KR102676398B1 - Manufacturing process of recyled oil using continuous waste vinyl pyrolysis unit with screw pre-heating unit - Google Patents

Abstract

The present invention includes a pretreatment step (S10) of heating waste vinyl, which is a raw material, to remove moisture, volatile matter, and chlorine; A pyrolysis step (S20) of thermally decomposing the pretreated raw material by heating it in a continuous reactor; A first cooling step (S30) in which the pyrolyzed raw materials are cooled in a rapid cooling tank and separated into high boiling point oil and gas; A high boiling point oil separation step (S40) in which the high boiling point oil generated in the first cooling step (S30) is separated into supernatant oil and precipitated oil by leaving it in a separation device for a predetermined period of time; A secondary cooling step (S50) of cooling the gas that has passed the first cooling step (S30) in a condensation tank and separating it into condensed oil and non-condensed gas; And a reclaimed oil storage step (S60) of collecting the supernatant oil produced in the high boiling point oil separation step (S40) and the condensed oil produced in the secondary cooling step into a storage tank to generate reclaimed oil; is performed continuously, This relates to a method of producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility. Since the pyrolysis temperature load is reduced by the screw preheating facility, the production efficiency of recycled oil can be improved.

Description

Method for producing recycled oil using continuous waste vinyl pyrolysis unit with screw pre-heating unit {Manufacturing process of recyled oil using continuous waste vinyl pyrolysis unit with screw pre-heating unit}

The present invention relates to a process for producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility. More specifically, the process for producing recycled oil can be improved by reducing the pyrolysis temperature load by using a screw preheating facility. This relates to a process for producing recycled oil using a continuous waste vinyl pyrolysis device.

In the case of waste vinyl generated at home and at work, most of it is waste vinyl subject to EPR (Expanded Producer Responsibility), and each local government is responsible for collecting waste vinyl. Disposal of waste vinyl is emerging as a major environmental problem.

In order to solve this problem, efforts are being made to process waste vinyl and use it for purposes such as solid fuel or recycled raw materials. However, due to the lack of facilities to process waste vinyl, the disposal of waste vinyl is not only an environmental problem, but also a social problem. It's leading to problems.

Accordingly, various attempts have been made to develop a process that can improve added value by recovering the recycled oil produced by pyrolyzing waste vinyl and recycling the recycled oil to various industries. However, the continuous treatment process in which actual commercial operation is normally carried out is not possible. It is not developed yet.

In the case of waste vinyl, it contains various foreign substances and about 10-20% moisture, and in the case of some waste vinyl, it contains chlorine compounds such as PVC, and hydrochloric acid (HCl) is generated during thermal decomposition, which is harmful to workers. In addition to polluting the environment and corroding equipment, there is a possibility that the final products, such as recycled oil and solid fuel, may contain a large amount of hydrochloric acid, so a process to remove hydrochloric acid must be carried out first.

On the other hand, since the temperature at which waste vinyl is normally thermally decomposed is approximately 450-500℃, various obstacles occur in the process until waste vinyl in bulk at room temperature is heated to the thermal decomposition temperature to produce recycled oil. Due to this, it is difficult to develop a process that can be practically commercialized.

In particular, when the heating load of the pyrolysis emulsification process is concentrated in one place, the temperature deviation inside the reactor increases, and the yield of pyrolysis regenerated oil decreases to about 50%, making the process uneconomical.

Accordingly, in the process of producing recycled oil using waste vinyl, various obstacles in the process are removed, heat load is distributed to enable high-yield recycled oil production, and a new waste vinyl pyrolysis process is available for commercial use. development is needed.

Registered Patent No. 10-1260760 (registered on April 29, 2013)

The present invention seeks to provide a process for producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating equipment, which can improve the production efficiency of recycled oil by reducing the pyrolysis temperature load.

One embodiment of the present invention includes a pretreatment step (S10) of heating waste vinyl, which is a raw material, to remove moisture, volatile matter, and chlorine; A pyrolysis step (S20) of thermally decomposing the pretreated raw material by heating it in a continuous reactor; A first cooling step (S30) in which the pyrolyzed raw materials are cooled in a rapid cooling tank and separated into high boiling point oil and gas; A high boiling point oil separation step (S40) in which the high boiling point oil generated in the first cooling step (S30) is separated into supernatant oil and precipitated oil by leaving it in a separation device for a predetermined period of time; A secondary cooling step (S50) of cooling the gas that has passed the first cooling step (S30) in a condensation tank and separating it into condensed oil and non-condensed gas; And a reclaimed oil storage step (S60) of collecting the supernatant oil produced in the high boiling point oil separation step (S40) and the condensed oil produced in the secondary cooling step into a storage tank to generate reclaimed oil; is performed continuously, This relates to a method of producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility.

The precipitated oil obtained in the high boiling point oil separation step (S40) may be returned to a continuous reactor where the pyrolysis step is performed.

A portion of the reclaimed oil obtained in the reclaimed oil storage step (S60) may be transferred to a quench tank where the primary cooling step (S30) is performed and sprayed.

The non-condensed gas obtained in the secondary cooling step (S50) can be used as a heat source in at least one of the pretreatment step (S10) and the pyrolysis step (S20).

The pretreatment step (S10) includes a first pretreatment step (S11) in which raw materials are supplied to a primary screw preheating facility and heated to 250-300°C; and a second pretreatment step (S12) in which the raw material that has undergone the first pretreatment step is supplied to a secondary screw preheating facility and heated to 300-330°C.

Between the first cooling step (S30) and the high boiling point oil separation step (S40), the high boiling point oil generated in the first cooling step (S30) is supplied to a buffer tank, left to stand for a predetermined time, and then supplied to the separation device. (S31); can be performed.

The recycled oil can be supplied to the distillation column and separated into low boiling point, medium boiling point and high boiling point.

The non-condensed gas obtained in the secondary cooling step (S50) can be used as fuel to heat the distillation column.

Before the pretreatment step (S10), a raw material preparation step (S00) of removing non-combustible materials charged together with the waste vinyl as a raw material and molding the waste vinyl as a raw material into a predetermined size may be included.

In the process of producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility of the present invention, the pyrolysis temperature load is reduced by providing a screw preheating facility, so the production efficiency of recycled oil can be improved.

Figure 1 is a process diagram for producing recycled oil using a continuous waste vinyl pyrolysis device according to an embodiment of the present invention.
Figure 2 is a block diagram briefly showing a continuous waste vinyl pyrolysis device according to an embodiment of the present invention.
Figure 3 is a conceptual diagram showing a screw reactor according to the first embodiment.
Figure 4 is a cross-sectional view taken along line AA of Figure 3.
Figure 5 is a perspective view of the inner tube connector of Figure 3.
Figure 6 is a conceptual diagram showing a screw reactor according to the second embodiment.
Figure 7 is a cross-sectional view taken along line BB of Figure 6.
Figure 8 is a schematic diagram of a distillation column.

Before explaining in detail the preferred embodiments of the present invention below, terms and words used in the present specification and claims should not be construed as limited to their usual or dictionary meanings, but rather have meanings that are 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 component, this means that it may further include other components rather than excluding other components, unless specifically stated to the contrary.

The identification code for each step is used for convenience of explanation. The identification code does not explain the order of each step, and each step may be performed differently from the specified order unless a specific order is clearly stated in the context. there is. 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.

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. .

Below, we will look at embodiments of the present invention. However, the scope of the present invention is not limited to the following preferred embodiments, 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 process for producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating equipment, which can improve the production efficiency of recycled oil by reducing the pyrolysis temperature load.

Figure 1 is a process diagram for producing recycled oil using a continuous waste vinyl pyrolysis device according to an embodiment of the present invention, and Figure 2 is a block diagram briefly showing a continuous waste vinyl pyrolysis device according to an embodiment of the present invention.

The process for producing recycled oil using a continuous waste vinyl pyrolysis device according to an embodiment of the present invention includes a pretreatment step (S10) of heating waste vinyl, which is a raw material, to remove moisture, volatile matter, and chlorine; A pyrolysis step (S20) of thermally decomposing the pretreated raw material by heating it in a continuous reactor; A first cooling step (S30) in which the pyrolyzed raw materials are cooled in a rapid cooling bath (130) to separate them into high boiling point oil and gas; A high boiling point oil separation step (S40) in which the high boiling point oil that has undergone the first cooling step is left in the separation device 140 for a predetermined period of time to separate it into supernatant oil and precipitated oil; A second cooling step (S50) in which the gas that has undergone the first cooling step is cooled in the condensation tank 150 and separated into condensed oil and non-condensed gas; and a reclaimed oil storage step (S60) of generating reclaimed oil by collecting the supernatant oil produced in the high boiling point oil separation step and the condensed oil produced in the secondary cooling step in the storage tank 160. are performed continuously.

First, the pretreatment step (S10) is a step of removing moisture, volatile matter, and chlorine from waste vinyl, which is a raw material, and preheating the raw material.

In this step, the raw material is preheated and the load on the continuous reactor in which thermal decomposition is performed in the thermal decomposition step (S20) is reduced, so the efficiency of producing high boiling point oil in the thermal decomposition step (S20) can be significantly improved.

The pretreatment step (S10) includes a first pretreatment step (S11) of supplying the waste vinyl raw material to the primary screw preheating equipment (111) and heating it to 250-300°C; and a second pretreatment step (S12) in which the raw material that has undergone the first pretreatment step is supplied to the secondary screw preheating equipment 112 and heated to 300-330°C.

The first pretreatment step (S11) is a step in which waste vinyl, which is a raw material, is supplied to the primary screw preheating facility 111 and heated to 250 to 300° C. to melt it. Through this step, moisture and volatile matter contained in waste vinyl can be removed. Preferably, a filter is provided at the rear of the primary screw preheating equipment 111, so that solid raw materials or foreign substances remaining unmelted are filtered out, and then only the melted raw materials can be introduced into the second pretreatment step (S12).

The second pretreatment step (S12) is a step in which the raw material from which moisture and volatile matter has been removed through the first pretreatment step (S11) is supplied to the secondary screw preheating equipment 112 and heated to 300-330°C. Through this step, chlorine compounds, such as hydrochloric acid, generated from waste vinyl raw materials containing chlorine such as PVC can be removed, so no hydrochloric acid is generated during the process, ensuring the safety of workers, and hydrochloric acid is removed in advance. Therefore, corrosion of equipment can be prevented in subsequent processes and the hydrochloric acid content in recycled oil can be reduced.

At this time, a filter is provided at the rear of the secondary screw preheating facility 112, so that only molten raw materials excluding non-meltable materials can be input into the pyrolysis step (S20).

In this way, the pretreatment step (S10) is divided into a first pretreatment step (S11) at a relatively low temperature and a second pretreatment step (S12) at a relatively high temperature, so that moisture, volatile matter, and chlorine, which are unnecessary components contained in the raw materials, are removed. can be removed efficiently.

In particular, since the chlorine content is removed in the second pretreatment step (S12), an additional process to separately remove the chlorine content from the mixture of unnecessary components generated in the pretreatment step (S10) can be omitted, and the primary The heat load of the screw preheating facility 111 and the secondary screw preheating facility 112 can be reduced.

The first screw preheating facility 111 and the secondary screw preheating facility 112 may be the screw reactor shown in FIG. 3.

First, FIGS. 3 to 5 relate to a screw reactor according to the first embodiment, FIG. 3 is a conceptual diagram showing the screw reactor, FIG. 4 is a cross-sectional view taken along line A-A of FIG. 3, and FIG. 5 is a perspective view of the inner cylinder connector. am.

The screw reactor includes a plurality of screws 20 that agitate and transport waste plastic to the outlet, a jacket 10 that covers the screws 20 from the outside, and moisture generated from the waste plastic inside the jacket 10. , an exhaust port 15 through which volatile matter and chlorine are discharged, and a heat medium oil supply pump P1 that supplies heat medium oil to the jacket 10.

Referring to Figures 3 and 4, the screw reactor according to the first embodiment is provided with a pair of screws 20 arranged upward and downward, and the heat medium oil flowing into the jacket 10 can flow inside the screw shaft. An inner cylinder 21 is formed, and the jacket 10 is divided into upper and lower parts according to the position of the screw 20, and has a structure in which an outer cylinder 11 through which the heat medium oil can flow is formed.

Referring to FIG. 4, an outer cylinder 11 through which the heat medium oil can flow is formed around the jacket 10, and the inside of the outer cylinder 11 is divided according to the position of the pair of screws 20 arranged upward and downward. It is divided into upper and lower parts.

In dividing the interior of the outer cylinder 11 up and down to block the flow of heat medium oil between the upper and lower parts of the outer cylinder 11, the inner wall and the outer wall of the outer cylinder 11 are located at the midpoint in the vertical direction inside the outer cylinder 11. The diaphragm 12 connecting the diaphragms (not shown) is formed continuously in the horizontal direction.

Outside the jacket 10, there is an inner tube connecting the inner tubes 21 to each other so that the heat medium oil flowing into the inner tube 21 of the screw located on the lower side can flow into the inner tube 21 of the screw located on the upper side. A connector 40 is installed.

In addition, outside the jacket 10, there is a device interconnecting the jacket 10 and the inner cylinder 21 of the screw so that the heat medium oil can continuously flow between the jacket 10 and the inner cylinder 21 of the screw. External pipe connectors 31 and 32 are installed.

The outer tube connectors 31 and 32 include a lower connector tube 31 that connects the lower part of the jacket 10 and the inner tube 21 of the screw located on the lower side of the plurality of screws 20, It includes an upper connection pipe 32 that connects the upper part of the jacket 10 and the outer cylinder 11 of the screw 20 located at the upper side of the plurality of screws 20.

The lower part of the outer cylinder 11 of the jacket is connected to the inner cylinder 21 of the screw located on the lower side among the plurality of screws 20 by the outer cylinder connectors 31 and 32, and the outer cylinder 11 of the jacket The upper part is connected to the inner cylinder 21 of the screw located at the upper side among the plurality of screws 20.

The heat medium flowing into the lower part of the outer cylinder 11 of the jacket through the connection structure of the outer cylinder 11 of the jacket, the inner cylinder 21 of the screw, the inner cylinder connector 40, and the outer cylinder connectors 31 and 32 as described above. Oil is the lower part of the outer cylinder 11 of the jacket, the inner cylinder 21 of the screw located on the lower side of the screw 20, the inner cylinder 21 of the screw located on the upper side of the screw 20, and the outer cylinder of the jacket ( 11) As it sequentially passes through the upper part, heat transfer is performed to remove moisture, volatile matter, and chlorine from the waste plastic.

The screw axis of the screw 20 is installed so that both ends protrude outside the jacket 10, and the intersection between the screw axis of the screw 20 and the jacket side wall 13 extends outside the jacket 10. At the (connection portion), a jacket fixing mechanical seal 51 is installed to rotatably couple the screw axis of the screw 20 to the side wall 13 of the jacket.

As the pair of screws 20 are provided, the jacket fixing mechanical seal 51 is installed at four locations corresponding to the intersection between both ends of each screw shaft and the jacket 10.

At both ends of the screw shaft of the screw 20 located outside the jacket 10, an inner cylinder connection mechanical seal 52 rotatably couples the screw shaft of the screw 20 to the end of the inner cylinder connector 40. And, an outer cylinder connection mechanical seal (53) rotatably coupled to the ends of the outer cylinder connection pipes (31, 32) is installed.

The jacket fixing mechanical seal (51), the inner cylinder connection mechanical seal (52), and the outer cylinder connection mechanical seal (53) are selected from among known mechanical seals in comprehensive consideration of the size, processing capacity, working conditions, etc. of the device. Since it is desirable to apply it, detailed descriptions of its structure and principles are omitted.

Generally, a mechanical seal has a structure that includes a ceramic ring and a carbon ring spring, and the outer diameter part of the ceramic ring and the inner diameter part of the housing (housing part) are sealed with an o-ring, and the inner diameter part of the carbon ring and the outer diameter of the shaft (shaft part) are sealed. ) is sealed with an o-ring, and the carbon ring is pushed by a spring so that the surfaces of the ceramic ring and the carbon ring meet and are driven, and sealing is achieved with that surface.

In addition, the jacket fixing mechanical seal (51), the inner cylinder connection mechanical seal (52), and the outer cylinder connection mechanical seal (53) are representatively selected and described as those judged to be most suitable for application to the embodiments of the present invention, It is not limited to a specific member or structure as long as the screw 20 can be rotatably fixed and supported while implementing an airtight structure capable of preventing loss of heat medium oil using other seal members.

In particular, the jacket fixing mechanical seal 51 is sufficient to airtighten the outer peripheral surface of the screw shaft of the screw 20 and the side wall 13 of the jacket, so it is possible to prevent the outflow of melted waste plastic inside the jacket 10. If a pressurized packing structure is implemented, it is desirable to apply an economical and robust sealing member with a simpler structure.

By rotating the upper and lower screws 20 in opposite directions, waste plastic is transferred from one side of the jacket 10 where the sample supply hopper is located to the other side, and the waste plastic is melted, so that the inside of the jacket 10 The discharge port 17 for discharging the waste plastic to the outside is preferably formed between the upper and lower screw shafts, where the transport force of the waste plastic is most smooth.

Accordingly, the discharge port 17 is located to overlap or intersect spatially with the inner cylinder connector 40 connecting the upper and lower screw shafts. This difficulty is due to the lung discharged through the discharge port 17. This can be easily solved by forming the inner tube connector 40 in a bent shape that can avoid the flow path with the plastic.

Referring to Figures 3 and 5, when forming the inner tube connector 40, the vertical extension portion 43 connecting the upper and lower ends is positioned forward or rearward compared to the upper and lower ends. By having a bent L-shaped bend, both installation and external discharge of waste plastic using the jacket fixing mechanical seal 51 and the inner cylinder connecting mechanical seal 52 can be easily implemented.

It is preferable that the heat medium oil is heated to a temperature of 250 to 330° C. in a heat medium boiler and then supplied to the jacket 10.

Specifically, the heat medium oil supplied to the primary screw preheating equipment 111 used in the first pretreatment step (S11) may be heated to 250 to 300°C and supplied, and the heat medium oil used in the second pretreatment step (S12) may be supplied. The heat medium oil supplied to the primary screw preheating equipment 112 may be supplied heated to 300-330°C.

The jacket fixing mechanical seal 51, the outer cylinder connection mechanical seal 53, the inner cylinder connection mechanical seal 52, etc. may include a material that melts in a temperature range of 250 to 330°C.

Accordingly, to prevent damage to the jacket fixing mechanical seal 51, the outer cylinder connection mechanical seal 53, and the inner cylinder connection mechanical seal 52 due to the high temperature of the heat medium oil, the jacket fixation mechanical seal 51 and the outer cylinder connection mechanical seal are installed. It is additionally provided with a coolant circulation device (60) that supplies coolant to the seal (53) or the inner cylinder connection mechanical seal (52).

The cooling water circulation device 60 includes a cooler 61 for cooling the cooling water, the cooling water is connected to the outlet of the cooler 61, one side and the other of the pair of inner cylinder connecting mechanical seals 52, and a pair of outer cylinders. It has a structure including a coolant circulation line 62 that sequentially passes through one side and the other side of the mechanical seal 53 and the inlet of the cooler 61, forming a continuously circulated coolant flow path.

Cooling water can be cooled to a certain temperature in the cooler 61 and supplied to the inner cylinder connection mechanical seal 52, and if antifreeze is used as the coolant, it can be applied without difficulty even in winter.

When a coolant flow path (not shown) communicating with the coolant circulation line 62 is formed inside the inner cylinder connecting mechanical seal 52 and the outer cylinder connecting mechanical seal 53, the inner diameter portion is formed through more direct heat exchange with the coolant. It can effectively prevent overheating damage to soft sealing members, etc.

A structure in which a screw movable chain 70 that transmits the rotational force of the motor (P2) to the screw 20 and rotates it is coupled to the screw shaft of the plurality of screws 20 extending outside the jacket 10. And, by the screw movable chain 70, the plurality of screws 20 can be easily rotated simultaneously from the outside of the jacket 10.

The screw movable chain 70 is representatively selected and described as the one judged to be most suitable for application to the embodiment of the present invention, and is capable of transmitting rotational force to the plurality of screws 20 from the outside of the jacket 10. It is not limited to specific members and structures, including belt members, etc.

First, FIGS. 6 and 7 relate to a screw reactor according to the second embodiment. FIG. 6 is a conceptual diagram showing the screw reactor, and FIG. 7 is a cross-sectional view taken along line B-B of FIG. 6.

Referring to Figures 6 and 7, compared to the first embodiment, the screw reactor according to the second embodiment has an inner tube insert 80 installed inside the inner tube 21 to It has a structure with a smaller cross-sectional area.

In order to fix the inner cylinder insert 80 at a designated position inside the inner cylinder 21, a connecting member such as the inner cylinder connector 81 in FIG. 7 may be coupled to the inner wall of the inner cylinder 21 by welding or the like. . The inner tube connection portion 81 is formed continuously along the longitudinal direction of the inner tube 21, or is formed spaced apart at a number of locations along the longitudinal direction of the inner tube 21, or is formed in addition to the upper and lower two locations, It may also be formed in a radial shape like spokes of a wheel.

If the cross-sectional area of the inner tube 21 and the cross-sectional area of the upper or lower part of the outer tube 11 separated by the diaphragm 12 are different, stagnation of heat medium oil may occur partially, and the inner tube 21 As the cross-sectional area becomes smaller, the flow rate of heat medium oil increases, thereby reducing temperature deviation in the flow direction or longitudinal direction.

By installing the inner cylinder insert 80, the cross-sectional area of the inner cylinder 21 can be reduced and adjusted to compensate for the difference in cross-sectional area or passing flow rate with the outer cylinder 11, and the heat medium oil in the inner cylinder 21 can be compensated. Heat transfer efficiency can be further improved by increasing the flow rate.

The inner cylinder insert 80 has a bar or cylinder shape that extends continuously along the longitudinal direction of the inner cylinder 21, and when both ends are formed in a cone shape, the heat medium oil travels along the conical inclined surface and the inner cylinder insert ( Since it flows flexibly between the inner tube insert 80 and the inner tube 21, the heat medium oil flowing into the inner tube insert 80 or flowing out of the inner tube insert 80 suffers from pressure loss, friction, and pressure due to rapid changes in the cross-sectional area of the flow path. It can prevent fluidity from deteriorating due to shocks, vortices, etc.

The diameter of the inner tube connection pipe 40 and the outer tube connection pipes 31 and 32 may be smaller than the diameter of the screw axis of the screw 20, and in this way, the screw shaft of the screw 20 and the inner tube connection pipe 40 ), if there is a difference in diameter between the outer cylinder connection pipes (31, 32), a reducer is additionally installed on the connection end of one side with a relatively small diameter to compensate for the diameter difference, and the inner cylinder connection mechanical seal ( 52) and the external cylinder connection mechanical seal (53) can be installed.

When using a screw reactor having the above configuration, in removing moisture, volatile matter, and chlorine from waste plastic, the heat medium oil is placed below the outer cylinder 11 of the jacket and the lower part of the plurality of screws 20. The inside of the jacket 10 is sequentially passed through the inner cylinder 21 of the screw, the inner cylinder 21 of the screw located on the upper side among the plurality of screws 20, and the upper portion of the outer cylinder 11 of the jacket. A heat medium circulation heating structure capable of heat processing the waste plastic can be implemented.

In addition, in supplying coolant to the outer cylinder connection mechanical seal 53 or the inner cylinder connection mechanical seal 52 to prevent overheating damage to the inner cylinder connection mechanical seal 52 and the outer cylinder connection mechanical seal 53, the coolant is It sequentially passes through the outlet of the cooler (61), one side and the other of the pair of inner cylinder connecting mechanical seals (52), one side and the other of the pair of outer cylinder connecting mechanical seals (53), and the inlet of the cooler (61). It can be circulated.

Moisture, volatile matter, and chlorine discharged during the heating process of waste plastic are discharged through the exhaust port 15, and are transferred to a designated processing location and removed by a vacuum pump (not shown).

The description continues with reference to FIGS. 1 and 2.

Before the pretreatment step (S10), a raw material preparation step (S00) may be performed in which non-combustible materials charged together with the waste vinyl as a raw material are removed and the waste vinyl as a raw material is molded into a predetermined size.

The raw material preparation step (S00) includes a raw material selection step (S01) of removing foreign non-combustible materials; and a raw material molding step (S02) in which the selected raw materials are molded into a predetermined size.

The raw material selection step (S01) is a step of removing foreign substances such as glass, metal materials, and ceramics that are charged together with the waste vinyl as a raw material. This step can be performed manually or automatically, for example, by blowing on the raw material. It can be performed using a wind-powered sorting method that applies wind using a fan to sort raw materials according to particle size and specific gravity.

The raw material forming step (S02) is to easily supply the waste vinyl raw material obtained through the raw material selection step (S01) to the first and second screw preheating facilities (111, 112) where the pretreatment step (S10) is performed. This is the molding stage. This step may be a step of cutting and molding the selected raw materials into a certain size and shape using, for example, a ring die sorter. Through this step, the raw material can be processed and prepared into pellet form.

The pyrolysis step (S20) is a step of thermal decomposition by heating the raw material prepared through the pretreatment step (S10).

In this step, raw materials are introduced into the stirred continuous reactor (CSTR) 120 and heated to 450-500°C. Since the raw materials preheated through the previous pretreatment step (S10) are input into this step, the heat load on the stirred continuous reactor 120 can be reduced.

In particular, when the raw material is directly pyrolyzed without going through the pretreatment step (S10), it is difficult to keep the temperature of the stirred continuous reactor 120 constant, resulting in a low yield of pyrolysis gas of about 50%. Foreign substances, moisture, volatile matter, and chlorine are removed through step (S10), and when the preheated raw material is pyrolyzed, the temperature of the stirred continuous reactor 120 is maintained constant, resulting in a high pyrolysis gas production yield of about 75% or more. Therefore, a yield improvement of about 50% can be achieved compared to the case where the pretreatment step (S10) is not performed, and stable process operation is possible.

The external cylinder of the stirred continuous reactor 120 may be directly heated, and the internal temperature of the stirred continuous reactor 120 may be maintained in the range of 450 to 500°C.

If the internal temperature of the stirred continuous reactor 120 is less than 450°C, the conversion rate to pyrolysis gas decreases, causing a problem that the pyrolysis gas yield is significantly lowered. If it exceeds 500°C, the production rate of non-condensable gas increases, causing a problem that the conversion rate to pyrolysis gas decreases significantly. Since the recovery rate of usable condensable gas is low, it is important to adjust the internal temperature of the stirred continuous reactor 120 to the above-mentioned temperature range. For this purpose, the temperature of the external cylinder of the stirred continuous reactor 120 may be heated to maintain the range of 700 to 800°C.

The stirred continuous reactor 120 may be installed singly or in two or more units. When two or more stirred continuous reactors 120 are installed, each reactor can be operated simultaneously or alternately to allow the continuous waste vinyl pyrolysis device to operate continuously.

In this step, the gas generated through pyrolysis is introduced into the first cooling step (S30), and the residue remaining after failing to pyrolyze can be discharged through a residue discharge device installed at the bottom of the stirred continuous reactor 120.

The first cooling step (S30) is a step of cooling the pyrolysis gas obtained through the pyrolysis step (S20) and separating it into high boiling point oil and gas.

Cooling at this stage can be performed by spraying the reclaimed oil generated in the reclaimed oil storage step (S60), which will be described later, onto the upper part of the quenching tank 130 into which the pyrolysis gas is introduced. Since the reclaimed oil produced in the reclaimed oil storage step (S60) has a temperature range of about 30 to 50°C, the low temperature of the reclaimed oil itself is maintained even if a separate cooling device is not used for cooling in the first cooling step (S30). Because primary cooling can be performed, energy efficiency is excellent.

In this way, the pyrolysis gas is quickly cooled, and the gaseous high boiling point oil contained in the pyrolysis gas is cooled and changes into a liquid phase. The liquid high-boiling oil produced in this way is input to the high-boiling oil separation step (S40), and the uncondensed gas remaining without cooling is input to the secondary cooling step (S50).

The high boiling point oil separation step (S40) is a step in which the high boiling point oil generated in the first cooling step (S30) is left in the separation device 140 for a predetermined period of time to separate it into supernatant oil and precipitated oil.

The high boiling point oil generated in the first cooling step (S30) is a mixture of oil components with different specific gravity. When left for a certain period of time, it is divided into superior oil with a relatively low specific gravity and precipitated oil with a relatively high specific gravity. separated.

In this step, using this principle, the high boiling point oil generated in the first cooling step (S30) is left in the separation device 140 for a predetermined time to separate it into supernatant oil and precipitated oil, and then the supernatant oil and precipitated oil are separated. Dispose of each separately.

Specifically, after the high boiling point oil generated in the first cooling step (S30) is input into the separation device 140, after a predetermined time has elapsed, it is separated into supernatant oil and precipitated oil. The upper oil and settled oil separated in this way can be separately discharged through the upper oil outlet provided on the upper side of the separation device 140 and the settled oil outlet provided on the lower side of the separation device 140, where they can be discharged. The precipitated oil may be returned to the pyrolysis step (S20) and thermal decomposition may be performed again.

The upper oil outlet may be an overflow pipe without a separate valve. In this case, if the upper oil separated in the separation device 140 is located higher than the height of the upper oil outlet, it overflows and is automatically discharged to the upper oil outlet without a transfer pump. At this time, if necessary, a valve may be provided at the upper oil outlet.

The upper oil discharged from the upper oil discharge port may be stored in the storage tank 160 as reclaimed oil according to the reclaimed oil storage step (S60), which will be described later.

The settled oil outlet is provided on the lower side of the separation device 140, and can discharge the settled oil that has settled in the lower part of the separation device 140 due to the difference in specific gravity. A transfer pump is provided at the settled oil outlet, so that the settled oil can be returned to the stirred continuous reactor 120 where the pyrolysis step (S20) is performed.

Discharging the settled oil measures the pressure within the separation device 140, determines the level of the settled oil according to the differential pressure with the standard pressure, and opens the settled oil discharge pipe when the level of the settled oil is judged to be above a predetermined level. Thus, the precipitated oil can be recovered in the stirred continuous reactor (120).

At this time, the settled oil discharge port may be formed as one, or may be formed as a plurality of two or more. When a plurality of settled oil outlets are formed, each settled oil outlet is formed to have a different height, so that the opened settled oil outlets may be operated differently depending on the level of the settled oil.

For example, when the level of the settled oil is low, only the settled oil outlet located at the bottom may be operated to be opened, and when the level of the settled oil is high, the settled oil outlet located at the top may be operated to be opened. This is an example of an operation method, and the operation method of the settled oil outlet is not limited to this.

Preferably, between the first cooling step (S30) and the high boiling point oil separation step (S40), a device is used to primarily separate the high boiling point oil generated in the first cooling step (S30) into supernatant oil and precipitated oil. A buffering step (S31) may be performed.

The buffering step (S31) is performed as needed, and the buffering step (S31) can be performed by leaving the high boiling point oil generated in the first cooling step (S30) in the buffer tank 131 for a predetermined period of time.

When going through the buffering step (S31), the supernatant oil and the precipitated oil may be initially separated and then inputted into the separation device 140 where the high boiling point oil separation step (S40) is performed. Therefore, the high boiling point oil present in a mixed state of the supernatant oil and the precipitated oil obtained in the first cooling step (S30) is not directly introduced into the separation device 140, so that the precipitated oil is contained in the supernatant oil in the separation device 140. Since mixing can be prevented, separation of supernatant oil and precipitated oil in the separation device 140 can be performed more effectively.

The secondary cooling step (S50) is a step of separating the non-condensed gas into condensed oil and non-condensed gas by cooling and condensing the uncondensed gas that is not cooled in the first cooling step (S30) and exists in gaseous form.

At this stage, components with relatively high boiling points are condensed to form liquid condensed oil, and components with relatively low boiling points are not condensed and remain in a gaseous state. Here, the high or low boiling point is determined based on the cooling temperature of the condensation tank 150 where the secondary cooling step (S50) is performed.

Cooling in the condensation tank 150 may be accomplished by condensing, and a refrigerant pipe containing the refrigerant may be provided at least either outside or inside the condensation tank 150.

The condensation tank 150 may be formed singly, or may be provided in two or more units and installed in series. In this case, primary condensation takes place in the condensation tank 150 located at the front, secondary condensation takes place in the condensation tank 150 located at the rear, and then non-condensed gas and condensation occur in the condensation tank 150 at the rear. It can be separated and discharged as oil.

The condensed oil condensed in this step is transferred to the storage tank 160 in the regeneration oil storage step (S60), which will be described later.

Additionally, non-condensable gas can be used as a heat source for equipment requiring a heating means in the reclaimed oil production process according to an embodiment of the present invention.

Non-condensed gas can be burned and used as a heat source to directly apply heat to equipment requiring a heating means, or a circulating heat medium can be heated to indirectly heat the equipment by the heat medium.

The part marked with a dotted line in FIG. 2 means that the non-condensable gas is not directly supplied as a raw material to the device, but is used as a heating source.

More preferably, the non-condensable gas is compressed through the gas compressor 170, stored in the compressed gas storage tank 180, and the compressed gas supplied from the compressed gas storage tank 180 is used as fuel to require a heating means. Heat can be supplied to equipment.

Non-condensable gas is produced by decomposition of waste vinyl raw materials and is not produced at the beginning of process operation. Therefore, when stored and used in the form of compressed gas, the stored compressed gas can be used immediately when the process is stopped and restarted, thereby improving overall process operation stability.

Compressed gas supplied from the compressed gas storage tank 180 can be used as fuel to heat the stirred continuous reactor 120 in which the thermal decomposition step (S20) is performed.

In addition, it can be used as fuel to heat the heat medium used as a heat source for the first screw preheating facility 111 and the second screw preheating facility 112 in which the pretreatment step (S10) is performed.

Additionally, it can be used as fuel to heat the distillation tower 200 and the reboiler, which will be described later.

The reclaimed oil storage step (S60) is a step of storing the supernatant oil separated in the high boiling point oil separation step (S40) and the condensed oil separated in the secondary cooling step (S50) in the storage tank 160.

The supernatant oil and condensed oil stored in the storage tank 160 are light oils and form reclaimed oil, which is a product of the reclaimed oil production process using the continuous waste vinyl pyrolysis device according to this embodiment. That is, the regenerated oil, which is the final product in the present invention, is a mixture of supernatant oil and condensed oil.

Here, a portion of the recycled oil stored in the storage tank 160 is transferred to the quench tank 130 where the primary cooling step (S30) is performed and sprayed, thereby performing primary cooling in the primary cooling step (S30). .

Additionally, the remaining part of the recycled oil may be supplied to the distillation tower 200 and separated into low boiling oil, medium boiling oil, and high boiling oil. A reduced-pressure distillation column may be preferably used as the distillation column 200, and in this case, energy efficiency can be improved by a boiling point lowering phenomenon.

FIG. 8 is a schematic view of the distillation tower 200. When described in detail with reference to FIG. 7, through the distillation step (S70) of distilling the recycled oil generated in the recycled oil storage step (S60), the recycled oil has a boiling point. It can be divided into low boiling point with a boiling point of 200°C or lower, medium boiling point with a boiling point ranging between 200 and 380°C, and high boiling point with a boiling point of 380°C or higher.

Low-boiling oil with a boiling point of 200℃ or lower contains naphtha and can be used as a naphtha raw material, while high-boiling oil with a boiling point of 380℃ or higher can be used as general fuel. In addition, heavy fuel oil with a boiling point ranging between 200 and 380 degrees Celsius can be used as diesel for power generation.

After the recycled oil is heated in the distillation step (S70), it may be introduced into the distillation tower 200, or may be introduced into the distillation tower 200 and heated, and may be separated in the distillation tower 200 according to its boiling point.

A condenser 210 is connected to the top of the distillation tower 200, and the gas components at the top of the distillation tower 200 are cooled to about 200°C to recover the condensed low boiling point oil, and the uncondensed gas components are returned to the distillation tower 200. Reflux.

A reheater 220 is connected to the lower part of the distillation tower 200, and reheats the regenerated oil in the lower part of the distillation tower 200. The high boiling point oil, which is a liquid component, is recovered, and the gas component is refluxed to the distillation column 200. At this time, in order to prevent a change in the temperature of the distillation tower 200 due to the temperature of the gas component refluxed from the reboiler 220 to the distillation tower 200, the internal temperature of the reboiler 220 is preferably maintained at 320 to 350 ° C. do.

In addition, a medium boiling point having a boiling point in the range of 200 to 380° C. can be obtained through an outlet provided in the center of the distillation tower 200.

The heavy density obtained in this way is high-quality diesel and can be used for power generation. More preferably, various conventional additives are further added to improve the combustion efficiency of diesel fuel, reduce the generation of exhaust gases, and prevent the generation of residues adhering to the generator engine, so that it can be used as diesel fuel for power generation.

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: Jacket 11: Outer barrel
12: diaphragm 13: side wall
15: Chlorine discharge port 17: Discharge port
20: screw 21: inner cylinder
31: lower connector 32: upper connector
40: inner tube connector 43: vertical extension part
51: Jacket fixing mechanical seal 52: Inner cylinder connection mechanical seal
53: External cylinder connection mechanical seal 60: Coolant circulation device
61: Cooler 62: Coolant circulation line
70: Screw movable chain 80: Inner tube insert
81: Inner cylinder connection P1: Heat oil supply pump
P2: Motor 111: Primary screw preheating facility
112: Secondary screw preheating facility 120: Stirred continuous reactor
130: Quick cooling tank 131: Buffer tank
140: separation device 150: condensation tank
160: storage tank 170: gas compressor
180: Compressed gas storage tank 200: Distillation tower

Claims (9)

A pretreatment step (S10) of heating waste vinyl, which is a raw material, to remove moisture, volatile matter, and chlorine;
A pyrolysis step (S20) of thermally decomposing the pretreated raw material by heating it in a continuous reactor;
A first cooling step (S30) in which the pyrolyzed raw materials are cooled in a rapid cooling tank and separated into high boiling point oil and uncondensed gas;
A buffering step (S31) in which the high boiling point oil generated in the first cooling step (S30) is supplied to a buffer tank, allowed to stand for a predetermined time, and then supplied to a separation device;
A high boiling point oil separation step (S40) in which the high boiling point oil obtained through the buffering step (S31) is left in a separation device for a predetermined period of time to separate it into supernatant oil and precipitated oil;
A secondary cooling step (S50) of cooling the uncondensed gas obtained in the first cooling step (S30) in a condensation tank and separating it into condensed oil and non-condensed gas; and
A reclaimed oil storage step (S60) of collecting the supernatant oil produced in the high boiling point oil separation step (S40) and the condensed oil produced in the secondary cooling step in a storage tank to generate reclaimed oil is performed continuously,
The pretreatment step (S10) is a first pretreatment step (S11) in which the raw material is supplied to the primary screw preheating equipment and heated to 250-300°C; and the raw material that has passed the first pretreatment step is supplied to the secondary screw preheating equipment. A second pretreatment step (S12) of heating to 300-330°C;
The primary screw preheating facility and the secondary screw preheating facility include an exhaust port through which moisture, volatile matter, and chlorine generated from waste vinyl, which is a raw material, are discharged,
The precipitated oil obtained in the high boiling point oil separation step (S40) is returned to a continuous reactor where the pyrolysis step is performed,
Using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility, characterized in that a part of the reclaimed oil obtained in the reclaimed oil storage step (S60) is transferred to a quenching tank where the first cooling step (S30) is performed and sprayed. Renewable oil production method.
delete delete According to paragraph 1,
The non-condensed gas obtained in the secondary cooling step (S50) is a continuous waste gas equipped with a screw preheating facility, characterized in that it is used as a heat source in at least one of the pretreatment step (S10) and the pyrolysis step (S20). Method for producing recycled oil using a vinyl pyrolysis device
delete delete According to paragraph 1,
The recycled oil is supplied to a distillation column and separated into low boiling point, medium boiling point and high boiling point. A method of producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility.
In clause 7,
A method of producing recycled oil using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility, wherein the non-condensed gas obtained in the secondary cooling step (S50) is used as fuel for heating the distillation tower.
According to paragraph 1,
Before the pretreatment step (S10), a raw material preparation step (S00) of removing non-combustible materials charged together with the waste vinyl as a raw material and molding the waste vinyl as a raw material into a predetermined size. Recycled oil production method using a continuous waste vinyl pyrolysis device equipped with a screw preheating facility

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