WO2016175387A1 - Gasification method for generating synthetic gas from waste, gasification apparatus for generating synthetic gas from waste, and power generation system comprising same - Google Patents

Abstract

The purpose of the present invention is to provide a gasification method and gasification apparatus for generating synthetic gas from waste, capable of minimizing the discharge of environmentally hazardous substances. According to the present invention, provided is a gasification method comprising: a first thermal decomposition step for generating char from waste; and a second thermal decomposition step for gasifying the char generated in the first thermal decomposition and the other products excluding the char, wherein the temperature for performing the second thermal decomposition step is higher than a temperature at which at least one of dioxin and tar starts to decompose.

Description

Gasification method for producing syngas from waste, gasification apparatus for generating syngas from waste, and power generation system including the same

Embodiments of the present invention relate to a gasification method for generating syngas from waste, a gasification apparatus for generating syngas from waste, and a power generation system including the same.

In general, waste or biomass can be broadly divided into flammable and organic wastes, which include, for example, municipal waste, workplace, construction and agriculture waste, landfill waste, and organic waste, for example, food waste. , Sewage sludge, and livestock manure.

On the other hand, gasification (or pyrolysis) is a substance in the gaseous state by heat, chemical energy conversion methods such as coal, waste, wood-based biomass (chaff, corn stalks, sawdust, wood chips, etc.) As a form of phosphorus syngas, the gasification method can be largely divided into a fixed bed method, a fluidized bed method and a fractionated bed method.

Among them, in the fixed bed method, a bottom-up gasification method in which a solid raw material is introduced from the upper side and an oxidant is supplied in a direction opposite thereto, and a direction in which the solid raw material is fed and an air feeding direction are parallel and a tar content is relatively low. It can be subdivided into a top-down gasification method which can be produced, and a countercurrent gasification method in which the introduction of an oxidant is made in terms of.

Next, the fluidized bed method may be subdivided into a circulating fluidized bed gasification method, a bubble bed fluidized bed gasification method, a dual bed fluidized bed gasification method, and the like, and may be a fuel of several millimeters to several centimeters, for example, waste or fine fuel having various properties. Although it can be used for gasification of lower coal, which cannot be used as a furnace, sand is added as a heat medium and a fluidizing material that induces or promotes a reaction in the reactor, so the calorific value is low, the fluctuation is high, and fluidization is performed to operate the fluidized bed gasifier. This requires a certain pressure, a certain flow rate, a gas above a certain temperature, and thus complicated reactor design.

However, the pyrolysis gasification method emits a large amount of dioxin, which is an environmentally harmful substance. In particular, in the case of the fixed-bed gasification method, there is a disadvantage in that the tar content is high at a low gasification temperature and the quality of the generated synthesis gas is low. The burning valves easily clog and corrode and are expensive to remove.

In addition, the pyrolysis gasification method as described above is a waste after pre-treatment such as crushing / crushing, primary magnetic screening, hot air drying, primary wind screening, grinding, secondary magnetic screening, slaked injection, molding, cooling, vibrating screen screening, etc. Since it is supplied to the gasifier, a lot of energy and cost is used in the pretreatment step.

On the other hand, the fractionation layer method is used for gasification by putting an excess of fine fuel together with an oxidant in a high temperature combustion zone of 1600 ° C or higher, and is generally used for gasification of coal, which is easy to be finely divided. It is hard to be applied to waste which is hard to make.

[Preceding technical literature]

[Patent Documents]

Republic of Korea Patent Publication No. 10-1391723 (2014. 02. 28.)

Republic of Korea Patent Publication No. 10-1428160 (2014. 08. 01.)

Republic of Korea Patent Publication No. 10-1452327 (2014. 10. 13.)

Republic of Korea Patent Publication No. 10-0537247 (2005. 12. 09.)

Republic of Korea Patent Publication No. 10-1218976 (2012. 12. 29.)

Republic of Korea Patent Publication No. 10-1466836 (2014. 11. 24.)

Republic of Korea Patent Publication No. 10-1363270 (2014. 02. 07.)

Republic of Korea Patent Publication No. 10-1391723 (2014. 04. 28.)

Republic of Korea Patent Publication No. 10-1041592 (2011. 06. 08.)

Republic of Korea Patent Publication No. 10-1294219 (2013. 08. 01.)

Republic of Korea Patent Publication No. 10-1347788 (2013. 12. 27.)

Republic of Korea Utility Model Registration Publication No. 20-0314598 (2003. 05. 27.)

Embodiments of the present invention are to provide a gasification method and a gasification apparatus for generating syngas from waste, which can minimize the emission of environmentally harmful substances.

In addition, embodiments of the present invention are to provide a gasification method and a gasifier for producing syngas from waste, in which the pretreatment of the waste is simple.

In addition, embodiments of the present invention to provide a power generation system using a syngas generated from waste, which can minimize the emission of environmentally harmful substances.

However, the technical problem to be achieved by the present invention is not limited to the above-mentioned problem, another task that is not mentioned will be clearly understood by those skilled in the art from the following description.

According to one aspect of the invention, a first pyrolysis step for generating char from the waste; And a second pyrolysis step of gasifying a car produced in the first pyrolysis step and a product other than the car, wherein the temperature at which the second pyrolysis step is carried out begins to decompose at least one of dioxins and tars. Provided is a gasification method for generating syngas from waste that is at or above a temperature.

The first pyrolysis step may be performed under a temperature range of 300 to 900 ° C and atmospheric pressure.

The gasification method for generating a synthesis gas from the waste, the step of cooling the car produced in the first pyrolysis step, when the first pyrolysis step is performed in a temperature range of 300 ~ 400 ℃; And a grinding step of grinding the tea.

The size of the crushed tea may be 50 ㎛ ~ 5 mm.

The first pyrolysis step may be performed in a fixed bed pyrolysis method.

The second pyrolysis step may be performed in a fractionation layer pyrolysis method in a temperature range of 900 ~ 2500 ℃.

The second pyrolysis step may be performed by a microwave steam plasma gasifier.

The method of generating syngas from the waste may further include supplying at least a portion of the syngas generated in the first pyrolysis step to the first pyrolysis step.

The gasification method of generating a synthesis gas from the waste may further include the step of rapidly cooling the product gas generated in the second pyrolysis step.

The rapid cooling step may be performed at 60 ° C or less.

Waste supplied to the first pyrolysis step may be magnetic screening and non-ferrous metal sorting.

According to another aspect of the invention, there is provided a pyrolysis gasifier for generating char from waste; A gasifier for producing syngas from waste is provided, comprising a char produced in the pyrolysis gasifier and a fractionation bed gasifier for gasifying other products except the char.

The pyrolysis gasifier may be a fixed bed type.

The fractionation layer gasifier may be a microwave steam plasma gasifier.

The fractionation layer gasifier may be integrated with the pyrolysis gasifier so that at least one of the gas and the char generated in the pyrolysis gasifier may be directly supplied to the fractionation layer gasifier.

According to another aspect of the present invention, there is provided a gasification apparatus for generating syngas from the waste; A gas engine supplied with the synthesis gas generated by the gasifier; A power generation system is provided that is connected to the gas engine and includes a generator for generating power.

According to another aspect of the invention, a first pyrolysis step for generating tea from waste; A gasification method for producing syngas from waste is provided, comprising a car produced in the first pyrolysis step, and a second pyrolysis step for gasifying a product other than the car in a fractionation bed manner.

The second pyrolysis step may be performed by a microwave steam plasma gasifier.

According to another aspect of the invention, a first pyrolysis step for generating tea from waste; And a second pyrolysis step of gasifying the car generated in the first pyrolysis step in a fractionation layer manner.

The gasification method for producing syngas from the waste includes a third pyrolysis step of pyrolyzing other products except for the cha, generated in the first pyrolysis step, wherein the temperature at which the third pyrolysis step is performed is dioxin and At least one of the tars may be above the temperature at which it begins to decompose.

1 is a schematic diagram of a gasification apparatus for generating syngas from waste and a power generation system including the same, according to an embodiment of the present invention;

2 is a flow chart illustrating a gasification method for generating syngas from waste, according to another embodiment of the present invention;

3 is a schematic diagram of a gasifier for producing syngas from waste, in accordance with a variant of the present invention;

4 is a graph showing the volume concentration of the gas produced over time when the char is gasified in a microwave steam plasma apparatus;

5 is a table relating to the properties and components of the waste test piece used in the experimental example of the present invention,

Figure 6 is a graph showing the composition of the synthesis gas produced over time when the pyrolysis temperature is 300 ℃ in the experimental example of the present invention as a volumetric concentration (%) (vollumetric concentration (%)),

7 is a graph showing the composition of the synthesis gas produced according to time when the pyrolysis temperature is 400 ℃ in the experimental example of the present invention in volumetric concentration,

8 is a graph showing the composition of the synthesis gas produced according to time when the pyrolysis temperature is 500 ℃ in the experimental example of the present invention in volumetric concentration,

9 is a graph showing the composition of the synthesis gas produced according to time when the pyrolysis temperature is 600 ℃ in the experimental example of the present invention in volumetric concentration,

10 is a graph showing the composition of the synthesis gas produced over time as a volume concentration when the pyrolysis temperature is 700 ℃ in the experimental example of the present invention,

11 is a graph showing the composition of the synthesis gas produced over time as the volume concentration when the pyrolysis temperature is 800 ℃ in the experimental example of the present invention,

12 is a graph showing the volume concentration of the generated CH ₄ gas with time when the pyrolysis temperature is 300, 400, 500, 600, 700, 800 ℃ in the experimental example of the present invention, respectively.

Hereinafter, specific embodiments of the present invention will be described with reference to the drawings. However, this is only an example and the present invention is not limited thereto.

In describing the present invention, when it is determined that the detailed description of the known technology related to the present invention may unnecessarily obscure the subject matter of the present invention, the detailed description thereof will be omitted. In addition, terms to be described below are terms defined in consideration of functions in the present invention, which may vary according to the intention or custom of a user or an operator. Therefore, the definition should be made based on the contents throughout the specification.

The technical spirit of the present invention is determined by the claims, and the following embodiments are merely means for efficiently explaining the technical spirit of the present invention to those skilled in the art.

Referring to FIG. 1, there is shown a schematic diagram of a gasifier 100 for generating syngas from waste, and a power generation system 1000 including the same, in accordance with one embodiment of the present invention.

As shown in FIG. 1, the gasifier 100 for generating syngas from waste according to an embodiment of the present invention is a pyrolysis gasifier for pyrolyzing waste W to generate char. 10, and a fractionation-bed gasifier 40 for receiving and gasifying a product produced from the pyrolysis gasifier 10 and a product including tar or dioxins other than the char, for example, a pyrolysis gasifier If the cha produced in (10) is not easily crushed (ie, broken easily even in a small impact or collision), the crusher 30 for crushing the tea may be further included.

According to the configuration as described above, according to an embodiment of the present invention, the gasifier 100 for producing syngas from the waste, pyrolysis gasifier 10 in the pyrolysis gasifier 10 to generate a car The powder can be crushed by a grinder or can be supplied to the fractionation layer gasifier 40 in an easily pulverized state, so that the syngas is discharged from the waste using the fractionation layer gasifier 40 without crushing the waste. In addition to production, dioxins and tars can be decomposed in the fractionation layer gasifier 40, thereby minimizing the emission of environmentally harmful substances.

The pyrolysis gasifier 10 may convert waste into a cha, for example under a temperature range of 300-900 ° C. and atmospheric pressure, and may be configured, for example, with a fixed bed pyrolysis gasifier. If the pyrolysis temperature is less than 300 ° C, not only the production of tea is difficult, but also the amount of syngas generated is very small, and if the pyrolysis temperature exceeds 900 ° C, the synthesis gas is generated for an excessively short time, which makes it difficult to use in subsequent processes. . Fixed bed pyrolysis gasifiers are disclosed, for example, in Korean Patent Publication Nos. 10-0537247, 10-1363270, 10-1391723, 10-1466836, 10-1452327, 10-1218976, and the like. It may have a configuration such as, but is not limited to this, it is possible to have a configuration necessary to generate a car from the waste, it can be operated under conditions such as temperature and pressure suitable for this.

In the reactor 15 of such a pyrolysis gasifier 10, the solid waste W is, for example, above the reactor 15 by the waste supply unit 20 that can pretreat the waste, which will be described later. Through the oxidant supply line 14, an oxidant such as, for example, air, oxygen or steam can be supplied, for example, in the same way as the waste W supply direction, or in the same or transverse direction. have. The waste W supplied into the reactor 15 can be maintained in the reaction zone by, for example, a grate 16 provided below the reactor 15. The temperature of the reactor 15 is initially raised by a starter burner (not shown), and during operation can be maintained by oxidizing syngas and tar produced by pyrolysis of waste with oxidant. The char generated from the waste W in the reactor 15 may pass through the grate 16 and move to the outlet 17 side disposed below the grate 16.

A funnel-shaped discharge part 17 is formed at the lower end of the pyrolysis gasifier 10, and thus, the car generated in the reactor 15 may be discharged to the outside of the pyrolysis gasifier 10. In addition, the discharge unit 17 may be provided with valves 18 and 19 to control the opening and closing of the discharge unit.

When the cha produced in the pyrolysis gasifier 10 is not easily crushed, the grinder 30 for crushing the cha is disposed below the outlet 17 of the pyrolysis gasifier 10, for example. Can be. By such an arrangement, the grinder 30 can be directly supplied with the car from the pyrolysis gasifier 10 without passing through a separate car moving means. The grinder 30 may grind the tea supplied from the pyrolysis gasifier 10 to have an average particle size of, for example, 50 μm to 10 mm, or to make an average particle size of 50 μm to 5 mm. In the case where the cha is pulverized in this way, it may be completely reacted in the fractionation layer gasifier 40 described later, for example, for a residence time of about 1 to 15 seconds, or about 2 to 5 seconds. The finely pulverized char as described above may be supplied to the fractionation layer gasifier 40 through the char supply line 31, for example.

In this way, the waste is converted into a cha easily pulverized, and the pulverized waste is fed to the chafing fractionation gasifier 40 in a finely divided state or easily pulverized. Not only is it possible to gasify, but it also saves the energy used to crush waste in the pretreatment stage.

In addition, products other than the char generated in the pyrolysis gasifier 10, such as syngas, tar and dioxins, may be supplied to the fractionation bed gasifier 40 via, for example, the product supply line 11. have. At this time, at least a portion of the syngas may be fed back into the reactor 15 via, for example, the return line 12, and by re-supplying such syngas into the reactor 15, By continuously changing the flow of the waste (W) it can increase the thermal decomposition rate or efficiency of the waste (W).

The fractionation layer gasifier 40 is capable of gasifying fine fuel of tens to hundreds of microns with an oxidizing agent, for example, into a high-temperature combustion zone of 1600 ° C. or higher, and is composed of, for example, a microwave steam plasma gasifier. Can be. The microwave steam plasma gasifier may include, for example, a configuration disclosed in Korean Patent Publication Nos. 10-1294219, 10-1316607, 10-1347788, and 10-1294219, but is not limited thereto. It is not. When the fractionation layer gasifier 40 is configured as a microwave steam plasma gasifier as described above, the fractionation layer gasifier 40 is connected to an electromagnetic wave oscillator (not shown) or an electromagnetic wave oscillator that is supplied with electric power to generate electromagnetic waves. A circulator (not shown) for outputting electromagnetic waves, a tuner (not shown) for inducing impedance matching by adjusting the intensity of incident and reflected waves of the electromagnetic waves output from the circulator, a waveguide (not shown) for transmitting electromagnetic waves from the tuner to the discharge tube, and It may include a discharge tube (not shown) for generating a plasma from the electromagnetic wave and auxiliary gas supplied from the waveguide. The plasma thus generated is, for example, a steam plasma flame of about 2000 ° C. or more, and for example, syngas can be generated by directly gasifying the pulverized char supplied through the cha feed line 31 by direct heating under atmospheric pressure ( Scheme 1).

(Scheme 1) CH + H ₂ O Plasma-> CO + H ₂

Referring to FIG. 4, a graph showing the change in volume concentration (%) over time of the gas produced by gasification of a differential, for example, petroleum cokes, into a microwave steam plasma gasifier (915 MHz). Is shown. As shown, the cha meets and reacts with the steam plasma to generate syngas, ie carbon monoxide and hydrogen.

In addition, since dioxin supplied through the product supply line 11 starts to decompose from about 850 ° C., and tar from about 850 ° C., for example, it may be decomposed by being exposed to a plasma flame of about 2000 ° C. or more for several seconds. have. Therefore, according to an embodiment of the present invention, the gasifier 100 for generating syngas from waste can generate syngas by pyrolysis gas waste while minimizing the environmentally harmful substances discharged.

In addition, according to an embodiment of the present invention, the gasifier 100 for producing a synthesis gas from the waste is generated and discharged from the fractionation layer gasifier 40, the synthesis gas, and dioxin and tar decomposed gas, etc. It may include a cooling unit 50 for cooling the product gas comprising a. The cooling unit 50 may include, for example, a configuration disclosed in Korean Utility Model Publication No. 20-0314598, and the like, but is not limited thereto, and may suppress a DE-NOVO phenomenon. It is possible if the exhaust gas can be cooled so that it can At this time, the cooling unit 50 can suppress the recombination of decomposed dioxins and tars by rapidly cooling the generated gas discharged from the fractionation layer gasifier 40 to a temperature of, for example, 60 ° C. or less.

Thus produced syngas is passed through, for example, a wet scrubber (not shown), and through this process, dust and ash, which are rotten in the syngas, can be removed and purified.

In addition, in the above description, the pulverizer 30 is directly connected to the lower end of the pyrolysis gasifier 10, but is not limited thereto. As described below, cooling the product generated from the pyrolysis gasifier 10 is performed. If necessary, that is, when the pyrolysis temperature of the pyrolysis gasifier 10 is 300 to 400 ° C., a cooling device (not shown) for cooling the product generated from the pyrolysis gasifier 10 is provided. It may be provided between the lower end and the grinder 30.

Power generation system 1000 according to another embodiment of the present invention, as described above, the gas engine 60 is driven by receiving the synthesis gas generated in the gasifier 100 for generating a synthesis gas from waste, And a generator (not shown) connected to the gas engine 60 to produce electric power. In addition, the power generation system 1000 includes a steam generator (not shown) capable of converting water into high-temperature, high-pressure steam by using high-temperature combustion gas generated from the gas engine 60, and power generation using the steam. It may also include a turbine (not shown).

With reference to FIG. 2, a flow diagram illustrating a gasification method for generating syngas from waste, according to another embodiment of the present invention, is shown. As shown in FIG. 2, a gasification method for producing syngas from waste according to another embodiment of the present invention includes a first pyrolysis step (S3) for converting the waste into a char; And a second pyrolysis step (S5) which is carried out in a temperature range for converting the car into a syngas and decomposing at least one of dioxins or tars produced in the first pyrolysis step (S3), for example When the tea generated in the first pyrolysis step S3 is not easily crushed, the tea crushing step S4-1 may be further included for crushing the tea.

According to the method as described above, the car produced by converting the waste in the first pyrolysis step S3 is easily crushed or crushed (S4-1) and supplied to the second pyrolysis step S5. Since it is converted into syngas, the gasification of the tea can be performed smoothly in the second pyrolysis step (S5) (see Scheme 1), and the emission of environmentally harmful substances is not only small, but also the generation of tar and dioxins can be decomposed. It is possible to gasify the waste while minimizing this.

The first pyrolysis step (S3) for converting the waste to char may be carried out, for example, under a temperature range of 300 to 900 ° C. and under atmospheric pressure. In the first pyrolysis step (S3), for example, the temperature of the reactor 15 of the pyrolysis gasifier 10 is initially increased by using a starter burner, and the waste W is introduced to synthesize the waste W as it is pyrolyzed. Reactor 15 temperature can be maintained by oxidizing with gas or tar, for example, with air or oxygen. The chemical reaction (exothermic reaction) that occurs at this time is as follows.

Scheme 2 C + O _2- > -394 KJ / mol

(Scheme 3) CO + 1/2 O _2- > -283 KJ / mol

(Scheme 4) H ₂ + 1/2 O _2- > -242 KJ / mol

Scheme 5 CH ₄ + 2 O _2- > -803 KJ / mol

In addition, the first pyrolysis step S3 may be performed in a fixed bed manner in which wastes supplied to the pyrolysis gasifier 10 are accumulated therein. In this case, since the waste can be supplied into the reactor 15 in a large particle size or a dump state without being crushed and pyrolyzed, the pretreatment process described later can be simplified.

That is, when the waste supplied to the first pyrolysis step S3 is received (S1), firstly, through the magnetic screening and the non-ferrous metal sorting step (S2), in this step, the waste steel (magnetic) in the waste is, for example For example, it may be selectively removed by an electromagnet of about 5,000 Gauss, and metal material waste (such as aluminum cans) having no magnetism may be selectively removed using, for example, an eddy current separator. Therefore, breakage or failure of the grinder 30 due to the metal can be prevented in the grinding step S4-1 of the below-mentioned car.

According to such a pretreatment step that can be carried out in the waste supply unit 20, the gasification method according to another embodiment of the present invention, the shredding of the waste, vibrating screen screening for sorting the shredded waste of a predetermined particle size, and It does not require a step such as drying to remove the moisture of the waste, and can be supplied to the first pyrolysis step (S3) of the fixed bed type only by magnetic screening and non-ferrous metal screening (S2), which is considerably compared to the conventional pretreatment step. It can be simplified, and thus the effect of increasing the amount of waste that can be treated per hour and saving energy can be obtained.

Next, the tea produced in the first pyrolysis step S1 may go through the tea grinding step S4-1, for example, when the tea is not easily crushed. In this step, the cha is ground to have an average particle size of about 50 μm to 5 mm, so that the second pyrolysis step (S5) described below, in particular about 2 to 5 in a fractionation layer gasification method such as in a microwave steam plasma gasifier It can react completely during the residence time of seconds. In addition, the cha can be easily crushed compared to the waste, thereby saving energy, cost and time compared to crushing the waste.

On the other hand, as will be described later, when the pyrolysis temperature of the first pyrolysis step (S3) is 300 ~ 400 ℃, the state of the product may be a liquid of the same properties as asphalt, in this case, such a product is naturally cooled or rapidly When cooled, it can be ground in micro units.

In addition, a product including syngas, tar, dioxins, and the like, produced in the first pyrolysis step S1 is supplied to the second pyrolysis step S5 through, for example, the product supply line 11 (S4-). 2). At this time, at least a part of the synthesis gas, for example, may be supplied back to the first pyrolysis step (S3) through the return line 12, by the re-supply of the synthesis gas, in the case of a fixed bed type reactor ( 15) The wastes in the stream can be continuously flowed to increase the thermal decomposition efficiency or speed of the wastes.

The second pyrolysis step (S5) is a process for converting the tea in a easily crushed state or converting the crushed tea into syngas and decomposing at least one of tar and dioxin, for example, 900 to 2,500 ° C. Can be carried out under a temperature range of and atmospheric pressure. Since dioxin starts to decompose from 850 ° C. and tar also begins to decompose from 850 ° C., dioxin and tar can be decomposed and removed in this temperature range. The second pyrolysis step (S5) can also be carried out in a fractionated bed manner, for example in a microwave steam plasma gasifier, in which case the plasma flame can be, for example, 2000 ° C. or higher, so that dioxin Staying for a few seconds can break down and tar can break down.

Further, in the second pyrolysis step S5, the micronized char is fed in a fractionation bed manner, for example in a microwave steam plasma gasifier under atmospheric pressure, for example a short residence time of 2-5 seconds, for example 2000 Directly heated by a plasma flame of < RTI ID = 0.0 > In this case, the micronized tea may react directly with at least one of an oxidizing agent, for example, oxygen, air, and steam, and by controlling the amount of the oxidizing agent, all reactions may be completed within a maximum of 5 seconds, and the amount of dioxins generated Can be significantly reduced.

According to the configuration as described above, the second pyrolysis step (S5) can reduce the amount of dioxins generated, even if dioxin is generated is decomposed by the high temperature, and also the tar and dioxins produced in the first pyrolysis step (S3) Since it can be decomposed by the high temperature of the second pyrolysis step (S5), the waste gasification method according to the present invention can gasify the waste while minimizing the emission of environmentally harmful substances.

Next, the product gas including the syngas generated in the second pyrolysis step S5 may undergo a rapid cooling step S6, whereby the decomposed dioxins and tar contained in the product gas recombine. Can be suppressed.

Next, the rapidly cooled product gas may go through a purification step S7 such as, for example, passing through a wet scrubber, in which dust or ash in the product gas is removed to be located downstream, It is possible to reduce the failure, shorten the life of the gas engine 60 using the synthesis gas.

Thus, the purified synthesis gas is supplied to the gas engine 60, for example, to drive the gas engine 60, so that electricity can be generated in the generator connected to the gas engine 60, and the gas engine ( By generating a steam at a high temperature generated in 60) it is possible to generate electricity by rotating a turbine (not shown) (S8).

In the above description, in the case of the gasifier 100 for producing syngas from the waste, according to one embodiment of the present invention, the car produced in the pyrolysis gasifier 10, and the product except the cha Although described as being supplied to the fractionation layer gasifier 40 through the 31 and the product supply line 11, the pyrolysis gasifier 10 and the fractionation layer gasifier 40 are not limited thereto. And at least one of the products other than the tea may be integrated with each other so that the products may be directly supplied without passing through the tea supply line 31 or the product supply line 11. For example, referring to FIG. 3, there is shown a diagram of a gasifier 100a for generating syngas from waste, according to one variation of the present invention. For simplicity of explanation, the following description will focus on differences from the gasifier 100 for generating syngas from waste, according to an embodiment of the present invention.

As shown in FIG. 3, according to a modification of the present invention, the gasifier 100a for generating syngas from waste is connected to a lower end through a connection part 34 on an upper side of the pyrolysis gasifier 10a. A storage tank 33 may be provided on the cha supply line 31 for supplying the fractionated bed gasifier 40a and supplying the pulverized car to the fractionated bed gasifier 40a. Can be. Synthetic gas exiting the discharge line 41 of the fractionation layer gasifier 40a may be supplied to the cooling unit 50 as illustrated in FIG. 1. In addition, waste may be supplied into the reactor 15 of the pyrolysis gasifier 10a through the waste supply 20 as shown in FIG.

According to such a structure, the synthesis gas (G) produced by the pyrolysis gasifier 10, such as dioxin and tar, is not supplied through the separate product supply line 11, but through the connection part 34. It can be supplied directly to the lower portion of the fractionation layer gasifier 40a, so that the configuration can be simplified. Moreover, the storage tank 33 is arrange | positioned on the cha supply line 31, and it is possible to stably supply the crushed cha to the fractionation layer gasifier 40a at a fixed level.

In addition, the integration of the pyrolysis gasifier 10a and the fractionation layer gasifier 40 is not limited thereto, and the fractionation layer gasifier 40 may be connected to, for example, a lower end or a side surface of the pyrolysis gasifier 10a. Can be. At this time, the crusher 30 is not necessarily disposed between the pyrolysis gasifier 10a and the fractionation layer gasifier 40. That is, the char discharged from the pyrolysis gasifier 10a may be directly supplied to the fractionation layer gasifier 40 without passing through the grinder 30.

Further, in the above-described embodiments and modifications of the present invention, a product containing dioxins, tars, and the like produced in the first pyrolysis step S3 or the pyrolysis gasifier 10; Although described as being supplied to the second pyrolysis step (S5) or fractionation bed gasifier (40; 40a), it is not limited thereto, and is only supplied to the second pyrolysis step (S5) or fractionation bed gasifier (40; 40a) It is also possible to supply other products, except for the char, to be supplied to a separate pyrolysis step or a pyrolysis device to decompose dioxins and tars contained in the product.

Experimental Example

In connection with the first pyrolysis performed in the first pyrolysis step (S3) of the gasification method for producing syngas from the waste according to an embodiment of the present invention, the waste was pyrolyzed under the following conditions, the results are shown in Table It is summarized in 1.

Experimental conditions

(1) Waste: Samples of household garbage from Yanggu County Office (see Fig. 5 for properties and composition)

(2) sample weight: 130 g

(3) Pyrolysis temperature: 300, 400, 500, 600, 700, 800 ℃

(4) pyrolysis heating time: 30 ~ 60 minutes

(5) Inert gas: N2_20 lpm (not used in case of 300 ℃)

(6) pressure: atmospheric pressure

6 to 11 are graphs showing the volume of the composition of the synthesis gas generated according to the reaction time when the pyrolysis temperature is 300, 400, 500, 600, 700, and 800 ° C., respectively.

As shown in FIG. 6, when the pyrolysis temperature was 300 ° C., there was almost no change in gas composition for 60 minutes, and a small amount of syngas was generated.

As shown in FIG. 7, when the pyrolysis temperature is 400 ° C., CH ₄ slightly increased over time for 30 minutes, and the amount of syngas generated was small.

As shown in FIG. 8, when the pyrolysis temperature is 500 ° C., as time passes for 30 minutes, the generation amount of CH ₄ is greatly increased, and the production amount of the synthesis gas is also increased.

As shown in FIG. 9, when the pyrolysis temperature is 600 ° C., CH ₄ is generated at a constant level for a certain time, and the amount of syngas produced is also large.

As shown in FIG. 10, when the pyrolysis temperature is 700 ° C., CH ₄ was generated at a higher constant concentration for a shorter time than in the case of 600 ° C., the reaction was completed more quickly, and the amount of syngas produced was also large. It was.

As shown in FIG. 11, when the pyrolysis temperature is 800 ° C., the reaction is started after about 30 seconds and pyrolysis is completed in about 10 minutes. During this time, CH ₄ is intensively generated and the amount of H ₂ is also increased. It became.

In addition, FIG. 12 is a graph showing the volume concentration (%) of CH ₄ according to temperature according to time in the above-described experiment. When the pyrolysis temperature is 600 ° C., CH ₄ is generated at a constant level for a certain time, and thus, stably. Supply to gas engines is possible. In addition, in FIG. 12, it can be seen that, even when the pyrolysis temperature is 900 ° C., the generation of the car and the generation of syngas are possible through the change in the graph form as the pyrolysis temperature is changed from a low temperature to a high temperature.

As described above, the present invention has been described with reference to the embodiments, but it is possible to make other various modifications other than the above-described modifications without departing from the technical spirit of the present invention. It will be apparent to those who have it.

In addition, the substitution or modification of the components shown in the present invention to the technical elements that perform a known similar function will be apparent to those skilled in the art, or belong to the common sense.

Therefore, the technical scope of the present invention to the scope of the claims should not be limited to the described embodiments, but extends to the spirit and equivalents shown in the claims below.

[Description of the code]

10; 10a: pyrolysis gasifier

11: product feed line

12: return line

14: oxidant supply line

15: reactor

16: great

17: discharge part

18: valve

19: valve

20: waste supply unit

30: grinder

31: tea supply line

40: fractionation layer gasifier

50: cooling unit

60 gas engine

100; 100a: gasifier

1000: Power Generation System

Claims (20)

1. A first pyrolysis step for producing char from the waste; And

   A second pyrolysis step of gasifying a tea produced in the first pyrolysis step and a product other than the tea,

   Wherein the temperature at which the second pyrolysis step is carried out is at least the temperature at which any of dioxin and tar begins to decompose, thereby producing syngas from the waste.
2. The method according to claim 1,

   The first pyrolysis step is a gasification method for producing syngas from waste, which is performed under a temperature range of 300 to 900 ° C. and atmospheric pressure.
3. The method according to claim 2,

   Gasification method for generating a synthesis gas from the waste,

   When the first pyrolysis step is performed at a temperature in the range of 300 to 400 ° C., cooling the tea produced in the first pyrolysis step; And

   And a pulverizing step of pulverizing the cha, the gasification method for producing syngas from the waste.
4. The method according to claim 3,

   The size of the pulverized car is 50㎛ ~ 5mm, gasification method for producing a synthesis gas from the waste.
5. The method according to claim 1,

   Wherein said first pyrolysis step is carried out in a fixed bed pyrolysis manner.
6. The method according to any one of claims 1 to 5,

   The second pyrolysis step is a gasification method for producing syngas from waste, which is carried out in a fractionation bed pyrolysis method in the temperature range of 900 ~ 2500 ℃.
7. The method according to claim 6,

   Wherein said second pyrolysis step is performed by a microwave steam plasma gasifier.
8. The method according to claim 1,

   The method for generating syngas from the waste,

   And supplying at least a portion of the syngas produced in the first pyrolysis step back to the first pyrolysis step.
9. The method according to claim 1,

   Gasification method for generating a synthesis gas from the waste,

   And rapidly cooling the product gas produced in the second pyrolysis step, the gasification method of producing syngas from the waste.
10. The method according to claim 9,

    The rapid cooling step is carried out at 60 ℃ or less, the gasification method for producing syngas from the waste.
11. The method according to claim 1,

    Waste that is supplied to the first pyrolysis step is magnetic screening and non-ferrous metal sorting, the gasification method for producing syngas from the waste.
12. Pyrolysis gasifiers for producing char from waste;

    And a fractionation bed gasifier for gasifying the product produced in the pyrolysis gasifier and other products except the cha.
13. The method according to claim 12,

    The pyrolysis gasifier is a fixed bed type, gasifier for producing syngas from waste.
14. The method according to claim 12,

    The fractionation layer gasifier is a microwave steam plasma gasifier, a gasifier for producing syngas from waste.
15. The method according to claim 12,

    The fractionation layer gasifier is integrated with the pyrolysis gasifier so that at least one of the gas and the char generated in the pyrolysis gasifier can be directly supplied to the fractionation layer gasifier, a gasifier for producing syngas from the waste. .
16. A gasifier for producing syngas from waste according to claim 12;

    A gas engine supplied with the synthesis gas generated by the gasifier;

    A generator coupled to the gas engine and including a generator for generating electricity.
17. A first pyrolysis step for producing tea from the waste;

    And a second pyrolysis step of gasifying the car produced in the first pyrolysis step and a product except the car in a fractionation layer manner.
18. The method according to claim 17,

    Wherein said second pyrolysis step is performed by a microwave steam plasma gasifier.
19. A first pyrolysis step for producing tea from the waste; And

    And a second pyrolysis step of gasifying the car generated in the first pyrolysis step in a fractionation layer manner.
20. The method according to claim 19,

    Gasification method for generating a synthesis gas from the waste,

    A third pyrolysis step of pyrolyzing other products except for the tea produced in the first pyrolysis step,

    And the temperature at which the third pyrolysis step is carried out is at least a temperature at least one of dioxin and tar begins to decompose, thereby producing syngas from the waste.

Images