KR101131170B1 - Apparatus for multy-stage pyrolysis and method thereof - Google Patents

Abstract

The present invention is a multi-stage pyrolysis apparatus and a multi-stage pyrolysis method that can control the process step by step, implement a step-by-step continuous production process, and increase the energy efficiency by using the energy generated in the combustion process in the pyrolysis process. The present invention relates to a multistage pyrolysis apparatus according to the present invention, comprising: a supply unit supplying a combustible material; A first pyrolysis section configured to pyrolyze the combustible material conveyed from the supply section to produce a first gaseous fraction and a first pyrolysis residue; A second pyrolysis section configured to pyrolyze the first pyrolysis residue conveyed from the first pyrolysis section to generate a second gaseous fraction and a second pyrolysis residue; And partial oxidation and combustion gaseous fraction and combustion residues are produced through the partial oxidation and combustion reaction of the second pyrolysis residue transferred from the second pyrolysis portion, and the partial oxidation and combustion gaseous fraction is subjected to the second pyrolysis. And a combustion unit for transferring to the unit, wherein at least one of the first gas phase fraction and the second gas phase fraction is converted into gaseous or liquid fuel.

Description

Multistage pyrolysis apparatus and multistage pyrolysis method {Apparatus for multy-stage pyrolysis and method

The present invention relates to a multi-stage pyrolysis apparatus and a multi-stage pyrolysis method, more specifically, it can be pyrolyzed in multiple stages to control the process step by step, to implement a step-by-step continuous production process, and pyrolysis process energy generated in the combustion process It relates to a multi-stage pyrolysis apparatus and a multi-stage pyrolysis method that can be used to increase the energy efficiency.

Conventional techniques for pyrolyzing waste, lower fuel, or organic-inorganic mixtures and converting them into carbides, liquids, and gaseous substances have achieved pyrolysis or gasification through unit reactors. This conventional process does not take into account the various pyrolysis and gasification characteristics of each waste, lower fuel, or organic-inorganic mixture, etc., and pyrolysis gasification in the unit reactor is low conversion efficiency and low productivity.

It is necessary to extract useful energy sources before treating combustible materials. To this end, the development of technologies that use waste resources as energy sources is spreading worldwide. To this end, technologies for producing syngas, which is a liquid fuel or a gaseous fuel, by pyrolyzing or gasifying waste resources are being developed one after another.

A technology for producing syngas from waste pyrolysis melt gasification was developed at Thermoselect in Switzerland in 1994, and has been commercialized in Japan's Kawasaki Steel. Daewoo E & C and Korea Advanced Institute of Technology are also trying to commercialize in Korea. However, the above-described technique applies waste to gasification melting technique, which results in low energy efficiency. In particular, since Thermoselect gasifies most of the waste by combustion of oxygen, it is difficult to smoothly operate a gas engine without auxiliary fuel because the amount of heat generated from syngas is low. In addition, Toshiba, Japan, has developed a process for pyrolysis and gasification of ASR using a rotary kiln. It is a process that produces gas phase oil by pyrolyzing at about 550 ℃ through indirect heating and reforming it at 1100 ℃ for high temperature. This process releases char to pyrolysis residues, which requires additional reduction and char treatment and combustion.

In addition, the process of producing gaseous fuel from high calorific value materials such as plastics or waste tires, low fuel, wood, waste paper, etc. among waste resources is based on pyrolysis gasification process and produces syngas. Such syngas production is more difficult to process and store than the production of liquid fuels and has lower added value.

In addition, most pyrolysis gasification technologies are operated in batch mode, resulting in low productivity and low efficiency.

Therefore, this patent produces liquid and gaseous fuels at the same time through pyrolysis gasification from waste resources, or efficiently produces gaseous fuels, and finally, chars are minimized in the remaining residues. It is proposed a multi-stage pyrolysis gasification apparatus and method for discharging ash to be less than 10% as a reference.

The present invention has been made to solve the above problems, an object of the present invention, by subjecting the target material such as waste, low-grade fuel, organic-inorganic mixture, etc. in multiple stages to control the process step by step, suitable for the target material It is to provide a multi-stage pyrolysis apparatus and a multi-stage pyrolysis method that can implement a step-by-step process to reach the desired final material.

It is also an object of the present invention to provide a multi-stage pyrolysis apparatus and a multi-stage pyrolysis method capable of realizing a step-by-step continuous production process by transporting materials continuously at each stage.

It is also an object of the present invention to provide a multi-stage pyrolysis apparatus and a multi-stage pyrolysis method which can increase energy efficiency by using energy generated in a combustion process in a pyrolysis process.

Multistage pyrolysis apparatus according to the present invention according to the above object is a supply unit for supplying a combustible material; A first pyrolysis section configured to pyrolyze the combustible material conveyed from the supply section to produce a first gaseous fraction and a first pyrolysis residue; A second pyrolysis section configured to pyrolyze the first pyrolysis residue conveyed from the first pyrolysis section to generate a second gaseous fraction and a second pyrolysis residue; And partial oxidation and combustion gaseous fraction and combustion residues are produced through the partial oxidation and combustion reaction of the second pyrolysis residue transferred from the second pyrolysis portion, and the partial oxidation and combustion gaseous fraction is subjected to the second pyrolysis. And a combustion unit for transferring to the unit, wherein at least one of the first gas phase fraction and the second gas phase fraction is converted into gaseous or liquid fuel.

Multistage pyrolysis apparatus according to the present invention according to the above object comprises a first cooling unit for cooling the first gas phase fraction; A separation unit for separating the cooled liquid component from the first gas phase fraction; A storage unit for storing the separated liquid component; And, it is preferable to further include a first induction blower for attracting the first gas phase fraction remaining after separating the liquid component.

Multi-stage pyrolysis apparatus according to the present invention according to the above object is a reforming unit for converting the second gas phase fraction to a synthesis gas through a reforming reaction; A second cooling unit cooling the synthesis gas; A first filter unit filtering the cooled synthesis gas; And a second attracting blower for attracting the filtered synthesis gas.

Multi-stage pyrolysis apparatus according to the present invention according to the above object is a third cooling unit for cooling the partial oxidation and combustion gaseous fraction; A second filter part for filtering the cooled partial oxidation and combustion gaseous fraction; And a third drawer blower for attracting the filtered partial oxidation and combustion gaseous fraction.

Multistage pyrolysis apparatus according to the present invention according to the above object is preferably characterized in that for supplying the second gas phase fraction to the first pyrolysis unit.

Multistage pyrolysis apparatus according to the present invention according to the above object is preferably characterized in that for supplying the partial oxidation and combustion gaseous fraction to the second pyrolysis unit.

Multi-stage pyrolysis apparatus according to the present invention according to the above object is preferably characterized in that for supplying the partial oxidation and combustion gaseous fraction passing through the second pyrolysis portion to the first pyrolysis portion.

Multi-stage pyrolysis apparatus according to the present invention according to the above object is such that the second pyrolysis residues from the second pyrolysis section to the combustion section, and the second gaseous fraction cannot move to the combustion section at the interface between the second pyrolysis section and the combustion section It is preferable to further include a shielding device.

In the multi-stage pyrolysis apparatus according to the present invention according to the above object, the first pyrolysis unit pyrolyzes at a temperature of 350 ° C. to 600 ° C. for 10 minutes or more, the second pyrolysis unit is pyrolyzed at a temperature of 600 ° C. or more, and the combustion unit is 800 It is preferable to make it burn at the temperature of more than degreeC.

In the multi-stage pyrolysis apparatus according to the present invention according to the above object, the first pyrolysis unit is dried and preheated at 100 ° C. or higher, and the second pyrolysis unit is pyrolyzed at a temperature of 350 ° C. or higher for 10 minutes or more, and the combustion unit has a temperature of 800 ° C. or higher. It is preferable to characterize the partial oxidation and combustion at.

Multi-stage pyrolysis apparatus according to the present invention according to the above object is a plurality of heating the first pyrolysis section, the second pyrolysis section, the combustion section below the first pyrolysis section, the second pyrolysis section, the combustion section, respectively. It is preferable to further include a heating device.

Multi-stage pyrolysis apparatus according to the present invention according to the above object further comprises an oxidant supply device for supplying any one or more of steam, oxygen, and air to at least one of the second pyrolysis unit and the combustion unit. Do.

Means for moving the materials generated in the first pyrolysis section, the second pyrolysis section, and the combustion section may be one of a stalker type, a rotary kiln type, a fluidized bed type, or a combination of two or more means. It is preferable to characterize.

Multi-stage pyrolysis method according to the present invention according to the above object comprises the steps of (a) supplying a combustible material; (b) introducing the combustible material into a first pyrolysis section and pyrolysing to produce a first gaseous fraction and a first pyrolysis residue; (c) introducing the first pyrolysis residue into second pyrolysis and drying, preheating or pyrolysing to produce a second gaseous fraction and a second pyrolysis residue; And (d) introducing the second pyrolysis residue into the combustion section and producing partial oxidation and combustion gaseous fraction and combustion residues through partial oxidation and combustion reactions, wherein the first gaseous fraction and the second Preferably, at least one of the gaseous fraction is converted into a gaseous or liquid fuel.

Multi-stage pyrolysis method according to the present invention according to the above object (b-1) cooling the first gas phase fraction; (b-2) separating the cooled liquid component from the first gas phase fraction; (b-3) storing the separated liquid component; And, (b-4) it is preferable to further include the step of attracting the first gas phase fraction remaining after separating the liquid component.

Multi-stage pyrolysis method according to the present invention according to the above object (c-1) converting the second gas phase fraction into a synthesis gas through a reforming reaction; (c-2) cooling the syngas; (c-3) filtering the cooled syngas; And, (c-4) preferably further comprises the step of attracting the filtered synthesis gas.

Multi-stage pyrolysis method according to the present invention according to the above object (d-1) cooling the partial oxidation and combustion gaseous fraction; (d-2) filtering the cooled partial oxidation and combustion gaseous fraction; And (d-3) attracting the filtered partial oxidation and combustion gaseous fraction.

The multi-stage pyrolysis method according to the present invention according to the above object (e-1) converting the second gas phase fraction and partial oxidation and combustion gas phase fraction into a synthesis gas through a reforming reaction; (e-2) cooling the syngas; (e-3) filtering the cooled syngas; And (e-4) attracting the filtered syngas.

Multistage pyrolysis method according to the present invention according to the above object preferably further comprises the step of (f) supplying the second gas phase fraction to the first pyrolysis unit.

Multistage pyrolysis method according to the present invention according to the above object preferably further comprises the step of supplying the partial oxidation and combustion gaseous fraction to the second pyrolysis unit.

The multistage pyrolysis method according to the present invention according to the above object preferably further comprises the step of (f) passing the partial oxidation and combustion gaseous fraction through the second pyrolysis section and feeding it to the first pyrolysis section.

In the step (b), the first pyrolysis unit is heated to a temperature of 350 ℃ to 600 ℃, the flammable material is to remain in the first pyrolysis unit for 10 minutes or more, in the step (c), in the second The pyrolysis unit is heated to a temperature of 600 ℃ or more, and in the step (d), it is preferable that the combustion unit is heated to a temperature of 800 ℃ or more.

In the step (b), the first pyrolysis section is heated to a temperature of 100 ℃ or more, in the step (c), the second pyrolysis section is heated to a temperature of 350 ℃ or more, and stayed for 10 minutes or more and (d) In the step, the combustion unit is preferably characterized in that the heating to a temperature of 800 ℃ or more.

Preferably, any one or more of steam, oxygen, and air is supplied to at least one of the steps (c) and (d).

The materials produced in the steps (b) to (d) are moved by any one of a stalker type, a rotary kiln type, and a fluidized bed type, or the means are moved in a combined form of two or more. It is preferable.

1 is a view showing a multi-stage pyrolysis apparatus according to a first embodiment of the present invention.
Figure 2 is a view showing the implementation of a multi-stage pyrolysis apparatus according to the first embodiment of the present invention by rotary kiln transfer means.
Figure 3 is a view showing the implementation of the multi-stage pyrolysis apparatus according to the first embodiment of the present invention in a fluidized bed.
4 is a view showing a multi-stage pyrolysis apparatus according to a second embodiment of the present invention.
5 is a view showing a multi-stage pyrolysis apparatus according to a third embodiment of the present invention.
6A to 6F are graphs showing the results of thermogravimetric analysis of PVC, PP, RPF, RDF, waste tire, and wood, respectively.
Figure 7 is a graph showing the removal rate of chlorine over time when the mixture of PE and PVC pyrolyzed at 350 ℃ and 400 ℃, respectively.
8 is a graph showing the weight of the gaseous phase, liquid phase, and solid residue produced when isothermal pyrolysis of RPF at 400 ° C, 600 ° C, and 800 ° C.
9 is a graph showing the mass reduction according to the size of the PVC when the thermal decomposition of the PVC at 350 ℃.
10 is a graph showing the yield of gaseous, liquid, and solid materials produced by pyrolysis of RPFs when oxygen and steam are supplied.
11 is a graph showing the yield of gaseous, liquid, and solid materials produced by pyrolysis of RPFs when steam is supplied.

Hereinafter, a multi-stage pyrolysis apparatus according to a first embodiment of the present invention will be described in detail with reference to the accompanying drawings.

1 is a view showing a multi-stage pyrolysis apparatus according to a first embodiment of the present invention.

In the multi-stage pyrolysis apparatus according to the first embodiment of the present invention, the first gaseous fraction and the first pyrolysis residue are dried, preheated or pyrolyzed by the supply unit 110 supplying the combustible material and the combustible material transferred from the supply unit 110. A second pyrolysis unit 122 for generating a second gaseous fraction and a second pyrolysis residue by pyrolyzing the first pyrolysis unit 120 and the first pyrolysis residue transferred from the first pyrolysis unit 120 The second pyrolysis residue conveyed from the second pyrolysis section 122 is composed of a combustion section 124 that generates partial oxidation and combustion gaseous fraction and combustion residues through partial oxidation and combustion reactions.

Supply unit 110 is household waste, industrial waste, rural greenhouse plastic waste, waste plastic. Hopper flammable waste such as waste tires and electronic waste, or lower fuel such as lignite, anthracite, pet coke, oil sand, etc. or organic-inorganic mixtures such as wood, biomass, sewage sludge, organic waste, etc. Transfer to the first pyrolysis unit 120 through a device such as a (hopper). At this time, the combustible materials to be supplied are preferably provided in the form of a pulverized material having a size of about 1 ~ 10 cm in order to increase the efficiency of pyrolysis, but can be supplied in a larger size, which is adjusted according to the residence time in each step It is possible.

The first thermal decomposition unit 120 substantially reduces the harmful components such as chlorine, sulfur and bromine in the combustible material, so that the halogen components such as chlorine and bromine are preferably about 90% or more, more preferably Is dried, preheated or pyrolyzed under conditions which can be removed by at least about 95%. In this case, 'pyrolysis' refers to a reaction that induces chemical decomposition of the combustible material by heating the combustible material in a state of limiting contact with oxygen, and “drying” and “preheating” are generally used as the description. It will be omitted. That is, the first pyrolysis unit 120 may perform reactions of any one of drying, preheating, or pyrolysis or a combination thereof with respect to the combustible material.

6A to 6F, 7, 8, and 9 illustrate appropriate temperature conditions of the first pyrolysis unit 120.

6a to 6f are graphs showing the results of thermogravimetric analysis of PVC, PP, RPF, RDF, waste tires and wood, respectively, and FIG. 7 is a time when pyrolyzed mixtures of PE and PVC at 350 ° C and 400 ° C, respectively. Figure 8 is a graph showing the removal rate of chlorine according to, Figure 8 is a graph showing the weight of the gas phase, liquid, solid residues generated when isothermal pyrolysis of RPF at 400 ℃, 600 ℃, 800 ℃, Figure 9 is a PVC 350 When thermal decomposition at ℃ is a graph showing the mass decrease according to the size of the PVC.

PVC contains more than 50% chlorine (Cl ₂ ), referring to Figure 6a, it can be seen that most of the chlorine is discharged in the vicinity of 400 ℃ through pyrolysis.

In addition, looking at Figure 6b to 6f, it can be seen that even in the case of PP, RPF, RDF, waste tire, and wood pyrolysis at about 400 ℃ or more 90% or more chlorine is discharged.

Referring to FIG. 7, when the mixture of PE and PVC is thermally decomposed at 350 ° C., 85% is removed after about 10 minutes and 90% is removed after 20 minutes. In addition, when the mixture of PE and PVC is pyrolyzed at 400 ° C, 91.5% is removed after about 10 minutes and 90% is removed after 20 minutes.

Referring to FIG. 8, when the pyrolysis temperature is raised to 600 ° C. or more, the liquid component decreases and the gas phase component increases accordingly.

Therefore, the first pyrolysis unit 120 preferably pyrolyzes the combustible material at a temperature of 400 ° C. to 600 ° C. for at least 10 minutes.

Referring to FIG. 9, it can be seen that the time required for mass reduction is gradually reduced when the size of the PVC is small compared to the case where the size of the PVC is large. That is, the pyrolysis progress time can be properly adjusted according to the size of the PVC.

The second pyrolysis unit 122 introduces a first pyrolysis residue transferred from the first pyrolysis unit 120 and undergoes pyrolysis at a temperature higher than that of the first pyrolysis unit 120 to maintain the second gaseous fraction and the second pyrolysis residue. Produces water. At this time, the second pyrolysis unit 122 is preferably pyrolyzed at a temperature of about 600 ℃ or more.

The combustion unit 124 preferably introduces a second pyrolysis residue transferred from the second pyrolysis unit 122 to partially oxidize and burn at a temperature of about 800 ° C. or more to generate partial oxidation and combustion gaseous fraction and combustion residue. Do. Combustible materials such as PE (polyethylene) are gasified in the second pyrolysis section 122, but most of the organic and inorganic materials such as waste tires remain in carbide form in the second pyrolysis section 122 and are transferred to the combustion section 124. do. The combustion unit 124 may completely burn the second pyrolysis residue and discharge only ash.

On the other hand, it is noted that the second gaseous fraction may be supplied to the first pyrolysis section 120, and the partial oxidation and combustion gaseous fraction may be supplied to the first pyrolysis section 120 through the second pyrolysis section.

In addition, when the first pyrolyzing unit 120 is dried and preheated without pyrolyzing the combustible material and the second pyrolyzing unit 122 pyrolyzes the combustible material, the first pyrolyzing unit 120 is at 100 ° C. or more. It is preferable to dry and preheat the flammable material, after which the second pyrolysis section 122 thermally decomposes at a temperature of 350 ° C. or more for 10 minutes or more, and the combustion section is partially oxidized and burned at a temperature of 800 ° C. or more.

≪ Example 1 >

The multi-stage pyrolysis apparatus according to the first embodiment of the present invention is connected to the first pyrolysis section 122 to separate the liquid components cooled in the first cooling section 150 and the first gas phase fraction to cool the first gas phase fraction. It is preferable to further include a separator 152, a storage unit 154 for storing the separated liquid component, and a first induction blower 156 for guiding the remaining first gas phase fraction after separating the liquid component.

In addition, the reforming unit 160 is connected to the second pyrolysis unit 124 to convert the second gaseous fraction into the synthesis gas through the reforming reaction, the second cooling unit 162 for cooling the synthesis gas, and the cooled synthesis gas. It is preferable to further include a first filter 164 for filtering, a second attracting blower 166 for attracting the filtered synthesis gas.

Also, a third cooling unit 172 connected to the combustion unit to cool the partial oxidation and combustion gaseous fraction, a second filter unit 174 for filtering the cooled partial oxidation and combustion gaseous fraction, filtered partial oxidation and combustion gas phase It is preferable to further include a third attracting blower 176 to attract oil.

The liquid component stored in the storage unit 154 may be used as the liquid fuel, and the gas phase component attracted by the first attracting blower 156 may be used as the gaseous fuel.

The synthesis gas attracted by the second attracting blower 166 may be utilized as a gaseous fuel as the clean synthesis gas filtered by the first filter unit 164.

The partial oxidation and combustion gaseous fraction attracted by the third attracting blower 176 is carbon monoxide (CO) or carbon dioxide (CO ₂ ).

In the multi-stage pyrolysis apparatus of the present invention, the first pyrolysis unit 120, the second pyrolysis unit 122, and the lower portion of the combustion unit 124 may include a first heating unit 130, a second heating unit 132, and a third heating unit. Preferably, the apparatus 134 is further included. A burner or a plasma generator may be used as the first heating device 130, the second heating device 132, and the third heating device 134, respectively, and the first pyrolysis part 120 and the second pyrolysis part 122 may be used. ), The combustion unit 124 is heated according to a preset temperature.

The multi-stage pyrolysis apparatus of the present invention preferably further includes an oxidant supply device for supplying at least one of steam, oxygen, and air to at least one of the second pyrolysis unit 122 and the combustion unit 124. Compared with FIG. 8 with reference to FIGS. 10 and 11, it can be seen that when oxygen and steam are supplied during the thermal decomposition of the RPF, the yield of the gas phase is higher.

At this time, the supply amount of steam, oxygen and air can be adjusted according to the properties of the material therein.

The multi-stage pyrolysis apparatus of the present invention may further include a discharge unit 140 for discharging combustion residues transferred from the combustion unit 124. At this time, the discharge portion 140 is composed of ash (burn) residue is discharged.

The first pyrolysis unit 120, the second pyrolysis unit 122, and the combustion unit 124 are formed of a plurality of parallel movable steps, and the material generated therein moves in a stocker manner. The material introduced into the first pyrolysis unit 120 is placed on the first step and undergoes the pyrolysis process, pushing the material from the first step to the second step and removing the remaining material after going through a plurality of steps in the same manner. 2 to the pyrolysis section 122. Subsequently, the material introduced into the second pyrolysis unit 122 is thermally decomposed while sequentially passing through a plurality of steps therein, and pushes the remaining material into the combustion unit 124. Inside the combustion unit 124, partial oxidation and combustion are also performed while passing through a plurality of stairs. As described above, a process of pyrolysis through the first pyrolysis unit 120, the second pyrolysis unit 122, and the combustion unit 124 may be performed sequentially and continuously by parallel movement of a plurality of steps.

In the above described the manner in which the product material is moved to the stocker type in the interior of the multi-stage pyrolysis apparatus according to the first embodiment of the present invention, the first embodiment of the present invention may be implemented in a rotary kiln type, fluidized bed, 2 and 3 are shown. In addition, it may be implemented in the form of a combination of two or more of the stocker, rotary kiln, and fluidized bed.

Figure 2 is a view showing the implementation of the multi-stage pyrolysis apparatus according to the first embodiment of the present invention with a rotary kiln transfer means, Figure 3 is a multi-stage pyrolysis apparatus according to the first embodiment of the present invention implemented by the fluidized bed It is a figure which shows that.

The rotary kiln equation, referring to Figure 2, the first pyrolysis unit 120, the second pyrolysis unit 122, the third pyrolysis unit 124 is composed of a kiln is connected to each other, the kiln is a predetermined angle between the front end and the rear end It has a slope of, so that the product generated inside is moved by the rotary motion of the kiln.

In the drawing, the first heating device 130, the second heating device 132, and the third heating device 134 each include a first pyrolysis unit 120, a second pyrolysis unit 122, and a combustion unit 124. Although provided at the front end of the present invention, the present invention is not limited thereto, and may be installed at the rear end.

When the first pyrolysis unit 120, the second pyrolysis unit 122, and the combustion unit 124 are to be heated by indirect heating, it is also possible to indirectly heat the gas by passing a hot gas through the outer wall of the kiln.

In addition, it is preferable to further include an oxidant supply unit 180 for supplying any one or more of steam, oxygen, and air to at least one of the front end or the rear end of any one of the second pyrolysis unit 122 and the combustion unit 124.

Fluidized-bed is 3, the first thermal cracking unit 120, a second thermal cracking unit (122), as hard as blowing fluidization as Inc. and flow the material inside to put the air in the lower part of the combustion section 124, the air It is mixed with hot fluid sand and pyrolyzed and combusted.

The first pyrolysis unit 120, the second pyrolysis unit 122, and the combustion unit 124 are connected to each other by a pipe, through which the residue generated therein moves like a flow yarn. The first pyrolysis unit 120 receives and heats the flow sand discharged from the second pyrolysis unit 122, and the second pyrolysis unit 122 receives and heats the flow sand discharged from the combustion unit 124.

Additional gas such as steam, oxygen, air is supplied under the conditions necessary to fluidize the fluidized bed reactor.

<Example 2>

Hereinafter, a multi-stage pyrolysis apparatus according to a second embodiment of the present invention will be described in detail with reference to the accompanying drawings.

4 is a view showing a multi-stage pyrolysis apparatus according to a second embodiment of the present invention.

In the multi-stage pyrolysis apparatus according to the second embodiment of the present invention, the first gaseous fraction and the first pyrolysis residue are dried, preheated or pyrolyzed by the supply unit 210 supplying the combustible material and the combustible material transferred from the supply unit 210. A second pyrolysis unit 222 for generating a second gaseous fraction and a second pyrolysis residue by pyrolyzing the first pyrolysis unit 220 and the first pyrolysis residue transferred from the first pyrolysis unit 220 The second pyrolysis residue conveyed from the second pyrolysis section 222 is composed of a combustion section 224 to generate partial oxidation and combustion gaseous fraction and combustion residue through the partial oxidation and combustion reaction.

The supply unit 210, the first pyrolysis unit 220, and the second pyrolysis unit 222 have the same characteristics as those of the first embodiment, and thus description thereof will be omitted.

The multi-stage pyrolysis apparatus according to the second embodiment of the present invention is connected to the first pyrolysis unit 220 to separate the liquid components cooled in the first cooling unit 250 and the first gas phase oil to cool the first gas phase oil. It is preferable to further include a separation unit 252, a storage unit 254 for storing the separated liquid component, and a first induction blower 256 for guiding the first gas phase fraction remaining after separating the liquid component.

In addition, the reforming unit 260, which is connected to the second pyrolysis unit 222 and the combustion unit 224 to convert the second gaseous fraction and the partial oxidation and combustion gaseous fraction into a synthesis gas through a reforming reaction, the converted synthesis gas It is preferable to further include a second cooling unit 262 for cooling, a filter unit 264 for filtering the cooled synthesis gas, and a second attracting blower 266 for attracting the filtered synthesis gas.

The liquid component stored in the storage unit 254 may be used as the liquid fuel, and the gas phase component attracted by the first attracting blower 256 may be used as the gaseous fuel.

The clean synthesis gas filtered by the first filter unit 264 and the synthesis gas drawn by the second attracting blower 266 may be used as clean gaseous fuel.

The partial oxidation and combustion gaseous fraction is carbon monoxide (CO) or carbon dioxide (CO ₂ ), which moves in a direction opposite to the direction in which the combustion residues are discharged and passes the second pyrolysis unit 222 to heat the second pyrolysis unit 222. It can be discharged together with the second gaseous fraction.

In this case, when necessary, when the first pyrolysis residue discharged from the first pyrolysis unit 220 moves to the first pyrolysis unit 222, a shielding device for separating the movement to pass only the solid phase component and not the gaseous phase component is further provided. Can be formed.

In the multi-stage pyrolysis apparatus of the present invention, the first pyrolysis unit 220, the second pyrolysis unit 222, and the lower part of the combustion unit 224 may include a first heating unit 230, a second heating unit 232, and a third heating unit. It is preferred to further include an apparatus 234.

The multi-stage pyrolysis apparatus of the present invention preferably further includes an oxidant supply device for supplying at least one of steam, oxygen, and air to at least one of the second pyrolysis unit 222 and the combustion unit 224.

The multi-stage pyrolysis apparatus of the present invention may further include a discharge unit 240 for discharging the combustion residue conveyed from the combustion unit 224. At this time, the discharge portion 240 is discharged from the combustion residue consisting of ash (ash).

In FIG. 4, a stalker equation is illustrated as a means of moving materials generated by the first pyrolysis part 220, the second pyrolysis part 222, and the combustion part 224, but the second embodiment of the present invention is a rotary kiln type. It may also be implemented in a fluidized bed, or may be implemented in a form in which two or more means of a stalker, a rotary kiln, and a fluidized bed are combined.

&Lt; Example 3 >

Hereinafter, a multi-stage pyrolysis apparatus according to a third embodiment of the present invention will be described in detail with reference to the accompanying drawings.

5 is a view showing a multi-stage pyrolysis apparatus according to a third embodiment of the present invention.

In the multi-stage pyrolysis apparatus according to the third embodiment of the present invention, the first gaseous fraction and the first pyrolysis residue are dried, preheated or pyrolyzed by the supply unit 310 supplying the combustible material and the combustible material transferred from the supply unit 310. A second pyrolysis unit 322 for generating a second gaseous fraction and a second pyrolysis residue by thermally decomposing the first pyrolysis unit 320 and the first pyrolysis residue transferred from the first pyrolysis unit 320, and The second pyrolysis residue conveyed from the second pyrolysis section 322 is composed of a combustion section 324 which generates partial oxidation and combustion gaseous fraction and combustion residues through partial oxidation and combustion reaction.

The supply unit 310, the first pyrolysis unit 320, and the second pyrolysis unit 322 have the same characteristics as those of the first embodiment, and thus description thereof will be omitted.

The multi-stage pyrolysis apparatus according to the third embodiment of the present invention is connected to the first pyrolysis unit 320 to separate the first cooling unit 350 and the first liquid phase component cooled in the first gas phase oil. It is preferable to further include a separator 352, a storage unit 354 for storing the separated liquid component, and a first induction blower 356 for guiding the remaining first gas phase fraction after separating the liquid component.

In addition, the reforming unit 360 is connected to the second pyrolysis unit 322 to convert the second gaseous fraction into the synthesis gas through the reforming reaction, the second cooling unit 362 for cooling the synthesis gas, and the cooled synthesis gas. It is preferable to further include a filter 364 for filtering, a second attracting blower 366 for attracting the filtered synthesis gas.

The liquid component stored in the storage unit 354 may be used as the liquid fuel, and the gas phase component attracted by the first attracting blower 356 may be used as the gaseous fuel.

The synthesis gas attracted by the second attracting blower 366 may be utilized as a gaseous fuel as the clean synthesis gas filtered by the filter unit 364.

At this time, if necessary, when the second pyrolysis residue discharged from the second pyrolysis unit 322 moves to the combustion unit 324, a shielding device may be further formed to separate the movement so that only the solid phase component passes and the gas phase component does not. Can be.

Therefore, due to the shielding device, the partial oxidation and combustion gaseous fraction generated in the combustion unit 324 is transferred to the lower portion of the second pyrolysis unit 322 to supply the amount of heat required for pyrolysis in the lower portion of the second pyrolysis unit 322. It is sent to the reforming unit 360 together with the two gaseous fractions. Thus, by using the partial oxidation and combustion gaseous fraction for heating the second pyrolysis section 322, it is possible to save the energy required in the present installation system.

In the multi-stage pyrolysis apparatus of the present invention, the first pyrolysis unit 320, the second pyrolysis unit 322, and the lower portion of the combustion unit 324 may include a first heating unit 330, a second heating unit 332, and a third heating unit. Preferably, the apparatus 334 is further included.

The multi-stage pyrolysis apparatus of the present invention preferably further includes an oxidant supply device for supplying at least one of steam, oxygen, and air to at least one of the second pyrolysis unit 322 and the combustion unit 324.

The multi-stage pyrolysis apparatus of the present invention may further include a discharge unit 340 for discharging the combustion residue conveyed from the combustion unit 324. At this time, the combustion residue consisting of ash is discharged to the discharge part 340.

FIG. 5 illustrates a stalker equation as a means of moving the materials generated by the first pyrolysis unit 320, the second pyrolysis unit 322, and the combustion unit 324, but the third embodiment of the present invention is a rotary kiln type. It may also be implemented in a fluidized bed, or may be implemented in a form in which two or more means of a stalker, a rotary kiln, and a fluidized bed are combined.

Hereinafter, the multi-stage pyrolysis method according to the first embodiment of the present invention will be described in detail. The multi-stage pyrolysis method according to the first embodiment of the present invention includes the steps of (a) supplying a combustible material, (b) Introducing the combustible material into a first pyrolysis section and drying, preheating or pyrolysing to produce a first gaseous fraction and a first pyrolysis residue, (c) introducing the first pyrolysis residue into a second pyrolysis and pyrolysing Producing a gaseous fraction and a second pyrolysis residue, (d) introducing the second pyrolysis residue into the combustion section and producing partial oxidation and combustion gaseous fraction and combustion residues through partial oxidation and combustion reactions. It is made to include.

In step (a), various kinds of waste are supplied to the first pyrolysis unit through a device such as a hopper. At this time, the wastes to be supplied are preferably provided in the form of a pulverized material having a size of about 1 ~ 10 cm in order to increase the efficiency of pyrolysis, but can be supplied in a larger size, which can be adjusted according to the residence time in each step Do.

Step (b) substantially reduces the presence of harmful components such as chlorine, sulfur and bromine in the combustible material, so that halogen components such as chlorine and bromine are preferably at least about 90%, more preferably at least about 95 The combustible material is heated, dried, preheated or pyrolyzed under conditions which can be removed by more than%.

To this end, the first pyrolysis unit 120 preferably performs pyrolysis of the combustible material at a temperature of 350 ° C. to 600 ° C. for at least 10 minutes. On the other hand, in the case of drying and preheating the combustible material, it is preferable to proceed to drying and preheating by heating to a temperature of 100 ℃ or more.

In the step (c), the first pyrolysis residue transferred from the first pyrolysis unit 120 is introduced and pyrolysis is performed at a higher temperature than the first pyrolysis unit 120 to generate the second gaseous fraction and the second pyrolysis residue. do. At this time, the second pyrolysis unit 122 is preferably pyrolyzed at a temperature of about 600 ℃ or more. On the other hand, in the step (b), on the other hand, when the combustible material is dried and preheated, it is preferable that the second pyrolysis section heats the combustible material to a temperature of 350 ° C. or higher and stays for 10 minutes or more.

In the step (d), it is preferable to introduce a second pyrolysis residue transferred from the second pyrolysis unit 122 and combust it at a temperature of about 800 ° C. or more to generate combustion gaseous fraction and combustion residue. Combustible materials such as PE (polyethylene) are gasified in the second pyrolysis section 122, but most of the organic and inorganic materials such as waste tires remain in carbide form in the second pyrolysis section 122 and are transferred to the combustion section 124. do. The combustion unit 124 may completely burn the second pyrolysis residue and discharge only ash.

In the multi-stage pyrolysis method according to the first embodiment of the present invention, the step of cooling the first gas phase fraction generated in step (b), separating the cooled liquid component from the first gas phase fraction, and storing the separated liquid component Preferably, the step of separating the liquid component and attracting the remaining first gas phase fraction.

In this case, the stored liquid component may be used as a liquid fuel, and the first gaseous fraction remaining after separating the liquid component may be used as a gaseous fuel.

In addition, converting the second gaseous fraction generated in step (c) to the synthesis gas through the reforming reaction, cooling the synthesis gas, filtering the cooled synthesis gas, attracting the filtered synthesis gas It is preferable to further include.

At this time, the attracted synthesis gas may be utilized as a gaseous fuel as a clean synthesis gas.

Further, the method may further include cooling the partial oxidation and combustion gaseous fraction generated in step (d), filtering the cooled partial oxidation and combustion gaseous fraction, and attracting the filtered partial oxidation and combustion gaseous fraction. desirable.

At this time, the attracted partial oxidation and combustion gaseous fraction is carbon monoxide (CO) or carbon dioxide (CO ₂ ).

In steps (b), (c) and (d), a heating device such as a burner or a plasma generator may be used to heat according to a predetermined temperature in each step.

At least one of steps (c) and (d) is preferably supplied with at least one of steam, oxygen, and air. At this time, the supply amount can be adjusted according to the properties of the material therein.

In steps (b), (c) and (d), the first pyrolysis residue, the second pyrolysis residue, and the combustion residue are preferably transported in a stocker manner by a number of parallel movable steps. The material introduced into the first pyrolysis section is placed on the first step and undergoes the pyrolysis process, pushing the material on the first step to the second step, and in the same manner, after the plurality of steps are sequentially passed, the remaining material is pushed to the second pyrolysis section. Serve Subsequently, the process of pyrolysis in the second pyrolysis unit and the combustion unit may be performed sequentially and continuously by parallel movement of a plurality of steps.

In addition, the steps (b), (c), (d) may be implemented not only by the stocker method, but also by a rotary kiln type or a fluidized bed, and may be combined with two or more means of the stocker type, the rotary kiln type, and the fluidized bed. It can also be implemented in the form.

Next, the multi-stage pyrolysis method according to the second embodiment of the present invention will be described in detail.

In the multi-stage pyrolysis method according to the second embodiment of the present invention, (a) supplying the combustible material, (b) introducing the combustible material into the first pyrolysis section and drying, preheating or pyrolyzing the first gaseous fraction and the first pyrolysis Producing a residue, (c) introducing the first pyrolysis residue into a second pyrolysis and pyrolysing to produce a second gaseous fraction and a second pyrolysis residue, (d) removing the second pyrolysis residue Introducing into the combustion section and producing partial oxidation and combustion gaseous fraction and combustion residues through partial oxidation and combustion reactions.

converting the second gaseous fraction generated in step (c) and the partial oxidation and combustion gaseous components generated in step (d) to synthesis gas through a reforming reaction, filtering the synthesis gas, attracting the filtered synthesis gas It is preferable to further comprise the step of.

The partial oxidation and combustion gaseous fraction generated in step (d) is carbon monoxide (CO) or carbon dioxide (CO ₂ ), which moves in a direction opposite to the direction in which the combustion residues are discharged, and passes the second pyrolysis portion to heat the second pyrolysis portion, It can be discharged together with the second gaseous fraction. At this time, if necessary, a shielding device may be further formed to separate the movement so that the first pyrolysis residue discharged from the first pyrolysis portion passes only the solid phase component and not the gaseous phase component when the first pyrolysis residue moves to the second pyrolysis portion.

Hereinafter, the multi-stage pyrolysis method according to the third embodiment of the present invention will be described in detail.

In the multi-stage pyrolysis method according to the third embodiment of the present invention, (a) supplying a combustible material, (b) introducing the combustible material into the first pyrolysis section and drying, preheating or pyrolyzing the first gaseous fraction and the first Producing a pyrolysis residue, (c) introducing the first pyrolysis residue into a second pyrolysis and pyrolysing to produce a second gaseous fraction and a second pyrolysis residue, (d) the second pyrolysis residue Is introduced into the combustion section and through partial oxidation and combustion reactions to produce partial oxidation and combustion gaseous fraction and combustion residues.

converting the second gaseous fraction generated in step (c) and the partial oxidation and combustion gaseous components generated in step (d) to synthesis gas through a reforming reaction, filtering the synthesis gas, attracting the filtered synthesis gas It is preferable to further comprise the step of.

The partial oxidation and combustion gaseous fraction generated in step (d) is carbon monoxide (CO) or carbon dioxide (CO ₂ ), which is transferred to the lower portion of the second pyrolysis portion to supply the amount of heat required for pyrolysis at the lower portion of the second pyrolysis portion, and the second It is sent to the reformer along with the gaseous fraction. By using the partial oxidation and combustion gaseous fraction in this way for heating the second pyrolysis section, energy can be saved. In this case, when the second pyrolysis residue discharged from the second pyrolysis unit moves to the combustion unit, it is preferable to further add a shielding device to separate the movement so that only the solid phase component passes and not the gas phase component.

On the other hand, the multi-stage pyrolysis method according to the first, second and third embodiments of the present invention (f) supplying the second gaseous fraction to the first pyrolysis portion, or (f) the partial oxidation and combustion gaseous fraction It is further noted that the method may further include supplying to the second pyrolysis section, or (f) feeding the partial oxidation and combustion gaseous fraction through the second pyrolysis section and feeding the first pyrolysis section. Since a detailed description thereof has been described above, it will be omitted here.

While preferred embodiments of the present invention have been described above, the present invention is not limited to the above-described specific embodiments. That is, those skilled in the art to which the present invention pertains can make many changes and modifications to the present invention without departing from the spirit and scope of the appended claims, and all such appropriate changes and modifications are possible. Equivalents should be considered to be within the scope of the present invention.

110, 210, 310: supply unit 120, 220, 320: first pyrolysis unit
122, 222, 322: second pyrolysis section 124, 224, 324: third pyrolysis section
150, 250: first cooling unit 152, 252, 352: separation unit
154, 254, 354: storage unit 156, 256, 356: first manned blower
160, 260, 360: Reforming part 162, 262, 362: Second cooling part
164: first filter part 264, 364: filter part
166, 266, 366: second manned blower 172: third cooling unit
174: second filter unit 176: third manned blower
180: oxidant supply device 370: shielding device

Claims (25)

A supply unit for supplying a combustible material;
A first pyrolysis section configured to dry, preheat, or pyrolyze the combustible material conveyed from the supply section to produce a first gaseous fraction and a first pyrolysis residue;
A second pyrolysis section configured to pyrolyze the first pyrolysis residue conveyed from the first pyrolysis section to generate a second gaseous fraction and a second pyrolysis residue; And,
A combustion section for generating partial oxidation and combustion gaseous fraction and combustion residues through partial oxidation and combustion reaction of the second pyrolysis residues transferred from the second pyrolysis section,
Converting any one or more of the first gas phase fraction and the second gas phase fraction into a gaseous or liquid fuel,
Characterized in that the second gas phase fraction is supplied to the first pyrolysis section,
Multistage pyrolysis unit.
The method of claim 1,
A first cooling unit cooling the first gas phase fraction;
A separation unit for separating the cooled liquid component from the first gas phase fraction;
A storage unit for storing the separated liquid component; And,
Further comprising a first induction blower for attracting the remaining first gas phase fraction after separating the liquid component,
Multistage pyrolysis unit.
The method of claim 1,
A reforming unit converting the second gas phase fraction into a synthesis gas through a reforming reaction;
A second cooling unit cooling the synthesis gas;
A first filter unit filtering the cooled synthesis gas; And,
Further comprising a second attracting blower for attracting the filtered synthesis gas,
Multistage pyrolysis unit.
The method of claim 1,
A third cooling unit cooling the partial oxidation and combustion gaseous fraction;
A second filter part for filtering the cooled partial oxidation and combustion gaseous fraction; And,
Further comprising a third drawer blower for attracting the filtered combustion gaseous fraction,
Multistage pyrolysis unit.
delete The method of claim 1,
The partial oxidation and combustion gaseous fraction is supplied to the second pyrolysis section,
Multistage pyrolysis unit.
The method of claim 1,
Characterized in that the partial oxidation and combustion gaseous fraction is passed through the second pyrolysis unit and supplied to the first pyrolysis unit,
Multistage pyrolysis unit.
The method according to claim 6 or 7,
Further comprising a shielding device at the interface between the second and third pyrolysis sections, wherein the second pyrolysis residues from the second pyrolysis section move to the combustion section and the second gaseous fraction cannot move to the combustion section.
Multistage pyrolysis unit.
The method of claim 1,
The first pyrolysis unit is pyrolyzed at least 10 minutes at a temperature of 350 ℃ to 600 ℃,
The second pyrolysis unit pyrolyzes at a temperature of 600 ° C. or higher,
The combustion unit is characterized in that the partial oxidation and combustion at a temperature of 800 ℃ or more,
Multistage pyrolysis unit.
The method of claim 1,
The first pyrolysis unit is dried and preheated at 100 ° C. or higher
The second pyrolysis unit pyrolyzes at least 10 minutes at a temperature of 350 ℃ or more,
The combustion unit is characterized in that the partial oxidation and combustion at a temperature of 800 ℃ or more,
Multistage pyrolysis unit.
The method of claim 1,
Further comprising a plurality of heating devices for heating the first pyrolysis section, the second pyrolysis section, the combustion section respectively under the first pyrolysis section, the second pyrolysis section, the combustion section,
Multistage pyrolysis unit.
The method of claim 11,
Further comprising an oxidant supply device for supplying any one or more of steam, oxygen, and air to at least one of the second pyrolysis unit and the combustion unit,
Multistage pyrolysis unit.
The method of claim 1,
Means for moving the materials generated in the first pyrolysis section, the second pyrolysis section, and the combustion section may be one of a stalker type, a rotary kiln type, a fluidized bed type, or a combination of two or more means. Characterized by
Multistage pyrolysis unit.
(a) supplying a combustible material;
(b) introducing the combustible material into a first pyrolysis section and drying, preheating or pyrolysing to produce a first gaseous fraction and a first pyrolysis residue;
(c) introducing the first pyrolysis residue into second pyrolysis and pyrolysing to produce a second gaseous fraction and a second pyrolysis residue; And,
(d) introducing the second pyrolysis residue into the combustion section and producing partial oxidation and combustion gaseous fraction and combustion residue through partial oxidation and combustion reactions; And
(f) supplying said second gas phase fraction to a first pyrolysis portion;
Including,
At least one of the first gas phase fraction and the second gas phase fraction is converted into a gaseous or liquid fuel,
Multistage pyrolysis method.
The method of claim 14,
(b-1) cooling the first gas phase fraction;
(b-2) separating the cooled liquid component from the first gas phase fraction;
(b-3) storing the separated liquid component; And,
(b-4) further separating the liquid component and attracting the remaining first gas phase fraction;
Multistage pyrolysis method.
The method of claim 14,
(c-1) converting the second gas phase fraction into a synthesis gas through a reforming reaction;
(c-2) cooling the syngas;
(c-3) filtering the cooled syngas; And,
(c-4) further comprising attracting the filtered syngas;
Multistage pyrolysis method.
The method of claim 14,
(d-1) cooling said partial oxidation and combustion gaseous fraction;
(d-2) filtering the cooled combustion gaseous fraction; And,
(d-3) further comprising attracting the filtered combustion gaseous fraction;
Multistage pyrolysis method.
The method of claim 14,
(e-1) converting the second gaseous fraction and the partial oxidation and combustion gaseous components into synthesis gas through a reforming reaction;
(e-2) cooling the syngas;
(e-3) filtering the cooled syngas; And
(e-4) further comprising attracting the filtered syngas;
Multistage pyrolysis method.
delete The method of claim 14,
(f) supplying the partial oxidation and combustion gaseous fraction to a second pyrolysis section,
Multistage pyrolysis method.
The method of claim 14,
(f) passing the partial oxidation and combustion gaseous fraction through a second pyrolysis section and feeding it to the first pyrolysis section,
Multistage pyrolysis method.
The method of claim 14,
In the step (b), the first pyrolysis unit is heated to a temperature of 350 ℃ to 600 ℃, the flammable material is to remain in the first pyrolysis unit for 10 minutes or more,
In the step (c), the second pyrolysis unit is heated to a temperature of 600 ℃ or more, and
In the step (d), characterized in that the combustion unit is heated to a temperature of 800 ℃ or more,
Multistage pyrolysis method.
The method of claim 14,
In the step (b), the first thermal decomposition unit is heated to a temperature of 100 ℃ or more,
In the step (c), the second pyrolysis unit is heated to a temperature of 350 ℃ or more, and to stay for 10 minutes or more, and
In the step (d), characterized in that the combustion unit is heated to a temperature of 800 ℃ or more,
Multistage pyrolysis method.
The method of claim 14,
Characterized in that any one or more of steam, oxygen, air to at least one of the steps (c) and (d),
Multistage pyrolysis method.
The method of claim 14,
The materials produced in step (b) to step (d),
Characterized in that the stalker, rotary kiln, and fluidized bed any one of the means, or the means are moved in a combined form of two or more,
Multistage pyrolysis method.

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