 heated through the heat exchanger 400 flows into the space S and enters the raw material input pipe 161. is heated and discharged from the space S in a relatively low temperature state and supplied back to the heat exchanger 400.

The heat transfer medium 50 may be water or heat transfer oil, and the heat transfer oil may be mineral oil, glycol aqueous solution, paraffin, diarylalkane, polyphenyl derivative, aryl ether, dimethylsiloxane polymer, etc., but is not limited thereto. .

Exhaust gas 20 discharged through the exhaust gas cyclone 210 may be preferably used as a heat source for heating the heat transfer medium 50 in the heat exchanger 400. At this time, when the entire amount of exhaust gas 20 is input into the heat exchanger 400, the exhaust gas 20 discharged from the heat exchanger 400 is directly input into the preliminary decomposition furnace 520 or is filtered through the bag filter 410. After dust or harmful gases are removed, it can be put into the preliminary decomposition furnace 520.

Alternatively, a part of the exhaust gas 20 discharged through the exhaust gas cyclone 210 may be directly supplied to the preliminary decomposition furnace 520, and the remaining part may be input into the heat exchanger 400. In this case, the heat exchanger 400 The exhaust gas 20 introduced into 400 may be supplied directly to the preliminary decomposition furnace 520 or after passing through the bag filter 410.

Figure 12 is a diagram schematically showing a double fluidized bed reactor according to another embodiment of the present invention.

In one embodiment of the present invention shown in FIG. 1, the bubble fluidized bed gasifier 100 and the high-speed fluidized bed combustion furnace 200 are configured to be separated from each other, but another embodiment of the present invention shown in FIG. 12 is a bubble fluidized bed gasifier. (100) is configured to surround the high-speed fluidized bed combustion furnace (200).

In the case of a double fluidized bed reactor according to another embodiment of the present invention shown in FIG. 12, a high-speed fluidized bed combustion furnace (200) is installed in the space inside the center rod (130) of the spiral blade (110) installed inside the bubble fluidized bed gasifier (100). ) is located, and heat is transferred to the bubble fluidized bed gasifier (100) through the wall of the high-temperature high-speed fluidized bed combustion furnace (200), thereby maximizing heat transfer and minimizing heat loss, thereby reducing operating costs of the gasifier.

The raw material input portion 160 of the double fluidized bed reactor of another embodiment of the present invention shown in FIG. 12 is spaced apart from the raw material input pipe 161 at a predetermined distance, and surrounds the raw material input pipe 161, as described with reference to FIG. 11. It may include an external pipe 164 formed to allow the heat transfer medium 50 to flow in the space S between the raw material input pipe 161 and the external pipe 164.

The heat transfer medium 50 may be heated again through the heat exchanger 400 and then supplied to the space S. At this time, an external heat source may be used as a heat source to heat the heat transfer medium 50 in the heat exchanger 400. However, preferably, the exhaust gas 20 discharged from the high-speed fluidized bed combustion furnace 200 can be used.

Since the specific technical details related to this are the same as those described with reference to FIGS. 1 to 11, overlapping descriptions will be omitted.

Meanwhile, the present invention includes a cement production method using shells and waste plastic (hereinafter referred to as 'cement production method').

The cement production method according to this embodiment is a method of producing cement using the cement production device previously described with reference to FIGS. 1 to 12. Cement is produced by calcining the shell using the heat generated by heating waste plastic. It's about how to produce it. Therefore, in the cement production method according to this embodiment, redundant descriptions related to the cement production apparatus described with reference to FIGS. 1 to 12 will be omitted.

The cement production method according to this embodiment supplies waste plastic raw materials to a double fluidized bed reactor including a bubble fluidized bed gasifier 100 and a high-speed fluidized bed combustion furnace 200 and combusts them, thereby producing gas produced in the bubble fluidized bed gasifier 100. A waste plastic combustion step of generating (10) and generating exhaust gas (20) in a high-speed fluidized bed combustion furnace (200); and a cement production step of manufacturing cement through a preheating step, a preliminary decomposition step, and a main decomposition step of heating the shell as a raw material, and a cooling step of cooling the cooled object to be heated.

At this time, exhaust gas 20 is used as a heat source in the preliminary decomposition step, and produced gas 10 is used as a heat source in the main decomposition step.

First, the waste plastic combustion step includes supplying waste plastic raw materials, steam, and heated fluid medium to the bubble fluidized bed gasification furnace 100 to decompose the waste plastic raw materials; Reheating the fluidized medium by supplying and burning the fluidized medium discharged from the bubble fluidized bed gasifier (100) and char generated by decomposition of waste plastic raw materials to the high-speed fluidized bed combustion furnace (200); Filtering fine particles contained in the product gas (10) generated in the bubble fluidized bed gasification furnace (100) through the product gas cyclone (140) and discharging the gaseous components; and separating the components discharged from the high-speed fluidized bed combustion furnace 200 through the exhaust gas cyclone 210, transferring the fluidized medium to the bubble fluidized bed gasification furnace 100, and discharging the remaining exhaust gas 20. Includes.

In the step of decomposing the waste plastic raw materials by supplying waste plastic raw materials, steam, and heated fluid medium to the bubble fluidized bed gasifier 100, the waste plastic raw materials supplied to the bubble fluidized bed gasifier 100 are decomposed to produce gas ( 10) This is the step to create.

Waste plastic raw materials can be supplied to the bubble fluidized bed gasifier 100 through the raw material input unit 160 provided at the front of the bubble fluidized bed gasifier 100, and from the raw material input pipe 161 of the raw material input unit 160. The waste plastic raw material is mixed and transferred with the fluidized medium through the transfer screw 162, so that the waste plastic raw material can be smoothly supplied to the bubble fluidized bed gasification furnace 100 both in solid phase and in liquid phase.

In the bubble fluidized bed gasifier (100), waste plastic raw materials and fluid media are supplied through the raw material input pipe 161, steam and heated fluid media are additionally supplied to form a bubble fluidized bed, and the waste plastic raw materials are heated to decompose. I order it. The produced gas 10 generated here is discharged to the top, and the char and part of the fluidized medium move to the high-speed fluidized bed combustion furnace 200.

The step of supplying and burning the fluidized medium discharged from the bubble fluidized bed gasifier 100 and char generated by decomposition of waste plastic raw materials to the high-speed fluidized bed combustion furnace 200 and reheating the fluidized medium is bubble fluidized bed gasification. This is a step of reheating the fluid medium so that it can be reused as a heat source for the furnace 100.

At this time, char can be used as a heat source for heating the high-speed fluidized bed combustion furnace 200, and the char reacts with the air supplied to the high-speed fluidized bed combustion furnace 200 and combusts to generate heat, which heats the fluid medium. It is used as a heat source for

The product generated by combustion of the heated fluid medium and char is separated into the exhaust gas 20 and the heated fluid medium through the exhaust gas cyclone 210, and the heated fluid medium is returned to the bubble fluidized bed gasification furnace 100. It is supplied and functions as a heat source, and the high-temperature exhaust gas 20 is discharged to the outside and supplied to the preliminary decomposition furnace 520, which will be described later, to supply heat.

The step of filtering the fine particles contained in the product gas 10 generated in the bubble fluidized bed gasifier 100 through the product gas cyclone 140 and discharging the gas component is a step of discharging the gas component from the bubble fluidized bed gasifier 100. This is a step of separating and discharging only useful gas components such as hydrogen, carbon monoxide, and methane among the components produced by decomposition, and this process can be performed in the produced gas cyclone 140.

At this time, the fine particles that were not discharged here are supplied again to the bubble fluidized bed gasification furnace 100, and the produced gas 10 is supplied and burned to the main decomposition furnace 530, which will be described later, and functions as a heat source.

On the other hand, the cement manufacturing step includes supplying and preheating shell as a raw material to a shell preheating unit including a plurality of cyclones 511 arranged vertically; Supplying preheated shells and exhaust gas 20 to the preliminary decomposition furnace 520 to first heat the preheated shells; Supplying primary heated shells and generated gas 10 to the main cracking furnace 530, burning the generated gas 10 to secondary heat the primary heated shells to produce cement; and cooling the cement.

First, the shell used as a raw material for cement production is supplied to the shell preheating unit 510 including a plurality of cyclones 511 arranged vertically and preheated.

Specifically, when the shell is supplied to the upper part of the cyclone 511a located at the top, the shell rotates through the cyclone 511 and moves downward, communicating with the cyclone 511e located at the bottom of the shell preheating unit 510. It is put into the preliminary decomposition furnace 520.

At the same time, the high-temperature gas discharged from the preliminary decomposition furnace 520 moves upward from the cyclone 511e located at the bottom to the cyclone 511a located at the top, and is mixed with the raw material moving to the bottom to preheat the raw material. Afterwards, the gas component may be discharged to the top of the cyclone 511a located at the top.

Next, the step of first heating the preheated shell by supplying the preheated shell and exhaust gas 20 to the preliminary decomposition furnace 520 is to oxidize some of the calcium carbonate by calcining the preheated shell in the preliminary decomposition furnace 520. This is the stage of manufacturing with calcium.

At this time, the high temperature exhaust gas 20 previously supplied from the exhaust gas cyclone 210 can be used as a heat source for calcination.

Next, the step of supplying primary heated shells and produced gas 10 to the main cracking furnace 530, burning the produced gas 10, and secondary heating the primarily heated shells to produce cement, This is the step of producing calcium oxide, that is, cement, by calcining the remaining calcium carbonate that was not calcined in the preliminary decomposition furnace 520.

At this time, the product gas 10 supplied from the product gas cyclone 140 may be used as a heat source for calcination, and the product gas 10 is supplied and burned at the rear of the main decomposition furnace 530 to improve pyrolysis efficiency. You can.

The high-temperature gas generated in the main cracking furnace 530 is used to heat the calcium carbonate inside, and can then be supplied to the preliminary cracking furnace 520 through the front end of the main cracking furnace 530.

Finally, a cooling step is performed to cool the cement produced in the main cracking furnace 530. This step can be performed in various ways, such as water-cooling or air-cooling, but is preferably performed by air-cooling.

Meanwhile, an additional step may be performed to maintain the temperature of the raw material input pipe 161 of the raw material input unit 160 constant. In this case, the heated heat transfer medium 50 flows through the heat exchanger 400 in the outer pipe 164 formed to surround the outside of the raw material input pipe 161, and a heat exchanger (50) is used to heat the heat transfer medium 50. At least a portion of the exhaust gas 20 discharged from the exhaust gas cyclone 210 may be used as 400). In this way, the exhaust gas 20 used in the heat exchanger 400 can be supplied back to the preliminary decomposition furnace 520.

The present invention is not limited to the specific embodiments and descriptions described above, and various modifications can be made by anyone skilled in the art without departing from the gist of the invention as claimed in the claims. and such modifications fall within the protection scope of the present invention.

10: Produced gas 20: Exhaust gas
21: exhaust gas line 30: steam
40: air 50: heat transfer medium
100: Bubble fluidized bed gasifier 110: Spiral blade
111: unit wing 113: extension part
120: bubble fluid bed 130: center rod
140: Produced gas cyclone 150: Produced gas cyclone connector
160: Raw material input unit 161: Raw material input pipe
162: transfer screw 163: discharge pipe
164: External pipe 170: Gasifier connector
200: High-speed fluidized bed combustion furnace 210: Exhaust gas cyclone
220: exhaust gas cyclone connector 221: valve
230: first fluid medium supply pipe 240: second fluid medium supply pipe
300: Raw material tank 400: Heat exchanger
500: shell processing unit 510: shell preheating unit
520: preliminary decomposition furnace 521: exhaust gas supply line
530: Main cracking furnace 531: Produced gas supply line
540: Cooling unit

Claims (8)

Raw material tank where waste plastic raw materials are stored;
A bubble fluidized bed gasification furnace in which raw materials are supplied from the raw material tank through the raw material input unit, steam flows in from the bottom and the fluidized medium flows inside, thereby forming a bubble fluidized layer, and the raw materials are gasified to produce produced gas inside;
Char contained in the fluidized medium and the produced gas is transferred from the bubble fluidized bed gasifier, air is additionally supplied, the fluidized medium is heated by burning the char, and the heated fluidized medium is heated. A high-speed fluidized bed combustion furnace transferred to the bubble fluidized bed gasifier;
a produced gas cyclone that is in communication with the bubble fluidized bed gasifier and separates fine particles from the produced gas discharged from the bubble fluidized bed gasifier, re-introduces the fine particles into the bubble fluidized bed gasifier, and discharges the remainder;
It is connected between the upper part of the high-speed fluidized bed combustion furnace and the upper part of the bubble fluidized bed gasifier, and after separating the fluidized medium from the exhaust gas, the exhaust gas is discharged and the fluidized medium is separately supplied to the bubble fluidized bed gasifier and the raw material input section. gas cyclone; and
It includes a shell processing unit that generates cement by heating the shell using the generated gas and exhaust gas,
The produced gas contains 40 to 70 vol% of hydrogen,
The shell processing unit includes a shell preheating unit 510 that preheats the shell; A preliminary decomposition furnace 520 for heating and partially calcining the shell supplied from the shell preheating unit 510; a main cracking furnace (530) for producing cement by heating the mixture supplied from the preliminary cracking furnace (520); And a cooling unit 540 that cools the cement supplied from the main cracking furnace 530,
Exhaust gas discharged from the exhaust gas cyclone is used as a heat source for the preliminary cracking furnace 520, and produced gas discharged from the produced gas cyclone is used as a heat source for the main cracking furnace 530,
A portion of the fluidized medium heated in the high-temperature fluidized bed combustion furnace 200 is supplied to the raw material input pipe 161 and mixed with the raw material, and the ratio of the volumetric flow rate of the fluidized medium and the raw material is 5 to 10. and cement manufacturing equipment using waste plastic. According to paragraph 1,
Inside the bubble fluidized bed gasifier, a center rod positioned vertically along the center of the bubble fluidized bed gasifier; and a spiral wing that moves the generated gas and steam in a swirling flow along the central rod. A cement manufacturing device using shell and waste plastic, characterized in that installed. delete delete delete A waste plastic combustion step of supplying waste plastic raw materials to a double fluidized bed reactor including a bubble fluidized bed gasifier and a high-speed fluidized bed combustion furnace for combustion to generate product gas in the bubble fluidized bed gasifier and generating exhaust gas in the high-speed fluidized bed combustion furnace; and
A cement manufacturing step of manufacturing cement through a preheating step, a preliminary decomposition step, and a main decomposition step of heating the shell as a raw material, and a cooling step of cooling the cooled object to be heated;
Exhaust gas is used as a heat source in the preliminary decomposition step, and produced gas is used as a heat source in the main decomposition step, and the produced gas contains 40 to 70 vol% of hydrogen,
The cement manufacturing step includes supplying and preheating shell, which is a raw material, to a shell preheating unit including a plurality of cyclones arranged up and down; Supplying preheated shells and exhaust gas to a preliminary decomposition furnace to first heat the preheated shells; Supplying primary heated shells and produced gas to the main decomposition furnace, burning the produced gas, and secondary heating the primarily heated shells to produce cement; and cooling the cement.
Exhaust gas discharged from the exhaust gas cyclone is used as a heat source for the preliminary cracking furnace 520, and produced gas discharged from the produced gas cyclone is used as a heat source for the main cracking furnace 530,
A portion of the fluidized medium heated in the high-temperature fluidized bed combustion furnace 200 is supplied to the raw material input pipe 161 and mixed with the raw material, and the ratio of the volumetric flow rate of the fluidized medium and the raw material is 5 to 10. and cement manufacturing method using waste plastic. The method of claim 6, wherein the step of burning waste plastic,
Decomposing waste plastic raw materials by supplying waste plastic raw materials, steam, and heated fluid medium to a bubble fluidized bed gasifier;
Reheating the fluidized medium by supplying and burning the fluidized medium discharged from the bubble fluidized bed gasifier and char generated by decomposition of waste plastic raw materials to a high-speed fluidized bed combustion furnace;
Filtering fine particles contained in the product gas generated in the bubble fluidized bed gasification furnace through a product gas cyclone and discharging the gaseous components; and
A cement manufacturing method using shells and waste plastics, including the step of separating components discharged from the high-speed fluidized bed combustion furnace through an exhaust gas cyclone, transferring the fluidized medium to the bubble fluidized bed gasification furnace, and discharging the remaining exhaust gas.
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