KR101738168B1

KR101738168B1 - Integrated Gasification Apparatus for Carbonaceous Fuel

Info

Publication number: KR101738168B1
Application number: KR1020100117621A
Authority: KR
Inventors: 박삼룡; 김규태; 김주회; 방진환; 이민회; 김용전; 오경석; 김민경
Original assignee: 에스케이이노베이션 주식회사
Priority date: 2010-11-24
Filing date: 2010-11-24
Publication date: 2017-05-22
Also published as: KR20120056091A

Abstract

The present invention relates to a carbon fuel gasification complex plant, which comprises a reactor for producing a synthesis gas, a carbon fuel containing water and the synthesis gas produced in the reactor, and the water content of the carbon fuel and the synthesis gas A separator for separating the synthesis gas from the carbon fuel discharged from the dryer and supplying the reduced carbon fuel to the reactor and supplying the reduced syngas to the purifier; The syngas produced in the reactor can be circulated and mixed with the carbon fuel containing water even if a separate heat exchanger is not employed, so that cooling of the syngas and drying of the carbon fuel can be simultaneously achieved.

Description

TECHNICAL FIELD [0001] The present invention relates to an integrated gasification apparatus for carbonaceous fuel,

The present invention relates to a carbon fuel gasification complex plant.

Gasification is a very old, classical technology that produces combustible gas fuels from solid fuels, but it is still a field of development. The history of fuel used by humans has changed from trees that are still used for cooking or heating to coal, gas, oil, electricity, and so on.

Industrial use of carbon fuels (commonly referred to as coal, classified as bituminous coal, bituminous coal, lignite, and anthracite) dates back to the Industrial Revolution of the late 18th century. At that time, it started to be used as a substitute for coke as charcoal as a reducing agent for the metal industry, or as a city gas. A combustible gas fuel, a gasification product of carbon fuels, is called a synthesis gas, which means that it is an artificially produced gas, not a natural gas buried naturally on earth. Syngas began to be used in urban street lamps, gradually replacing solid fuels, or expanding to produce chemical raw materials. Recently, it has been used for power generation and synthetic fuel production.

Such carbon-fuel gasification is a process in which a carbon fuel generates a synthesis gas, which is mainly composed of hydrogen and carbon monoxide, by oxidation reaction with an oxidizing agent supplied into the reactor and oxidation / reduction reaction with a gas such as carbon dioxide, will be.

The synthetic gas thus produced can be used as a high temperature gas for coal gasification combined cycle power generation (IGCC) or Fischer-Tropsch process. In order to apply this technology, a heat exchanger for cooling a high- .

Conventionally, a separate large-capacity heat exchanger is employed in the gasification combined facility to cool the high-temperature syngas produced in the reactor, resulting in an increase in the size of the gasification combined facility and an increase in equipment cost.

The present invention has been made to solve the above-mentioned problems, and it is an object of the present invention to provide a method of cooling a syngas and a carbon fuel by mixing a syngas produced in a reactor with a carbon fuel containing high water content without employing a separate heat exchanger The present invention has been made in view of the above problems.

The apparatus also includes a flow distributor, further comprising a small-capacity heat exchanger for preliminarily cooling the synthesis gas produced in the reactor and selectively discharging the syngas produced in the reactor, The cooling of the syngas can be efficiently achieved.

The present invention relates to a carbon fuel gasification complex plant, which comprises a reactor for producing a synthesis gas, a carbon fuel containing water and the synthesis gas produced in the reactor, and the water content of the carbon fuel and the synthesis gas A separator for separating the synthesis gas from the carbon fuel discharged from the dryer and supplying the reduced carbon fuel to the reactor and supplying the reduced syngas to the purifier; .

Further, the present invention is characterized in that the water content of the carbon fuel introduced into the dryer is 20 wt% to 60 wt%.

Further, the present invention is characterized in that the temperature range of the synthesis gas supplied to the dryer is 500 ° C to 950 ° C.

Further, the present invention is characterized in that the particle size of the carbon fuel flowing into the dryer is 2 mm or less.

Further, the present invention is characterized in that the pressure range of the synthesis gas introduced into the dryer is 1 to 50 atmospheres.

Further, the present invention is characterized in that the moisture content of the carbon fuel discharged from the dryer is 1 wt% to 10 wt%.

Further, the present invention is characterized in that the temperature range of the syngas discharged from the dryer is 150 ° C to 300 ° C.

Also, the dryer of the present invention employs an air stream dryer, wherein the carbon fuel and the synthesis gas are supplied to the lower side of the air stream dryer and then heat-exchanged and discharged to the upper side.

In addition, the dryer of the present invention employs an air flow dryer, and the carbon fuel and the synthesis gas are supplied to the upper side of the air flow dryer and then discharged to the lower side through heat exchange.

The present invention further includes a preliminary heat exchanger disposed between the reactor and the dryer for primarily cooling the syngas discharged from the reactor.

Further, the present invention further includes a flow distributor for distributing the syngas discharged from the preliminary heat exchanger to the dryer and the purifier.

The features and advantages of the present invention will become more apparent from the following detailed description based on the accompanying drawings.

Prior to that, terms and words used in the present specification and claims should not be construed in a conventional and dictionary sense, and the inventor may properly define the concept of the term in order to best explain its invention It should be construed as meaning and concept consistent with the technical idea of the present invention.

The carbon-dioxide gasification and mixing plant according to the present invention may include a heat exchanger for cooling the syngas at a high temperature, but may also be produced by circulating a high-temperature syngas and mixing it with carbon- Can be achieved at the same time.

In addition, the gasification complex equipment according to the present invention may include a small-capacity heat exchanger for preliminarily cooling the syngas flowing out from the reactor, so that the temperature of the syngas flowing into the dryer can be controlled.

And a flow distributor for supplying a portion of the syngas discharged from the reactor to the dryer and a portion of the syngas discharged from the reactor to the purifier so as to supply the syngas corresponding to the flow rate of the carbon fuel supplied to the dryer, The fueling rate can be adjusted.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic view showing a carbon fuel gasification and combined equipment according to a first preferred embodiment of the present invention; FIG.
FIG. 2 is a schematic view showing a modification of the carbon-dioxide gasification combined plant shown in FIG. 1; FIG.
FIG. 3 is a schematic view showing a carbon dioxide gasification combined facility according to a second preferred embodiment of the present invention.
FIG. 4 is a schematic view showing a modification of the carbon-dioxide gasification combined plant shown in FIG. 3; FIG.

BRIEF DESCRIPTION OF THE DRAWINGS The objectives, specific advantages and novel features of the present invention will become more apparent from the following detailed description taken in conjunction with the accompanying drawings, in which: FIG. It should be noted that, in the present specification, the reference numerals are added to the constituent elements of the drawings, and the same constituent elements are assigned the same number as much as possible even if they are displayed on different drawings. In the following description, well-known functions or constructions are not described in detail since they would obscure the invention in unnecessary detail.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

The gasification and mixing plant according to the present invention comprises a dryer in which a carbon fuel and a syngas are introduced without forming a separate heat exchanger to lower the temperature of the synthesis gas discharged from the reactor, The synthesis gas can be cooled and the carbon fuel can be dried.

At this time, the gasification combined equipment according to the present invention may be configured such that the moisture content of the carbon fuel discharged from the dryer is in the range of 1 wt% to 10 wt%, and the temperature of the syngas discharged from the dryer is in the range of 150 to 300 ° C . &Lt; / RTI > Hereinafter, a gasification combined equipment according to a preferred embodiment of the present invention will be described in detail with reference to FIGS. 1 to 4. FIG.

FIG. 1 is a schematic view showing a carbon fuel gasification combined facility according to a first preferred embodiment of the present invention, and FIG. 2 is a schematic view showing a modified example of the carbonaceous gasification combined facility shown in FIG. 1 FIG.

In the present specification, the carbonaceous fuel is a raw material for coal, and includes bituminous coal, bituminous coal, lignite, etc., except anthracite, which is low in volatile matter.

The gasification and mixing plant 1000 according to the present embodiment includes a reactor 100, a dryer 200, a separator 300, and a purifier 400. The components are connected through a connecting means for moving the fluid, such as a pipe, to discharge or supply syngas or carbon fuel.

Reactor 100 produces synthesis gas through a gasification process using carbon fuel. Gasification refers to reforming of carbon fuel into fuel gas, and refers to the process of producing synthesis gas by reforming carbon fuel and steam using combustion heat of carbon fuel. The synthesis gas includes hydrogen, carbon monoxide, carbon dioxide, nitrogen, water vapor, methane and the like, and the material accounts for about 95% by weight of the synthesis gas.

The syngas discharged from the reactor 100 is introduced into a gas turbine or the like to be used for power generation such as coal gasification combined cycle power generation technology (IGCC) or Fischer-Tropsch for producing liquid hydrocarbons from synthesis gas on Fe or Co catalyst, Tropsch) process.

The syngas produced in the reactor 100 is discharged at a pressure of 1 atm to 50 atm with a hot gas at a temperature in the range of 800 ° C to 980 ° C.

The temperature range and the pressure range of the syngas discharged from the reactor can be varied within the above range depending on the type and capacity of the gasifier which can be employed in the reactor included in the present invention. The gasification may be employed in any known range, including a fractionation bed gasifier, a fast fluidized bed gasifier.

The dryer 200 is discharged after the carbon fuel containing moisture and the synthesis gas generated from the reactor 100 are introduced into the dryer 200. In this process, the heat exchange occurs to reduce the moisture content of the carbon and the temperature of the synthesis gas.

The syngas flowing into the dryer 200 has a lower temperature range than immediately after being discharged from the reactor 100. The syngas flowing into the dryer 200 has a temperature ranging from 500 ° C to 950 ° C. After the synthesis gas is discharged from the reactor 100, it is naturally cooled, or the synthesis gas is preliminarily cooled through a small heat exchanger To have the temperature in the above range.

The carbon fuel containing moisture introduced into the dryer 200 is mixed with the high-temperature syngas to perform heat exchange with the syngas to reduce the temperature of the syngas, and the dried carbon fuel is supplied to the reactor 100 And is used as a raw material for synthesis gas.

At this time, the water content of the carbon fuel flowing into the dryer 200 is preferably 20 wt% to 60 wt%. If the moisture content is less than the above range, the cooling efficiency of the syngas is lowered. If the moisture content is above the above range, the water content of the carbon fuel flowing into the reactor 100 is high.

The particle size of the carbon fuel flowing into the dryer 100 is preferably 2 mm or less. When the particle size of the carbon fuel is large, the contact area with the syngas is small and the heat exchange between the syngas and the carbon fuel is not efficiently performed, so the cooling efficiency of the synthesis gas is low.

Therefore, the particle size of the carbon fuel is preferably 2 mm or less in order to increase the contact area between the carbon fuel and the syngas, and it is preferable that the carbon fuel is pulverized through a pulverizer (not shown) before the carbon fuel is introduced into the dryer 200 Lt; / RTI >

Although various types of dryers may be employed as the dryer 200, it is preferable that a flash dryer 200 is employed as shown in FIG.

When the air dryer 200 is employed, carbon fuel and syngas may be supplied to the lower side of the air dryer 200 and then discharged upward as shown in FIG.

For example, the carbon fuel flows into the lower side of the airflow dryer 200, and the high-temperature synthesis gas flows into the lower surface of the airflow dryer 200. At this time, the syngas and the carbon fuel move to the upper side of the dryer 200 by the pressure of the introduced synthesis gas, heat-exchanged and discharged.

In this case, when the carbon fuel having a particle size of 2 mm or less flows into the air flow dryer 200, even if the hydraulic pressure of the synthesis gas supplied to the dryer 200 is somewhat low, .

As shown in FIG. 2, the gasification and mixing plant 1000 'employs an airflow dryer 200, in which carbon fuel and syngas are supplied to the upper side of the airflow dryer 200 and discharged downward.

For example, the carbon fuel flows into the upper side of the air flow dryer 200, and the high-temperature synthesis gas flows into the upper side of the dryer 200.

A simple flow path (for example, a pipe) design is provided between the reactor 100 and the air dryer 200 by introducing the syngas into the upper side of the air flow dryer 200 when the synthesis gas is discharged to the upper end of the reactor 100 And it is advantageous that the manufacturing cost of the gasification combined equipment is reduced and the space utilization is improved.

As described above, the gasification combined equipment according to the present invention is characterized in that a carbon fuel containing a large amount of moisture and a high-temperature syngas are introduced into the dryer 200, so that it is not necessary to provide a heat exchanger of a large capacity for cooling a high- can do. Further, there is no need to add a separate dryer for controlling the moisture of the carbon fuel supplied to the reactor, which simplifies the facility and reduces the equipment cost.

In the gasification complex system according to the present invention, the syngas discharged from the dryer 200 is heated to a temperature ranging from 150 to 300 ° C to improve efficiency in a subsequent process using a synthesis gas such as a Fischer-Tropsch process .

The carbon fuel discharged from the dryer 200 may preferably have a water content of 1 wt% to 10 wt% in order to improve the production efficiency of the synthesis gas in the reactor 100.

The temperature of the syngas discharged through the dryer 200 and the moisture content of the carbon fuel (hereinafter, the drying performance of the dryer) are determined by the temperature and pressure of the synthesis gas flowing into the dryer 200, the initial moisture content and particle size of the carbon fuel, The syngas flowing into the dryer 200 and the carbon fuel are mixed with the synthetic gas flowing into the dryer 200 and the carbon fuel, The weight ratio of the fuel is in the range of 1: 1 to 1:30 (when the syngas introduced into the dryer is in the temperature range of 500 to 950 캜 and the water content of the carbon fuel flowing into the dryer is 20 to 60 wt% ).

1 and 2, carbon fuel having an average particle size of 350 mu m and an initial moisture content of 28 wt% was introduced into the dryer 200, and the carbon fuel produced in the reactor 100 When the syngas at 950 ° C is introduced into the dryer 200 at a pressure of 7.2 atm (the mixing weight ratio of carbon fuel to syngas is in the range of 1: 5 to 1:20), the temperature of the synthesis gas discharged from the dryer is 270 ° C, The moisture content of the hydrocarbons ranged from 1 wt% to 5 wt%.

The carbon fuel and the synthesis gas discharged through the dryer 200 flow into the separator 300. Since the carbon fuel and the syngas are discharged in a mixed state, the separator 300 separates the carbon fuel and the cooled syngas to supply the carbon fuel to the reactor 100, and supplies the syngas to the purifier 400. Such a separator 300 may employ a cyclone.

The purifier 400 purifies the syngas supplied from the separator 300. The syngas cooled through the heat exchange in the separator 300 may contain foreign substances such as fine powders, sulfur compounds and the like. Accordingly, a syngas purification process is required to use syngas produced in the gasification combined facilities (1000, 1000 ') as a fuel gas.

The purifier 400 may be constituted by a ceramic filter for removing particles in the form of particles such as fine powder, tar, wax, or may be constituted by a water washing device or a desulfurizing device. The water scrubber has the effect of removing water vapor contained in the syngas, and the desulfurizer removes sulfur compounds or nitrogen compounds.

The gasification complex facilities 1000 and 1000 'according to such processes are supplied with synthetic gas from which the foreign substances have been removed through the purifier 400 to the coal gasification combined power generation technology (IGCC) and the Fischer-Tropsch process do.

FIG. 3 is a schematic view showing a carbon fuel gasification and mixing plant according to a second preferred embodiment of the present invention, and FIG. 4 is a view schematically showing a modified example of the carbon fuel gasification and mixing plant shown in FIG. 3 FIG. Hereinafter, a carbon dioxide gasification and complex equipment (hereinafter referred to as a gasification complex equipment) according to the present embodiment will be described with reference to these. However, detailed description of the same components as those described with reference to FIG. 1 will be omitted.

The gasification complex equipment 2000 according to the present embodiment further includes a preliminary heat exchanger 500 for preliminarily cooling the high-temperature syngas discharged from the reactor 100 and supplying it to the dryer 200.

The syngas discharged from the reactor 100 has a temperature ranging from 800 ° C. to 980 ° C. Since it is desirable that the syngas flowing into the dryer 200 has a temperature range of 500 ° C. to 950 ° C., the preheat heat exchanger 600 RTI ID = 0.0 > preliminarily < / RTI >

Unlike the conventional gasification complex equipment, which requires a large-capacity heat exchanger to lower the synthesis gas discharged from the reactor to a temperature range of 150 to 300 ° C, the gasification complex facility 2000 according to the present invention is capable of preliminarily Since a heat exchanger is used for cooling, a small-capacity heat exchanger is employed.

3, the pre-cooled syngas and the carbon fuel flow into the upper side of the airflow dryer 200, but the present invention is not limited thereto, and may be introduced into the lower side of the airflow dryer 200 as shown in FIG. 1, Other dryers may be employed.

4 further includes a flow distributor 600 for distributing and supplying the syngas discharged from the preliminary heat exchanger 500 to the dryer 200 and the purifier 400. 4 illustrates an example of a gasification combined facility in which a syngas and carbon fuel flow into a lower portion of an airflow dryer 200, as in FIG.

The flow distributor 600 includes a connecting pipe having one inlet and two outlets and a flow control valve for regulating the flow rate of the mixed gas discharged to the two outlets.

The gasification complex plant 2000 'further comprising a flow distributor 600 has the advantage that it is possible to feed a syngas at a flow rate suitable for the carbon fuel flow rate to the dryer 200. The moisture content of the carbon fuel supplied to the reactor 100 can be determined by preventing the excessive amount of the synthesis gas from being supplied to the carbon fuel supplied to the dryer 200.

On the other hand, the remaining mixed gas that is not supplied to the dryer 200 is supplied to the purifier 400. The remaining mixed gas is removed from the purifier together with the mixed gas discharged from the separator, such as fine particles, sulfur compounds and the like.

3 and 4, it was found that carbon fuel having an average particle size of 1000 mu m and an initial moisture content of 38 wt% flows into the dryer 200, and the carbon fuel produced in the reactor 100 The temperature of the synthesis gas discharged from the dryer 200 is 250 DEG C when the synthesis gas at 620 DEG C flows into the dryer 200 at a rate of 5.9 atm (the mixing weight ratio of the synthesis gas is in the range of 1: 1 to 1:30) The water content of the hydrocarbons ranged from 5 wt% to 10 wt%.

Meanwhile, a simulation of a Fischer-Tropsch facility for producing liquefied hydrocarbons using the syngas supplied from the gasification complex plant and the gasification complex plant according to the present invention was performed to calculate the energy efficiency and the carbon dioxide emission amount .

In the case of adopting the gasification combined facility according to the present invention, the energy efficiency is improved by 8% to 12% and the carbon dioxide emission is reduced by 9% to 15% as compared with the gasification facility for cooling the syngas by using the conventional heat exchanger I could.

In the case of a gasification system for cooling a synthesis gas using a conventional heat exchanger, there is a problem that electric power is required to drive the heat exchanger when the synthesis gas is cooled by a water-cooling type or an air-cooling type,

The present invention reduces the power consumption by about 8% to 12% as compared with the conventional gasification equipment because the synthetic gas produced in the reactor is naturally cooled using the moisture of the carbon fuel by circulating the syngas produced in the reactor, % Reduction.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit and scope of the invention as defined in the appended claims. It is therefore intended that such variations and modifications fall within the scope of the appended claims.

1000, 1000 ', 2000, 2000': Gasification and compounding plant of carbon fuel
100: reactor 200: dryer
300: separator 400: purifier
500: reserve heat exchanger 600: flow distributor

Claims

A reactor for producing syngas;
Wherein a carbon fuel containing moisture in the range of 20 wt% to 60 wt% and the synthesis gas produced in the reactor are introduced, reducing the moisture content of the carbon fuel to a range of 1 wt% to 10 wt% To a temperature in the range of 150 캜 to 300 캜;
A separator for separating the carbon fuel discharged from the dryer and the synthesis gas to supply the carbon fuel having a reduced moisture content to the reactor and supplying the synthesized gas with reduced temperature to the purifier;
A preliminary heat exchanger disposed between the reactor and the dryer for controlling the temperature of the synthesis gas discharged from the reactor to a range of 500 ° C to 950 ° C; And
And a flow distributor for distributing the syngas discharged from the preliminary heat exchanger to the dryer and the purifier.

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The method according to claim 1,
And the particle size of the carbon fuel flowing into the dryer is 2 mm or less.

The method according to claim 1,
Wherein the pressure of the synthesis gas flowing into the dryer is in the range of 1 atmosphere to 50 atmospheres.

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The method according to claim 1,
Wherein the dryer is equipped with an air flow dryer and the carbon fuel and the synthesis gas are supplied to the lower side of the air flow dryer and then heat exchanged and discharged to the upper side.

The method according to claim 1,
Wherein the dryer is equipped with an air flow dryer and the carbon fuel and the syngas are supplied to the upper side of the air flow dryer and then discharged to the lower side through heat exchange.

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