KR20230099776A - continuous operation equation pyrolysis emulsifier - Google Patents

Abstract

The present invention continuously puts combustible waste (vinyl, waste synthetic resin, etc.) selected from a landfill into a pyrolysis furnace for thermal decomposition, and continuously collects and purifies the pyrolyzed pyrolysis gas and carbonized by-products in a gas difference separator to separate and discharge them, More specifically, a multi-stage disk dust collector or high-temperature filter that passes the pyrolysis gas and carbonized by-products (soil, tea, non-combustible foreign matter, etc.) discharged by continuously pyrolyzing combustible waste in a pyrolysis furnace through a perforated disk dust collection plate formed in multiple stages in a gas difference separator High-concentration gas is separated from the distillation device to produce oil and gas with high-purity pyrolysis gas purified in the distillation device, and carbonized by-products that are not purified and collected in the gas difference separator are discharged and formed into pellets or briquettes in the molding machine to be recycled as resources. It relates to a gas differential separator connected to a thermal shunt for continuously pyrolyzing combustible waste to enable
The configuration according to the present invention includes a raw material input unit 100 for inputting flammable waste;
a raw material compression unit 200 for compressing and transferring combustible waste from the raw material input unit 100;
a pyrolysis furnace 300 for thermally decomposing and transporting the combustible waste compressed in the raw material compression unit 200;
a condensing unit 400 condensing the gas discharged from the pyrolysis furnace 300;
It is configured to include a distillation unit 500 for generating gas and oil by distilling the gas condensed and discharged in the condensation unit 400,
A gas difference separator 600 for receiving and separating the carbonized by-products mixed with the gas decomposed in the pyrolysis furnace 300 is connected between the pyrolysis furnace 300 and the condensation unit 400 to form,
The gas difference separator 600,
A dust collection hopper 611 having a conical lower part to store and discharge carbonized by-products;
A main body 610 having a gas outlet 612 formed on the top of the dust collecting hopper 611 to discharge the separated gas by collecting the dust;
The inside of the main body 610 includes a multi-stage disk dust collector 630 that collects and separates only the gas thermally decomposed in the pyrolysis furnace and guides it to the top,
The multi-stage disk dust collector 630 is equipped with a plurality of perforated disk dust collectors 620 at intervals in multiple stages (3 to 7 stages), and the center of the perforated disk collector 620 receives power from the motor 640 to rotate. A rotating shaft 650 is mounted, and the rotating shaft 650 is in contact with the upper and lower surfaces of the perforated disc collecting plate 620 while rotating to remove the fine powder of the carbonized by-products in contact with the perforated disc collecting plate 620 Rotating cleaner 660 It is characterized in that it is configured by mounting.

Description

Continuous operation type pyrolysis emulsifier {continuous operation equation pyrolysis emulsifier}

In order to pyrolyze combustible waste (vinyl, waste synthetic resin, etc.) discharged from daily life, the present invention continuously puts the pyrolyzed pyrolysis gas and carbonized by-products into a gas differential separator by continuously putting them into a pyrolysis furnace that blocks the contact between oxygen and air. It is for producing oil and gas by continuously collecting and purifying gas and carbonization by-products to separate and discharge them after pyrolysis in the input process. The pyrolysis gas and carbonized by-products (soil, tea, incombustible materials, etc.) discharged from pyrolysis are continuously supplied to the gas difference separator through the protruding guide part formed inside the pyrolysis furnace and the discharge screw of the transfer screw discharge pipe, The high-purity pyrolysis gas purified by separating the high-concentration gas through the high-temperature filter of the multi-stage disk dust collector or carbonized by-products passing through the multi-stage perforated disk collection plate formed inside the separation device passes through the distillation unit to generate oil and gas, and gas difference separation The carbonized by-products purified and collected in the device are collected in the hopper at the bottom and passed through a molding machine in a dough state by adjusting the humidity when discharged, and formed into pellets or briquettes and discharged to produce high-quality light oil, kerosene, gas, etc. , It relates to a continuous operation type pyrolysis emulsification device to enable recycling of resources without generation of wastewater and dust.

Since landfilling of combustible wastes, including disposable items that are generally used and discarded by people, causes serious environmental pollution, technologies for processing and recycling combustible wastes as resources are being actively researched. Recycling technologies for combustible waste include energy recycling, raw material recycling, and chemical recycling.

Energy recycling of combustible waste uses thermal energy obtained by incineration. However, when combustible waste is incinerated, dioxin and furan-based substances are inevitably created that are harmful to the environment and human body. There is a disadvantage that a lot of cost is required for investment and operation of the facility. Therefore, for combustible waste, raw material recycling and chemical recycling are given priority over energy recycling.

Raw material recycling of combustible waste classifies the combustible waste itself and uses it as a raw material for plastic products. In order to recycle raw materials of combustible waste, it is necessary to classify combustible waste by type, but due to many difficulties involved in classifying incompatible or wet combustible waste, problems of low workability and economic efficiency are involved.

In addition, chemical recycling is to obtain organic gas and oil that can be used as raw materials from combustible waste, and organic gas generated by thermally decomposing such combustible waste at a low temperature (300 ~ 600 ℃) of an oxygen-free type and cooling it to convert it into oil It is a low-temperature pyrolysis device for combustible waste. Existing emulsification equipment is classified into a batch type of batch type and a continuous type using a heating screw. The batch-type batch type has low facility costs, but since the operation and cooling discharge must be repeated once, there is a serious waste of heating energy and low productivity due to lack of process continuity. The screw continuous type requires technical sophistication of machinery It has a problem of low business feasibility due to the high facility cost of machinery and low throughput.

The low-temperature pyrolysis and emulsification device for combustible waste to solve these problems is a continuous batch type using a melt extruder, and is composed of a sorter, a grinder, a melt extruder, a main reactor, an auxiliary reactor, a gas separation tower, and a condenser. However, the melting extruder of the emulsifying device cannot block the contact between oxygen and air, and it consumes a lot of energy to heat the pulverized combustible waste at room temperature to the heating temperature for melting, which increases the cost of organic gas and oil production. There were high problems.

In addition, the discharge of steam generated when heating and melting combustible waste is not smooth, resulting in a decrease in the quality of organic gas and oil produced, and a coking phenomenon due to abnormal discharge from an explosive reactor, causing There was a problem in that the volume of the carbonized sludge was accumulated and clogged frequently in the discharge valve due to the decrease in the volume of the coking phenomenon and the negligence of minor management such as temperature check and time by the operator. In addition, since the raw material amount of the semi-fluid melt flowing into the auxiliary reactor cannot be accurately measured, the decomposition rate according to the continuous process cannot be managed, so that the entire production process is not performed smoothly.

On the other hand, among generators that produce electricity, gas turbine generators are generators that generate electricity by operating a turbine with high-temperature, high-pressure combustion gas, compressing air with a compressor, transporting the compressed air to a combustion chamber, and burning the injected fuel. The generated high-temperature, high-pressure combustion gas is emitted while the turbine is rotated to generate electricity. However, gas turbines have a problem in that maintenance costs are high due to high fuel consumption.

Therefore, there is a need to develop a system capable of more efficiently processing general solid fuel products including such combustible waste.

In addition, the pyrolysis device produces oil and gas by directly transferring the pyrolyzed gas decomposed in the pyrolysis furnace to the heat exchanger, but foreign substances (including fine carbonization by-products) mixed with the pyrolysis gas are transferred as they are, resulting in high-quality oil. There is a problem that gas cannot be obtained.

In addition, Patent Registration No. 10-1762092 disclosed as a dust collection technology, "low-temperature decomposition and incineration device for combustible waste using magnetized air" is a dust collector connected to a heat exchanger that exchanges heat generated from incinerated combustible waste, and only dust and dust It is a separation technique. Therefore, a technique for collecting and separately discharging gas and carbonized by-products obtained by thermally decomposing combustible waste is disclosed.

In addition, Utility Model Registration No. 20-0207679 "integrated facility of plasma reactor for harmful gas treatment and electric precipitator for removing by-products" is an integrated installation of a plasma reactor and an electric precipitator for removing by-products to remove harmful gases. The above configuration also discloses a technology for collecting and separating carbonized by-products mixed with gas obtained by pyrolyzing combustible waste.

In addition, "Electric precipitator using carbon fiber" of Patent Registration No. 10-1032617 is an electric precipitator for treating contaminated air. The electrostatic precipitator is a technology with a risk of explosion due to gas sparks, A technique for collecting and separately discharging mixed carbonized by-products is disclosed.

Republic of Korea Patent No. 10-1861753 Republic of Korea Patent No. 10-1762092 Republic of Korea Utility Model Registration No. 20-0207679 Republic of Korea Patent Registration No. 10-1032617

The present invention was created to supplement the above problems and the disclosed technology, and an object of the present invention is to continuously compress and input combustible waste into a pyrolysis furnace in a closed state to block oxygen and air, In addition, by supplying gas, carbonized by-products (window: char) and foreign substances continuously discharged from thermal decomposition in the pyrolysis furnace to the gas difference separation device (single or multiple), passing through the perforated disk dust collection plate installed in multiple stages on the upper side of the inside of the gas difference separation device The pyrolysis gas discharged after being collected and purified at a high concentration in the multi-stage disk dust collector or high-temperature filter passes through the condensation unit and the distillation unit to produce gas and oil, and at the same time, carbonized by-products that cannot be separated from the multi-stage disk dust collector or high-temperature filter are separated from the gas difference separator. When it is stored in the lower dust collection hopper and kneaded by adjusting the humidity through the supply storage silo and the powder transfer screw, and supplied to the mixing mixer and molding machine, it is formed into pellets or briquettes for the purpose of recycling resources as a heat source.

In addition, the present invention compresses and supplies combustible waste, which is crushed to a size of 100 mm to 1200 mm in the pretreatment process and introduced into the hopper of the input unit, into the primary compression space by the piston action of the compression plate formed in the raw material compression unit, and then supplied. The purpose is to secondarily compress combustible waste while blocking oxygen and air through an oxygen shutoff valve, and inject it into a pyrolysis furnace through an injection pipe so that it can be thermally decomposed.

In addition, it is an object of the present invention to separate only high-concentration gas by collecting the carbonized by-products on a perforated disk dust collecting plate formed in multiple stages, even if the fine powder of the carbonized by-products rises together with the gas through the multi-stage disk dust collector.

In addition, in the present invention, when the fine particles of the carbonized by-products transferred from the pyrolysis furnace to the gas difference separator and separated by the multi-stage disk dust collector do not fall freely and rise together with the gas and are collected on the perforated disk dust collector, the upper and lower surfaces of the perforated disk dust collector It is intended to be separated by a rotating rotary cleaner and collected and discharged by falling into a dust collection hopper formed at the bottom.

In addition, in another embodiment of the present invention, by using a high-temperature filter forming a filter dust collector to collect carbonized by-products and foreign substances mixed in the pyrolysis gas, only high-concentration gas can be separated and guided to the condensation unit and the distillation unit. It has a purpose.

In addition, according to the present invention, a multi-stage disk dust collector and a high-temperature filter dust collector may be used at the same time in order to produce high-concentration gas, if necessary.

A continuously movable pyrolysis and emulsification device for continuously pyrolyzing flammable waste according to an embodiment of the present invention to solve the above problems is

A raw material input unit 100 for inputting flammable waste;

a raw material compression unit 200 for compressing and transferring combustible waste from the raw material input unit 100;

a pyrolysis furnace 300 for thermally decomposing and transporting the combustible waste compressed in the raw material compression unit 200;

a condensing unit 400 condensing the gas discharged from the pyrolysis furnace 300;

It is configured to include a distillation unit 500 for generating gas and oil by distilling the gas condensed and discharged in the condensation unit 400,

A gas difference separator 600 for receiving and separating the carbonized by-products mixed with the gas decomposed in the pyrolysis furnace 300 is connected between the pyrolysis furnace 300 and the condensation unit 400 to form,

The gas difference separator 600,

A dust collection hopper 611 having a conical lower part to store and discharge carbonized by-products;

A main body 610 having a gas outlet 612 formed on the top of the dust collecting hopper 611 to discharge the separated gas by collecting the dust;

The inside of the main body 610 includes a multi-stage disk dust collector 630 that collects and separates only the gas thermally decomposed in the pyrolysis furnace and guides it to the top,

The multi-stage disk dust collector 630 is equipped with a plurality of perforated disk dust collectors 620 at intervals in multiple stages (3 to 7 stages), and the center of the perforated disk collector 620 receives power from the motor 640 to rotate. A rotating shaft 650 is mounted, and the rotating shaft 650 is in contact with the upper and lower surfaces of the perforated disc collecting plate 620 while rotating to remove the fine powder of the carbonized by-products in contact with the perforated disc collecting plate 620 Rotating cleaner 660 It is characterized in that it is configured by mounting.

In addition, in the present invention, the perforated disk dust collecting plate 620 is formed in a semicircular shape (1/2 circular shape) for convenient detachment and maintenance, and is fixed to all sides of the main body 610 to facilitate separation and coupling from the rotating shaft 650. It is characterized in that it is seated on the angle 624 mounted on the outer periphery of the fixing plate 623 and coupled using a fastener 625.

In addition, the present invention has a gas discharge hole 621 for collecting and separating only gas in the perforated disk dust collecting plate 620, and carbonized by-products mixed with gas by drilling a diameter 0.5 to 3 times larger than the gas discharge hole 621 It is characterized in that the carbonized fine powder discharge hole 622 for removing the fine powder of is made of a fan shape so as to cross diagonally to the perforated disk dust collecting plate 620.

In addition, in the present invention, the carbonized fine powder discharge hole 622 perforated in the perforated disk collecting plate 620 is not formed in a vertical state with the perforated disk collecting plate 620 formed at intervals in multiple stages, and the gas is vertical while going up to the upper side. It is characterized in that it is configured by arranging the perforated disk dust collecting plate 620 in a screw shape to inhibit discharge.

In addition, in the present invention, the diameter of the gas discharge hole 621 and the carbonized fine powder discharge hole 622 of the perforated disk dust collecting plate 620 is formed smaller by 1/2 to 1/3 toward the upper side to optimize the fine powder of the carbonized by-product. It is characterized in that it is configured to collect dust with.

In addition, the present invention is characterized in that the gas difference separator 600 is composed of a plurality of structures connecting one or more.

In addition, in the present invention, the pyrolysis furnace 300 is formed of a conical pyrolysis housing 320 at the front, so that carbonized by-products are introduced into the gas difference separation device 600 by the protruding guide part 340, or the pyrolysis furnace ( It is characterized in that the carbonized by-products dropped from the protrusion guide part 340 of 300) are configured to flow into the gas difference separator 600 through the discharge screw 344 of the transfer screw discharge pipe 343.

In addition, the configuration of the gas difference separator 600a of another embodiment according to the present invention is a high-temperature filter dust collector equipped with a high-temperature filter 710 to collect carbonized by-products and fine powder mixed with the gas discharged from the pyrolysis furnace 300 Forming 700,

In the high-temperature filter 710, a ceramic foam 711, a fibrous filter 712, and a particulate filter 713 are laminated inside a main body 714 formed vertically so that the plurality of main bodies 714 are closely attached to each other. It is characterized in that it is composed of.

In addition, in the present invention, the raw material input unit 100 sorts the combustible waste in the combustible waste sorter 2100, sorts the metal mixed in the sorted combustible waste with the magnetic separator 2200, and separates the sorted combustible waste It is characterized in that it is configured by connecting to the pre-processing device 2000 for crushing in the crusher 2300.

In addition, the present invention includes a chlorine removal device 550 for removing chlorine from the gas distilled and discharged from the distillation unit 500, a desulfurization device 560 for removing sulfur atoms or sulfur compounds, and a turbidity improving device for improving turbidity. It is characterized in that it is configured to store the separated gas in the gas tank 800 by connecting the 570 and the fine inspection device 580 for separating the fine dust.

The gas differential separator connected to the pyrolysis furnace for continuously pyrolyzing combustible waste of the present invention according to the configuration described above is supplied to the pyrolysis furnace in a compressed state by blocking oxygen or air, and carbonization that is continuously discharged by thermal decomposition High-purity gas and oil can be produced by enabling dust collection and purification through the gas discharge hole of the multi-stage perforated disk dust collector formed on the upper side of the multi-stage disk dust collector forming the gas difference separator for collecting and separating by-products and gas. There is an effect.

In addition, according to the present invention, the combustible waste injected into the input unit is firstly compressed by the rotary compression plate of the raw material input unit and introduced into the compression space of the raw material compression unit, and the combustible waste injected into the compression space is secondarily compressed by the piston action. It is transported through the oxygen cutoff valve to the front input pipe, and at the same time, liquid oil is sprayed from the oxygen cutoff nozzle to block external air, so that combustible waste flowing into the pyrolysis furnace can be completely burned and thermally decomposed.

In addition, in the present invention, the carbonized by-products and fine particles that are not purified by gas in the multi-stage disk dust collector and are attached to the upper and lower portions of the perforated disk dust collector, respectively, are separated by a rotary cleaner and fall into the carbonized fine powder discharge hole to be converted into briquettes or pellets. It has the effect of recycling resources as a heat source by molding.

In addition, as another embodiment of the present invention, there is an effect of obtaining only high-purity gas by separating and purifying the gas and carbonization by-products continuously discharged from the pyrolysis furnace through the high-temperature filter of the high-temperature filter dust collector.

1 is a front view showing the overall configuration of a continuously movable pyrolysis and emulsification apparatus of the present invention.
2 is a cross-sectional view showing a pyrolysis furnace of the present invention.
3 is a perspective view and a cross-sectional view showing a plurality of gas difference separation devices connected to the pyrolysis furnace of the present invention.
4 is a plan view showing a perforated disc dust collecting plate of the gas difference separator of the present invention.
5 is a side view illustrating a process of compressing carbonized by-products discharged from the gas difference separator of the present invention and transporting them to pyrolysis.
6 is a perspective view, a front cross-sectional view, and a side cross-sectional view in which a gas difference separator of the present invention is formed in a singular structure and partially developed.
7 is a perspective view showing a gas difference separator according to another embodiment of the present invention.
8 to 10 are perspective views showing a raw material inlet and a raw material compression unit according to the present invention.
11 is a partially enlarged view of the injection pipe of the present invention
12 is a front view showing an oil-water separator connected to the distillation tower of the present invention.
13 is a front view showing the vacuum distillation unit of the present invention.
14 is a front view showing the condenser of the present invention.
15 is a front view showing an absorption chiller of the present invention.

Hereinafter, the technical idea of the present invention will be described in more detail using the accompanying drawings. Prior to this, the terms or words used in this specification and claims should not be construed as being limited to the usual or dictionary meaning, and the inventor appropriately uses the concept of the term in order to explain his/her invention in the best way. It should be interpreted as a meaning and concept consistent with the technical idea of the present invention based on the principle that it can be defined.

Hereinafter, the specific configuration and characteristics of the thermal decomposition principle of the continuously movable thermal decomposition and emulsification apparatus 1000 of the present invention formed as a whole with reference to FIG. 1 will be described.

The continuously movable pyrolysis and emulsification apparatus 1000 of the present invention includes a raw material input unit 100 for inputting combustible waste, a raw material compression unit 200 for compressing the combustible waste discharged from the raw material input unit 100, and the raw material A pyrolysis furnace 300 for pyrolyzing the combustible waste compressed and supplied by the compression unit 200, connected to the pyrolysis furnace 300 to discharge raw materials to the outside of the pyrolysis furnace 300, and decomposed raw materials with gas A gas difference separator 600 for separating into carbonized by-products, a condensation unit 400 for condensing the gas separated in the gas difference separator 600, a distillation unit 500 for separating gas, oil and water, the distillation unit A gas tank 800 for storing the gas separated in 500 may be included.

Each of the above configurations will be described in more detail with reference to the drawings.

As shown in FIG. 2, the pyrolysis furnace 300 has a raw material inlet 330 for receiving raw materials on one side, a raw material outlet 310 having a conical front so as to discharge raw materials on the other side, and an inside for pyrolyzing the raw materials. A space may be formed, and a pyrolysis housing 320 may be rotated to pyrolyze the raw material. In addition, the raw material outlet 310 formed in a conical shape is combined with the connection bearing 670 of the gas difference separator 600 to be described later, and the pyrolysis housing 320 is seated on the lower rollers 370 and 371 to rotate. done smoothly Therefore, the pyrolyzed carbonized by-products flow into the discharge screw 344 of the transfer screw discharge pipe 343 by the rotation of the pyrolysis furnace 300, are discharged through the front raw material discharge port 310, and flow into the gas difference separator 600. Let it be.

The thermal decomposition furnace 300 applies constant heat to the thermal decomposition housing 320 and rotates the thermal decomposition housing 320 at a constant speed so that the thermal decomposition of the combustible raw material can be sufficiently performed automatically inside the thermal decomposition furnace 300. In more detail, the pyrolysis housing 320 may include a structure of a protruding guide 340 having a spiral protruding live line 341 and a straight protruding line 342 that allows the raw material to move from one side to the other as time passes inside the pyrolysis housing 320. there is.

Accordingly, the raw material is introduced into the pyrolysis housing 320 through the raw material input port 330 formed on one side of the pyrolysis housing 320, and then thermally decomposed for a predetermined time inside the pyrolysis housing 320, and the protruding guide part ( While moving from one side to the other side by 340), it is received into the gas difference separator 600 through the raw material discharge port 310 formed on the other side of the pyrolysis housing 320.

The thermal decomposition furnace 300 may further include a heating unit 360 to apply heat to the outside of the thermal decomposition housing 320 . In more detail, the heating unit 360 may be a nozzle for discharging hot gas to the outer surface of the pyrolysis housing 320 . While the pyrolysis housing 320 rotates, heat from the heating unit 360 can be evenly transferred to the entire side surface of the pyrolysis housing 320 .

Therefore, it is possible to automatically receive decomposed carbonization by-products (Char) and gas through the raw material outlet 310, like the principle of discharging ready-mixed concrete. At this time, the raw material outlet 310 preferably includes a structure capable of moving the raw material without user intervention in receiving carbonized (solid) by-products and gas.

And, as shown in FIG. 2, since the raw material outlet 310 of the pyrolysis furnace 300 is directly inserted into the gas difference separator 600, the pyrolyzed gas and carbonized by-products are automatically removed from the gas difference separator 600. ) will be received into the interior of

As described above, when the pyrolysis of combustible waste is performed, it can be operated automatically for a long time by adjusting the constant speed of the pyrolysis housing 320 without the need for separate parts separation, thereby increasing the pyrolysis efficiency and the pyrolysis furnace 300 ) can maximize the energy use efficiency and extend the life of each facility.

Hereinafter, the configuration and characteristics of the pyrolysis furnace 300 of the present invention will be described in more detail with reference to FIG. 2 .

As described above, the pyrolysis furnace 300 has a raw material inlet 330 for receiving raw materials on one side, a raw material outlet 310 formed in a conical shape to discharge raw materials at the end side of the other surface, and an internal space for thermally decomposing the raw materials This is formed, and is formed as a pyrolysis housing 320 that is supported by rollers 370 and 371 on the lower side and pyrolyzes raw materials while rotating. And the inner surface of the pyrolysis housing 320 may further include a protruding guide portion 340 for guiding the movement of the raw material forward. By including the protruding guide portion 340, the raw material inside the pyrolysis housing 320 can be induced to gradually move through the raw material outlet 310 on the other side from one side, like the discharge principle of ready-mixed concrete, gradually over time.

More specifically, the protrusion guide portion 340 may be one or more spiral protruding live lines 341 formed on the inner surface of the pyrolysis housing 320 . The raw material before pyrolysis is in a compressed solid state, and when the raw material is introduced into the pyrolysis housing 320 through the raw material inlet 330, it is biased on the inner side of the pyrolysis housing 320 by its weight. , At this time, it is possible to move to the other side (forward) while rotating the raw material biased on one side by the rotation of the spiral protruding active line 341 formed on the inner surface of the pyrolysis housing 320.

In addition, the protrusion guide portion 340 may be two or more straight protrusions 342 formed on the inner surface of the pyrolysis housing 320 and spaced apart from each other at regular intervals in a predetermined angular direction so as to form a spiral. Since the linear protrusion 342 is formed, the raw material may rotate and move from one side to the other side. In addition, even when the raw material is located on the upper inner surface of the pyrolysis housing 320 (since the pyrolysis housing 320 continuously rotates), the multi-stage linear protrusion 342 prevents the raw material from falling from the top to the bottom by gravity can be prevented, and thus the thermal decomposition efficiency of the raw material can be increased.

The linear protrusion 342 and the spiral protrusion live line 341 may be selected and formed according to the purpose, and both may be applied as shown in FIG. 2 . Carbonized by-products that have been pyrolyzed and transported forward by the protruding guide part 340 as described above are received into the gas difference separator 600 to be described later through the discharge screw 344 of the transfer screw discharge pipe 343.

The above-described protruding guide portion 340 is preferably made of the same material as the pyrolysis housing 320, and is preferably made of a material having heat resistance so as to withstand a high-temperature pyrolysis environment.

As the protruding guide part 340 is applied, the decomposed carbonization byproduct (Char) is stacked on the lower part of the other side of the pyrolysis housing 320, and the decomposed gas floats on the upper part, so that the separation process can be facilitated.

In addition, the pyrolysis housing 320 may include an inspection port 350 including a pressure gauge and a thermometer. At least one inspection port 350 may be installed, and is preferably formed on at least one surface of the pyrolysis housing 320 . Through the inspection opening 350, the user can check the state of the inside of the pyrolysis housing 320. The inspection port 350 is preferably located at the top or bottom of the pyrolysis housing 320 in more detail, and is spaced at a predetermined interval in the direction of the rotation axis of the pyrolysis housing 320 from the outermost surface of one side or the other side of the rotation axis of the pyrolysis housing 320. It is preferable to form in the position where it is. Accordingly, even if the inspection port 350 is opened while the pyrolysis raw material remains inside the pyrolysis housing 320, the raw material may not flow out through the inspection port 350.

In addition, it is preferable that a lid that can be opened and closed is coupled to an end of the inspection port 350, and the lid is completely closed during operation of the pyrolysis furnace 300 to block the inside and outside of the pyrolysis housing 320.

Hereinafter, the configuration and characteristics of the gas difference separator 600 of the present invention will be described with reference to FIGS. 3 to 6 .

As described above, the raw material outlet 310 of the pyrolysis housing 320 is seated on the connection bearing 670 and connected to one side of the gas difference separation device 600. The other side of the gas difference separator 600 is connected to the condensing unit 400 for condensing gas. And the gas difference separator 600 has a gas outlet 612 formed on the upper side, a multi-stage disk dust collector 630 is installed inside, and a dust collection hopper 611 for collecting and discharging carbonized by-products and carbonized fine powder at the lower part Is made of a body 610 is formed.

In addition, as shown in FIGS. 3 and 4, it is formed in multiple stages (3 to 7 stages or more) at intervals to collect and filter gas through the multi-stage disk dust collector 630 formed on the upper side of the main body 610. The perforated disk dust collecting plate 620 and the rotary cleaner 660 are spaced apart from the rotary shaft 650 that is connected to the motor 640 and rotates in order to detach the carbonized fine dust collected and attached to the perforated disk dust collecting plate 620. Many are formed. At this time, the rotary cleaner 660 is configured to closely adhere to the upper and lower portions of the perforated disk dust collecting plate 620 formed at intervals in multiple stages, respectively.

And as shown in (a) of Figure 4, the perforated disk dust collection plate 620 has a plurality of gas discharge holes 621 finely perforated by about 0.1 mm to 5 mm in order to collect carbonized fine powder, and also gas discharge The carbonized fine powder discharge hole 622 is fan-shaped to allow the carbonized fines attached to the perforated disk dust collecting plate 620 to be discharged to the lower part as the carbonized fines attached to the perforated disk dust collecting plate 620 are eliminated by drilling a diameter larger than that of the ball 621 by 2 to 10 times and 1.0 mm to 10 mm large. It is perforated to be symmetrical to each other with an area of about 1/6 of the furnace.

In addition, the carbonized fine powder discharge hole 622 perforated in the perforated disk collecting plate 620 is not formed in a vertical state in a straight line with the perforated disk collecting plate 620 formed in multiple stages, and can suppress vertical discharge of gas while going up to the upper side. It is configured by arranging them in a screw shape so that they are staggered with each other.

When the carbonized fine powder discharge hole 622 is formed in a straight vertical state, the carbonized fine powder mixed with the gas rises to the upper side without being purified and collected. It is preferable to install it as .

According to the configuration described above, the gas and carbonized by-products delivered to the gas difference separator 600 are easily separated and delivered without user intervention.

At this time, as shown in (b) of FIG. 4, the perforated disk dust collecting plate 620 is formed in a semicircular shape to facilitate separation and coupling from the rotating shaft 650, outside of the fixing plate 623 fixed to all sides of the main body 610. The angle 624 mounted on the periphery is coupled using a fastener 625.

In addition, as shown in (c) of FIG. 4, the diameters of the gas discharge hole 621 and the carbonized fine discharge hole 622 of the perforated disk dust collection plate 620 go toward the upper perforated disk dust collection plate 620. It is characterized in that it is formed in small portions by 1/2 to 1/3 to optimally collect the fine powder of carbonized by-products.

That is, the diameter of the gas discharge hole 621 drilled in the first perforated disk collecting plate 620 at the bottom is 10 mm, the diameter of the carbonization by-product discharge hole 622 is 15 mm, and the second hole is drilled in the first perforated disk collecting plate 620. The diameter of the gas discharge hole 621 is 7.5 mm, the diameter of the carbonization by-product discharge hole 622 is 10 mm, the diameter of the gas discharge hole 621 drilled in the third perforated disk dust collection plate 620 is 5.0 mm, the carbonization by-product The diameter of the discharge hole 622 is 7.5 mm, the diameter of the gas discharge hole 621 drilled in the fourth perforated disk dust collection plate 620 is 2.5 mm, the diameter of the carbonized by-product discharge hole 622 is 5.0 mm, and the fifth perforation The diameter of the gas discharge hole 621 drilled in the disk dust collecting plate 620 is 1.0 mm, and the diameter of the carbonization by-product discharge hole 622 is 2.5 mm.

In addition, as shown in (a) of FIG. 4, a perforated disk dust collecting plate 620 mounted on the fixing plate 623 at intervals in a multi-layer of 3 to 7 layers in the multi-stage disk dust collector 630 for collecting and filtering gas. ), and the rotary cleaner 660 for removing the carbonized fines attached to the perforated disk dust collecting plate 620, etc. In order to perform maintenance, cleaning or replacement, the perforated disk dust collecting plate 620 is manufactured in a semicircle to rotate the shaft 650 It is formed to be coupled to, and one side of the main body 610 is configured to include an inspection port 680.

In addition, at least one inspection hole 680 installed on one side of the main body 610 of the gas difference separation device 300 may be installed, and it is preferable to form at least one side of the gas difference separation device 600. Through the inspection opening 680, a user can inspect the state of the inside of the main body 610 of the gas difference separator 600. It is preferable that the inspection hole 680 be located at the top and side of the gas difference separator 600 in more detail.

In addition, it is preferable that an openable and openable lid is coupled to the end of the inspection port 680, and the lid is completely closed when the gas difference separator 600 is operated to block the inside and the outside.

And, as shown in FIG. 5, carbonized by-products discharged to the dust collection hopper 611 of the gas difference separator 600 are transported forward through the horizontal transfer screw 611a and dropped to the discharge transfer screw 690. The carbonized by-products transferred to the discharge transfer screw 690 are transferred to the supply storage silo 900 and stored.

The carbonized by-products stored in the carbonized by-product supply storage silo 900 cut off the supply of air and oxygen. Fine dust of dried carbonized by-products (char) by being supplied with compressed water through the compressed water supply nozzle 940 in the process of being discharged back to the lower discharge port and being transferred to the fine powder transfer screw 910 without generating fine powder of carbonized by-products ( Powder) and compressed water are mixed and transferred to the mixing mixer 920 for forming carbonized by-products.

At this time, the carbonized by-products transported through the fine powder feed screw 910 are removed by the compressed water supply nozzle 940 and at the same time compressed water is supplied to the outside of the fine powder feed screw 910 to maintain a kneaded state that is good for molding. A plurality of nozzles 940 may be connected, and the compressed water supply nozzle 940 pressurizes the fluid into the fine powder feed screw 910, thereby reducing the fine dust transported into the fine powder feed screw 910. It can be removed (kneaded with carbonized by-products) by a screw conveying movement, so that the recovery of carbonized by-products can be facilitated without generating fine dust. That is, the compressed water supply nozzle 940 may inject the fluid into the fine powder feed screw 910, and thus the fine dust transported into the fine powder feed screw 910 is carbonized by-product by the rotational movement of the screw. will be mixed with

In addition, a spray nozzle 922 for spraying fluid to the carbonized by-products stored in the mixing mixer 920 is formed on the upper side to supply fluid to the carbonized by-products transferred to the mixing mixer 920 to form the dough required for molding. Stirring is performed using the rotating body 921 for stirring so that the mixture can be mixed with a thin air.

And the carbonized by-products stirred in the mixing mixer 920 are discharged through the lower discharge port and introduced into the molding machine 930, and the carbonized by-products introduced into the inside are molded into pellets or briquettes by the piston 931 and discharged. will do Molded bodies such as briquettes of the discharged carbonized by-products are transferred to the outside through the transfer conveyor 960 and stored.

More specifically, the carbonized by-products transported through the pulverizing feed screw 910 are stored in the mixing mixer 920 to adjust the consistency of the dough required for molding, and to block external inflow air to promote smooth discharge. do.

In addition, at the lower side of the mixing mixer 920, a plurality of through-holes are perforated at the end side so that the carbonized by-products discharged by holding the fluid can be molded into a certain size such as briquettes by compression of the piston 931 and discharged. A molding machine 930 is installed.

Hereinafter, FIG. 6 shows another embodiment of the gas difference separator 600 according to the present invention, in which a multi-stage disk dust collector 630 mounted inside the main body 610 is installed in a plurality of two or more as in the above-described embodiment. It is not installed as a furnace, but a multi-stage disk dust collector 630 mounted inside the main body 610 can be installed and used as one single water tank.

The configuration of the gas difference separator 600 composed of the single water tank is the same as that of the above-described embodiment.

And, a gas difference separator according to another embodiment of the present invention will be described based on FIG. 7 as follows.

The gas difference separator 600a connected between the pyrolysis furnace 300 and the condensation unit 400 is equipped with a high-temperature filter 710 to collect carbonized by-products and fine particles mixed with the gas discharged from the pyrolysis furnace 300. A high-temperature filter dust collector 700 is formed.

In the high-temperature filter 710, a ceramic foam 711, a fibrous filter 712, and a particulate filter 713 are laminated inside a main body 714 formed vertically. In addition, a plurality of the main bodies 714 are mounted in close contact with each other to form the inside of the main body of the gas difference separator 600a.

In addition, another embodiment of the present invention, although not shown in the drawings, is connected between the pyrolysis furnace 300 and the condensing unit 400, and a gas difference separation device (not shown) includes a multi-stage disk dust collector 630 and a high-temperature filter It may be configured by combining the dust collector 700 in a stacked manner.

And with reference to Figures 8 to 9 will be described the configuration and characteristics of the raw material input unit 100 and the raw material compression unit 200 of the present invention.

The continuously movable pyrolysis and emulsification apparatus 1000 of the present invention may further include a raw material input unit 100 and a raw material compression unit 200. As shown in Figs. ) is opened by combining the hopper 110 at the top, and the rotary compression plate 120 is formed at the bottom to primarily compress the raw material injected into the hopper 110 to block external air while the raw material compression unit 200 ) It is preferable to be able to be injected into the compression space 210 of the.

In order to secondarily compress the raw material injected into the compression space 210, the compression plate 120 inserted into the compression space 210 and the piston 230 coupled to the side of the compression plate 120 can include

In addition, the compression plate 220 opens and closes the outlet 130 formed at the bottom of the hopper 140 while sliding left and right by the piston 230 . As described above, the raw material input unit 100 includes a hopper 110 for inputting combustible waste and a rotary compression tube 120 for compressing the combustible waste, so that combustible waste having various sizes and polygonal shapes such as squares or circles can be processed. can be easily received.

In addition, the raw material compression unit 200 is an opening and closing plate 221 having a long length toward the upper side of the compression plate 220 to open and close the outlet 130 of the raw material compression unit while compressing the combustible waste injected into the compression space 210 is formed Therefore, when the compression plate 220 moves horizontally, the outlet 130 formed at the bottom of the hopper 110 may be opened and closed.

The compression plate 210 preferably has the same size and shape as the cross-sectional area of the compression space 210, and the compression plate 220 starts from the side of the compression space 210 and extends to the inner front of the compression space 210. It is preferable to slide by the piston 230.

Therefore, when the raw material injected into the compression space 210 is instantly moved forward and compressed by the horizontal movement of the compression plate 220 in a forward and backward slide, it can be received by the raw material compression unit 200 while blocking oxygen and air.

Hereinafter, the configuration and characteristics of the raw material compression unit 200 of the present invention will be described with reference to FIG. 9 .

The continuously movable pyrolysis emulsification apparatus 1000 of the present invention may further include a raw material compression unit 200 between the raw material input unit 100 and the pyrolysis furnace 300. The raw material compression unit 200 is connected to one end of the raw material inlet 330 of the pyrolysis housing 320 and includes an input screw pipe 251 for inputting raw materials into the pyrolysis housing 320 and an input screw pipe 251. Combustible waste may be transferred to the pyrolysis furnace 300 by including an input transfer screw 250 inserted inside and the other end positioned inside the pyrolysis housing 320.

Furthermore, the raw material compression unit 200 may further include an oxygen blocking nozzle 252 that minimizes penetration of air particles between the combustible waste particles by injecting a fluid into the input pipe 240 and the input screw pipe 251. there is.

In the course of conveying the compressed combustible waste through the raw material compression unit 200, a space may be formed between the combustible wastes, and air, particularly a combustible gas such as oxygen, may permeate into this space. Since the inside of the pyrolysis furnace 300 maintains a very high temperature, a combustion reaction may occur when a combustible gas penetrates into the raw material. The oxygen blocking nozzle 252 minimizes this combustion reaction, and ), it is possible to maximize the thermal decomposition efficiency of the pyrolysis furnace 300 by increasing the density, watertightness, and lubricity of the combustible waste input.

At this time, the fluid sprayed from the oxygen blocking nozzle 252 may be water received from the external water tank 540, may be heavy oil distilled in the distillation unit 500 to be described later, or in the condensation unit 400 to be described later. It may be discharge water that is condensed and filtered in the oil-water separation unit 510 .

An action of compressing combustible waste by the piston 230 in the raw material compression unit 200 will be described in detail with reference to FIG. 9 .

As described above, the combustible waste injected into the hopper 110 of the raw material input unit 100 is primarily compressed by the rotary compression plate 120 and enters the compression space 210 of the raw material compression unit 200 through the outlet 130. flowed into

The combustible waste of the primary compression material introduced into the compression space 210 is subjected to secondary compression as the compression plate 210 is transported forward by the horizontal movement of the cylinder 230 . At this time, when the combustible waste is transported forward and subjected to secondary compression, the opening/closing plate 221 connected to the upper side of the compression plate 210 closes the outlet 130 of the raw material input unit 100, and at the same time, the primary compressed Inflow of combustible waste into the compression space 210 of the raw material input unit 200 is prevented.

As described above, when a predetermined amount of primary compressed combustible waste flows into the compression space 210, the compressed combustible waste is gradually compressed by the action of the piston 230 and formed in front of the compression space 210. It is laminated while being compressed in the form of a book in the injection pipe 240.

At this time, in order to prevent blocking of oxygen and air in the combustible waste that is secondarily compressed and transported to the front input pipe 240, the oxygen shutoff valve 260 is spaced between the compression space 210 and the input pipe 240. When two or more are formed, and the secondary compressed combustible waste moves to the inlet pipe 240, the oxygen shutoff valve 260 is first and second sequentially opened and transported to the inlet pipe 240, When the transfer to 240 is completed and the compression plate 210 moves backward by the action of the piston 230, the oxygen shutoff valve 260 is closed opposite to the opening. Therefore, after supplying the compressed water, the oxygen shutoff valve 260 is closed, thereby blocking the inflow of air.

That is, when the compression plate 230 transfers the combustible wastes that have been primarily compressed into the compression space 210 and transferred forward, they are sequentially compressed and stacked in a book shape. When the above operation is repeated, as shown, the combustible waste in steps 1, 2, 3, 4, and 5 is compressed secondarily and sequentially stacked, and also in the compression space 210, the compressed material is placed in the front 1, 2 , It is laminated in the form of a book in three stages. Therefore, when the compression action of the compression plate 230 is repeated, the combustible waste stacked in the form of a book in the compression space 210 is transported forward while serving as a compression plate, and compressed into a book form in the input pipe 240. The compressed combustible waste from the compressed combustible waste in the fifth step is sequentially transferred to the input transfer screw 250 mounted on the input screw pipe 251 and introduced into the pyrolysis furnace 300.

In addition, when the combustible waste is compressed and moved by the input pipe 240 and the input screw pipe 251, liquid flow is sprayed from the oxygen blocking nozzle 252 installed outside the input pipe 240 and the input screw pipe 251. Oxygen and air are blocked to facilitate the movement of the compressed combustible waste, and oxygen and air are prevented from being blocked in the thermal decomposition furnace 300, thereby increasing the efficiency of thermal decomposition.

10 according to the present invention is a perspective view showing another embodiment in which the raw material compression unit 200 has a circular or polygonal shape rather than the rectangular shape of the above-described embodiment.

In addition, as shown in FIG. 11, a thrust bearing 270 is inserted between the input screw pipe 251 and the raw material inlet 330, and the pyrolysis housing 320 rotates independently of the input screw pipe 251. It is desirable to do In more detail, it is preferable that the phase of the input screw pipe 251 is fixed, and the pyrolysis housing 320 is rotated independently of this. It is preferable that the input transfer screw 250 inserted into the input screw pipe 251 also rotates independently of the pyrolysis housing 320.

In addition, it is preferable that the heat insulating material 280 is inserted into the pipe between the input screw pipe 251 and the raw material input port 330. Accordingly, it is possible to prevent heat applied to the pyrolysis housing 320 from being transferred to the input transfer screw pipe 251 and further to the gas difference separator 600, and the lifespan of the equipment can be increased.

The heat insulating material 280 is to block heat generated in the pyrolysis furnace 300 from being transferred to the raw material compression unit 200 .

Hereinafter, the configuration and characteristics of the distillation unit 500 of the present invention will be described with reference to FIGS. 12 and 13 .

The continuously movable pyrolysis emulsification apparatus 1000 of the present invention may further include a distillation unit 500 and a gas tank 800. As shown in FIG. 12, the distillation unit 500 may include an oil and water separation unit 510 for separating oil and water. As shown in FIG. 13, the oil gas separated from the oil and water separation unit 510 It may include a distillation tower 520 receiving the distillation tower 520, a vacuum distillation unit 530 receiving and distilling oil gas from the distillation tower 520, and a water tank 540 supplying cooling water to the vacuum distillation unit 530.

The oil/water separation unit 510 shown in FIG. 12 may receive gas from the condensing unit 400 to be described later and separate moisture from the gas discharged through the gas distillation tube 440. The gas distillation pipe 440 may be formed of a triple pipe of a gas discharge pipe 441, a water discharge pipe 442, and a cooling water pipe 430.

The gas discharge pipe 441 discharges and separates the gas condensed in the condensing part 400 to the first separation part 511, and the drain pipe 442 flows into the condensing part 400 through the cooling water pipe 430. The drained water is discharged to the second separator 512 to be separated, and the cooling water pipe 530 supplies the cooling water in the water tank 540 to the cooling water pipe 530 installed inside the condensing unit 400 .

The water separated in the first and second separators 511 and 512 is discharged to the water tank 540a. And the water remaining in the distillation column 520 is discharged to the third separator 513 and separated.

The oil/water separator 510 may be connected to the distillation column 520 to deliver oil gas to the distillation column 520 . A fluid containing moisture has been applied to prevent air from penetrating between the raw materials in the oxygen shutoff valve 260 of the above-described raw material compression unit 200, and basically, moisture exists inside the combustible waste, and later When oil is obtained by distilling oil gas, if water is mixed in, the quality of the oil itself may deteriorate. Therefore, it is preferable to separate water by including an oil/water separation unit 510.

The oil-water separation unit 510 can separate water vapor inside the oil gas by using the difference in specific gravity between oil and water, and can condense the water vapor having a higher freezing point into water by contacting the gas with cooling water of a predetermined temperature.

The separated discharged water can be transmitted to the above-mentioned oxygen blocking spray hole 252 to prevent flammable gas from permeating between raw materials, or it can be connected to the water tank 540a and used as cooling water.

The vacuum distillation unit 530 shown in FIG. 13 may include a plurality of vacuum distillation tanks 531, and each vacuum distillation tank 531 may be connected in series. It is preferable that a pipe through which cooling water delivered from the water tank 540 flows is interpolated into the vacuum distillation tank 531 . The oil gas may be solidified into liquid oil while passing through the plurality of vacuum distillation tanks 531. The vacuum distillation unit 530 includes a plurality of vacuum distillation tanks 531, so that oil can be classified and solidified according to the freezing point. The vacuum distillation tank 531 may be connected to each oil tank, and at this time, the liquid oil collected in the oil tank may be classified and used for each purpose.

Excess gas that is not solidified even after passing through the last vacuum distillation tank 531 is collected in the gas tank 800 and passes through a gas turbine to generate electricity.

Hereinafter, the configuration and characteristics of the condensing unit 400 of the present invention will be described with reference to FIG. 15 .

The continuously movable pyrolysis emulsification apparatus 1000 of the present invention may further include a condensation unit 400. The condenser 400 may be positioned between the gas difference separator 600 and the distillation unit 500 to condense gas. In more detail, the gas separated from the gas difference separation device 600 connected to the gas outlet 612 of the gas difference separation device 600 may pass through the condensation unit 400 and then be transported to the distillation unit 500 .

The condensation unit 400 includes a condensation housing 410 having a space formed therein, and a condensation pipe 420 disposed in the inner space of the condensation housing 410 and flowing cooling water introduced through the cooling water pipe 430. can include

Cooling water flowing inside the condensation pipe 420 may be cooling water delivered from the water tank 540 through the cooling water pipe 430 described above.

At this time, the condensation pipe 420 may be formed of a single pipe, and the condensation pipe 420 may form a disc shape by spiraling in one plane around the cooling water pipe 430. It is preferable that the plurality of discs on which the condensation pipes 420 are densely arranged are arranged in multiple stages in the direction of gas flow. However, it is preferable to maintain a predetermined distance between the condensation pipe 420 and the condensation pipe 420 . This is to prevent heat exchange between the condensing pipes 420 . The cooling water pipe 430 is installed to pass through and be connected to the center of the condensation pipe 420 having the above structure, so that the gas can flow and be condensed.

The cooling water flowing in the condensation pipe 420 may have a temperature such that the temperature of the gas is lower than the freezing point of oil and maintained above the freezing point of water vapor during heat exchange with the gas. Accordingly, as the gas passes through the condensing unit 400, oil-water separation may be performed. Accordingly, when the gas is transferred to the oil-water separation unit 510, the solidified water can accumulate at the lower end of the oil-water separation unit 510 and be transferred to the water tank 540, and the non-congealed oil gas can be transferred to the distillation tower 520. After distillation under reduced pressure, it can be collected by the user as liquid oil.

The condensation unit 400 is included between the gas difference separation device 600 and the distillation unit 500 of the present invention, so that the separation of the oil and water separation unit 510 can be smoothed out, and the obtained oil quality can be improved.

And the present invention is a chlorine removal device 550 for removing chlorine from the gas distilled and discharged from the distillation unit 500, a desulfurization device 560 for removing sulfur atoms or sulfur compounds, and a turbidity improving device for improving turbidity ( 570) and the fine dust separation device 580 are connected to store the separated gas in the gas tank 800.

Hereinafter, the configuration and characteristics of the absorption chiller 950 of the present invention will be described with reference to FIG. 16 .

An absorption chiller 950 is formed at the top of the pyrolysis furnace 300 so that waste heat generated from the high temperature generated in the pyrolysis furnace 300 can be recycled to the outside, and cooling water is generated using the waste heat, and the generated cooling water is stored in a water tank. It is configured to be transported to 540 and recycled.

In addition, by recycling the cooling water generated in the absorption chiller 950 by supplying it to the condensing unit 400, the distillation column 520, and the gas distillation tube 440, wastewater generated in the pyrolysis process can be removed and used as supplementary water. There is.

And, as shown in FIG. 1, the continuously movable pyrolysis and emulsification apparatus according to the present invention is a facility at a stage before inputting and compressing combustible waste, and in the combustible waste sorter 2100 for sorting foreign substances such as soil, earth, stone, and iron from combustible waste A pretreatment device (2000) including a shredder (2300) that sorts combustible waste, sorts metal mixed in the sorted combustible waste with a magnetic separator (2200), and cuts and supplies the sorted combustible waste to a certain size or less It is constructed by connecting with

As described above, the detailed description of the present invention has been made by examples with reference to the accompanying drawings, but since the above-described embodiments have only been described with reference to preferred examples of the present invention, it is believed that the present invention is limited only to the above embodiments. should not be understood. Therefore, in addition to the above description, those skilled in the art, such as the quantitative input of grains, minerals, and soil, etc., can easily explain the embodiments of the present invention in other forms within the same scope as the above embodiments. The present invention of can be practiced, or the invention of the scope equivalent to the present invention will be able to be practiced.

1000. Continuous operation type pyrolysis emulsification equipment
100. Raw material input unit 110. Hopper
120. Rotary compression plate 130. Outlet
200. Raw material compression unit 210. Compression space
220. Compression tube 230. Piston
240. Input pipe 250. Input transfer screw
251. Input screw pipe 260. Oxygen cut-off valve
270. Thrust bearing 280. Insulation
300. Pyrolysis furnace 310. Raw material outlet
320. Pyrolysis housing 330. Raw material inlet
340. Protruding guide part 341. Spiral protruding live wire
342. Straight protrusion 343. Transfer screw discharge pipe
344. Discharge screw 350. Inspection port
360. Heating unit 370, 371. Rollo
400. Condensation unit 410. Condensation housing
420. Condensation pipe 430. Coolant pipe
440. Gas distillation pipe 441. Discharge pipe
442. Downpipe 500. Distillation
510. Oil and water separation unit 520. Distillation tower
530. Vacuum distillation unit 531. Vacuum distillation tank
540. Water tank 550. Chlorine removal device
560. Desulfurization device 570. Turbidity improvement device
580. Fine inspection equipment
600. Gas difference separator 610. Main body
611. Dust collection hopper 611a. horizontal transfer screw
612. Gas outlet 620. Perforated disk dust collection plate
621. Gas discharge hole 622. Carbonized fine discharge hole
623. Fixed plate 624. Angle
625. fasteners
630. Multi-stage disk dust collector 640. Motor
650. Rotating shaft 660. Rotary cleaner
670. Connected bearing 680. Inspection part
690. Discharge transfer screw
700. High-temperature filter dust collector 710. High-temperature filter
711. Ceramic foam 712. Fibrous filter
713. Particulate filter 714. Body
800. Gas Tank
900. Supply storage silo 910. Differential transfer screw
920. Mixer 921. Rotating body for stirring
930. Molding machine 940. Compressed water supply nozzle
950. Absorption chiller 960. Transfer conveyor
2000. Pretreatment device 2100. Combustible waste sorting department
2200. Magnetic separator 2300. Crusher

Claims (15)

A raw material input unit 100 for inputting flammable waste;
a raw material compression unit 200 for compressing and transferring combustible waste from the raw material input unit 100;
a pyrolysis furnace 300 for thermally decomposing and transporting the combustible waste compressed in the raw material compression unit 200;
a condensing unit 400 condensing the gas discharged from the pyrolysis furnace 300;
It is configured to include a distillation unit 500 for generating gas and oil by distilling the gas condensed and discharged in the condensation unit 400,
A gas difference separator 600 for receiving and separating the carbonized by-products mixed with the gas decomposed in the pyrolysis furnace 300 is connected between the pyrolysis furnace 300 and the condensation unit 400 to form,
The gas difference separator 600,
A dust collection hopper 611 having a conical lower part to store and discharge carbonized by-products;
A main body 610 having a gas outlet 612 formed on the top of the dust collecting hopper 611 to discharge the separated gas by collecting the dust;
The inside of the main body 610 includes a multi-stage disk dust collector 630 that collects and separates only the gas thermally decomposed in the pyrolysis furnace and guides it to the top,
The multi-stage disk dust collector 630 is equipped with a plurality of perforated disk dust collectors 620 at intervals in multiple stages (3 to 7 stages), and the center of the perforated disk collector 620 receives power from the motor 640 to rotate. A rotating shaft 650 is mounted, and the rotating shaft 650 is in contact with the upper and lower surfaces of the perforated disc collecting plate 620 while rotating to remove the fine powder of the carbonized by-products in contact with the perforated disc collecting plate 620 Rotating cleaner 660 Continuously movable pyrolysis emulsification apparatus, characterized in that configured by mounting. According to claim 1,
The perforated disk dust collecting plate 620 is formed in a semicircular shape (1/2 circular shape) for convenient detachment and maintenance of the fixing plate 623 fixed to all sides of the main body 610 to facilitate separation and coupling from the rotating shaft 650. Continuously movable pyrolysis emulsification apparatus, characterized in that it is seated on the angle 624 mounted on the outer periphery and coupled using the fastener 625. According to claim 1,
A gas discharge hole 621 for collecting and separating only gas in the perforated disk dust collecting plate 620 and a diameter 0.5 to 3 times larger than the gas discharge hole 621 are drilled to remove the fine powder of carbonized by-products mixed with the gas. Continuously movable pyrolysis and emulsification device, characterized in that the carbonized fine discharge hole 622 for the perforated disk dust collecting plate 620 is made of a fan shape so as to cross diagonally.
According to claim 1,
The carbonized fine powder discharge hole 622 perforated in the perforated disk collecting plate 620 is not formed in a vertical state with the perforated disk collecting plate 620 formed at intervals in multiple stages, and can suppress vertical discharge of gas while going up to the upper side. Continuously movable pyrolysis emulsification device, characterized in that arranged in the form of a screw so that the perforated disk dust collection plate 620 is staggered with each other. According to claim 1,
The diameters of the gas discharge hole 621 and the carbonized fine powder discharge hole 622 of the perforated disk dust collection plate 620 are formed smaller by 1/2 to 1/3 toward the upper side so that the fine powder of the carbonized by-product can be optimally collected. Continuously movable pyrolysis emulsification apparatus, characterized in that the configuration. According to claim 1,
The gas difference separator 600 is a continuously movable pyrolysis emulsification device, characterized in that consisting of a plurality of structures connecting one or more. According to claim 1,
The pyrolysis furnace 300 is formed with a conical pyrolysis housing 320 at the front, so that carbonized by-products are introduced into the gas difference separator 600 by the protruding guide part 340 or a protruding guide of the pyrolysis furnace 300. Continuously movable pyrolysis and emulsification apparatus, characterized in that the carbonized by-products dropped from the unit 340 are configured to flow into the inside of the gas difference separator 600 through the discharge screw 344 of the transfer screw discharge pipe 343. According to claim 1,
The configuration of the gas difference separator 600a is to form a high-temperature filter dust collector 700 equipped with a high-temperature filter 710 to collect carbonized by-products and fine powder mixed with the gas discharged from the pyrolysis furnace 300,
In the high-temperature filter 710, a ceramic foam 711, a fibrous filter 712, and a particulate filter 713 are laminated inside a main body 714 formed vertically so that the plurality of main bodies 714 are closely attached to each other. Continuously movable pyrolysis emulsification apparatus, characterized in that configured by. According to claim 1,
The raw material input unit 100 sorts combustible waste in the combustible waste sorter 2100, sorts metal mixed in the sorted combustible waste with the magnetic separator 2200, and sorts the sorted combustible waste in the crusher 2300. Continuously movable pyrolysis emulsification apparatus, characterized in that configured by connecting to the crushing preprocessor (2000). According to claim 1,
The gas distilled and discharged from the distillation unit 500 is a chlorine removal device 550 for removing chlorine, a desulfurization device 560 for removing sulfur atoms or sulfur compounds, a turbidity improving device 570 for improving turbidity, Continuously movable pyrolysis emulsification device characterized in that it is configured to store the separated gas in the gas tank 800 by connecting to the fine inspection device 580 for separating fine dust. According to claim 1,
The gas difference separator (600b) connected between the pyrolysis furnace 300 and the condensation unit 400 is a continuously movable pyrolysis and emulsification device, characterized in that it is configured by combining a multi-stage disk dust collector 630 and a filter dust collector 700 in a stacked manner. . According to claim 1,
Combustible waste injected into the input space 210 of the raw material compression unit 200 by the rotary compression plate 120 of the raw material input unit 100 is secondarily compressed by the action of the piston 230, and 240), two or more oxygen shutoff valves 260 are formed at intervals between the compression space 210 and the injection pipe 240 to prevent blocking of oxygen and air in the combustible waste,
When the secondly compressed combustible waste is moved to the inlet pipe 240, the oxygen cutoff valve 260 is first and second sequentially opened and transported to the inlet pipe 240, and transferred to the inlet pipe 240 When this is completed and the compression plate 210 moves backward by the action of the piston 230, the oxygen shutoff valve 260 is closed opposite to the opening to block the inflow of air. According to claim 12,
When the compression plate 230 transfers the combustible waste that has been first compressed into the compression space 210 forward and sequentially secondarily compressed and stacked in a book shape, 1, 2, 3, 4, The 5-step combustible waste is secondarily compressed and stacked sequentially, and the combustible waste is stacked in the form of books in the first, second, and third steps in the front in the compression space 210,
When the compression action of the compression plate 230 is repeated, the combustible waste stacked in the form of a book in the compression space 210 is transported forward while serving as a compression plate, and compressed into a book form in the input pipe 240. First stage compression Characterized in that the compressed combustible waste from the compressed combustible waste in the fifth step is sequentially transferred to the input transfer screw 250 mounted on the input screw pipe 251 and continuously introduced into the pyrolysis furnace 300. Characterized in that Continuously operated pyrolysis emulsifier. According to claim 12,
When the combustible waste is compressed and moved by the input pipe 240 and the input screw pipe 251, liquid flow is sprayed from the oxygen blocking nozzle 252 installed outside the input pipe 240 and the input screw pipe 251 to obtain oxygen and continuously movable pyrolysis and emulsification apparatus characterized in that it is configured to block air to facilitate the movement of compressed combustible waste and to prevent blocking of oxygen and air in the pyrolysis furnace (300). According to claim 1,
Carbonized by-products discharged to the dust collection hopper 611 formed at the lower part of the gas difference separator 600 are transferred forward through the horizontal transfer screw 611a and fall to the discharge transfer screw 690,
Carbonized by-products transferred to the discharge transfer screw 690 are formed to be transferred to the supply storage silo 900,
The carbonized by-products stored in the supply and storage silo 900 are discharged through the lower discharge port and dried by being supplied with compressed water through the compressed water supply nozzle 940 in the process of being transferred to the fine powder transfer screw 910 without generating fine powder of the carbonized by-products. Fine dust (fine powder) of carbonized by-products (Char) and compressed water are mixed to form a mixture to be transported to a mixing mixer 920 for forming carbonized by-products,
A spray nozzle 922 for spraying fluid to the carbonized by-products stored in the mixing mixer 920 is formed on the upper side to supply fluid to the carbonized by-products transported to the mixing mixer 920 to increase the dough quality required for molding. It is formed to stir using the rotating body 921 for stirring so that it can be mixed.
The carbonized by-products stirred in the mixing mixer 920 are discharged through the lower discharge port and introduced into the molding machine 930, and the carbonized by-products introduced into the inside are molded into pellets or briquettes by the piston 931 and discharged. Continuously movable pyrolysis emulsification apparatus, characterized in that configured to.

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