KR101486965B1 - Multistage gasifying apparatus and method - Google Patents

Abstract

The present invention relates to a multistage gasifying apparatus and a method thereof, wherein the multistage gasifying apparatus comprises a pre-heating unit for separating moisture included in fuel; a first reactor for gasifying the fuel with moisture separated in the pre-heating unit by combustion; and a second reactor for reforming synthetic gas produced at the first reactor. The multistage gasifying apparatus has the effect of increasing the gasification efficiency by separating moisture included in fuel before the gasification, and supplying only fuel components with moisture removed from the first reactor so as to increase the reaction time and get involved in the gasification.

Description

[0001] MULTISTAGE GASIFYING APPARATUS AND METHOD [0002]

The present invention relates to a multistage gasification apparatus and method, and more particularly, to a multistage gasification apparatus and method for gasifying a low-grade oil such as bio-pyrolysis oil, waste cooking oil, waste lubricating oil, and colloid fuel (Coal Water Slurry).

The technology of gasifying or cracking liquid fuels into other types of fuels is a relatively long-standing technology in chemical processes.

In recent years, as the liquid fuel to be used is becoming more and more diversified, waste fuel such as waste cooking oil, bio-pyrolysis oil obtained by pyrolyzing biomass, and low-grade coal slurry are expanding the fuel.

When these fuels are gasified, syngas composed of carbon monoxide, hydrogen, methane and the like are obtained. By converting these fuels with a catalyst or the like, expensive liquid or gaseous fuels or chemicals can be obtained.

In particular, recently, the importance of a polygeneration system for obtaining a variety of high value-added products from low-grade liquid fuels has become important, and the importance of gasification technology is increasing.

In the case of the gasification technology, the fuel is mostly solid in many cases. In this case, a method such as a fixed layer, a fluidized bed, and a classification bed is used.

Among them, the fractionation layer decomposes the solid fuel to gasify it by reacting with air, oxygen, steam or a mixture of these gases with a gasifying agent.

In the case of gasification of the liquid fuel, the classification layer is mostly used. The difference from the gasification of the solid fuel fractionation layer is that the solid fuel is injected into the reactor while the liquid fuel is atomized through the nozzle.

In the case of a fuel prepared by atomizing a liquid fuel or a solid fuel into a slurry, it is very important to design the burner to spray the liquid fuel or the solid fuel to react with the gasifier.

The present applicant has filed a patent application for a synthetic gas production apparatus in many of the following Patent Documents 1 and the like.

Korean Patent Registration No. 10-1066187 (issued on September 21, 2011)

On the other hand, low-grade oils such as bio-pyrolysis oil, waste cooking oil, waste lubricating oil, and coal water slurry have strong acidity, and include moisture, char, dust, ash and other impurities.

These impurities lower the calorific value and combustion characteristics of the low-grade oil, and cause various physical and chemical problems such as oil supply system, clogging of nozzles, and corrosion.

In the case of using a low-grade oil, since the amount of the tea component is small and the steam gasification reaction rate is low, when moisture (steam) is supplied to the reactor, sufficient residence time must be given in a very large reactor.

That is, in the conventional gasification apparatus, when the low-grade oil is used, the water supplied to the reactor acts as an inert material to prevent the synthesis gas production, thereby lowering the synthesis gas yield.

Accordingly, there has been a problem that it is difficult to directly apply the low-level oil to the combustion system according to the related art.

It is an object of the present invention to provide a multistage gasification apparatus and method capable of gasifying a low-grade oil through a multistage gasification process.

It is another object of the present invention to provide a multistage gasification apparatus and method capable of preventing the reduction of the calorific value and the combustion characteristics generated during the application of low-grade oil and improving the gasification efficiency.

It is still another object of the present invention to provide a multistage gasification apparatus and method capable of regenerating a catalytic material by supplying high-temperature steam when reforming the catalytic material filled in the reactor during application of low-grade oil.

In order to accomplish the above object, a multi-stage gasification apparatus according to the present invention comprises a preheater for separating moisture contained in fuel, a first reactor for gasifying the fuel separated by moisture in the preheater by combustion reaction, And a second reactor for reforming the syngas produced in the first reactor.

A preheating unit and a first reactor are connected to one side of the preheating unit and a first transfer tube for transferring the moisture separated from the preheating unit to the first reactor is connected to the preheating unit and the first reactor, And a second transfer pipe for transferring water separated from the fuel to the second reactor is connected between the second reactors, wherein the fuel is any one of biodegradable oil, waste cooking oil, waste lubricating oil, and colloidal fuel do.

And a heat transfer pipe for transferring the heat of the synthesis gas produced in the first reactor or the second reactor to the preheating unit is connected between the preheating unit and the first reactor or the second reactor.

The first reactor is a reactor which receives the water separated from the preheater, atomizes and injects the fuel, and mixes the injected fuel with the gasifying agent to produce synthesis gas by a combustion reaction.

And the second reactor is a reformer for modifying the synthesis gas and the unreacted hydrocarbon fuel generated in the first reactor by using the moisture in the superheated steam state separated from the fuel in the preheater and the catalyst material provided therein .

In order to achieve the above object, a multi-stage gasification method according to the present invention includes the steps of: (a) separating moisture contained in fuel by using a preheating unit; (b) (C) generating synthesis gas produced by the step (b) through steam gasification using water and a catalyst material from the fuel in the step (a) using a second reactor; And reforming the gas.

Wherein the step (a) comprises the steps of: (a1) receiving the fuel to which the lower oil is applied and heating the fuel to a predetermined low temperature region lower than the boiling point of the oil component contained in the fuel to separate moisture contained in the fuel; (A3) supplying water separated from the fuel to the second reactor in the step (a1); and supplying the water separated from the fuel to the second reactor in the step (a1) do.

In the step (a), the water is separated by heating the fuel to a predetermined set temperature using waste heat generated in the synthesis gas production process of the first reactor or the second reactor.

In the step (b), only the fuel component in which water is separated in the step (a) is mixed with a gasifying agent and gasified by a combustion reaction to produce a synthesis gas.

In the step (c), the synthesis gas produced in the step (b) and the unreacted hydrocarbon fuel are steamed using the catalyst material in the second reactor and the moisture in the superheated steam state separated from the fuel in the step (a) And is reformed through gasification and an aqueous gasification reaction to produce a fuel gas.

The step (c) is characterized by using a fuel component dissolved in the moisture separated from the fuel and an oxidizing agent as a heat source necessary for an endothermic reaction.

As described above, according to the multi-stage gasification apparatus and method of the present invention, moisture contained in the fuel is separated before the gasification reaction, and only the fuel component removed from the first reactor is supplied to participate in gasification, The gasification efficiency can be improved.

According to the present invention, by modifying the syngas by using the moisture in the superheated steam state separated from the fuel and the catalyst material, impurities contained in the syngas can be deposited on the surface, Loses.

According to the present invention, it is possible to supply the heat source necessary for the endothermic reaction by supplying the water containing the fuel component dissolved in the water and the oxidizing agent during the synthesis gas reforming.

As a result, according to the present invention, it is possible to prevent deterioration in the calorific value and combustion characteristics occurring when a low-grade oil such as bio-pyrolysis oil, waste cooking oil, waste lubricating oil, and colloidal fuel is applied as fuel, , Corrosion, and other physical and chemical problems can be solved, so that the low-grade oil can be effectively applied to the existing combustion system.

1 is a configuration diagram of a multi-stage gasification apparatus according to a preferred embodiment of the present invention,
FIG. 2 is a process diagram for explaining steps of a multi-step gasification method according to a preferred embodiment of the present invention.

BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, a multi-stage gasification apparatus and method according to a preferred embodiment of the present invention will be described in detail with reference to the accompanying drawings.

1 is a configuration diagram of a multi-stage gasification apparatus according to a preferred embodiment of the present invention.

As shown in FIG. 1, the multistage gasification apparatus according to the preferred embodiment of the present invention includes a preheating unit 10 for separating moisture contained in fuel, a preheating unit 20 for combusting fuel, And a second reactor (30) for reforming the syngas produced in the first reactor (20) and the first reactor (20).

The fuel may be provided as a low grade oil such as bio-pyrolysis oil, waste cooking oil, waste lubricating oil, colloidal fuel.

The preheating section 10 functions to separate the water contained in the fuel before supplying the fuel to the first and second reactors 20 and 30 and gasifying it.

For example, the preheating unit 10 may be configured to preheat the fuel using waste heat generated during the synthesis gas production process of the first reactor 20 or the second reactor 30, that is, sensible heat of the synthesis gas The water can be separated by heating to the set temperature.

Since the boiling point of water is 100 deg. C and the boiling point of the oil component contained in the fuel is at least about 250 deg. C, the preheating section 10 can easily separate moisture using waste heat in a low temperature region lower than the boiling point of the oil component.

The low temperature region may be set to less than about 200 < 0 > C.

The water separated in the preheating section 10 contains a fuel component dissolved in water.

A supply pipe 11 for supplying fuel is connected to one side of the preheating unit 10 and a fuel in which water is separated from the preheating unit 10 is supplied between the preheating unit 10 and the first reactor 20 1 is connected to a first transfer pipe 12 for transferring the moisture separated from the fuel in the preheating section 10 and the second reactor 30 between the preheating section 10 and the second reactor 30, The second transfer pipe 13 can be connected.

The heat transfer pipe 14 may be connected to the preheater 10 to receive the heat of the synthesis gas produced in the first reactor 20 or the second reactor 30.

On the other hand, the preheating unit 10 may separate moisture contained in the fuel by using a heater (not shown) provided additionally.

In this embodiment, the moisture separated from the fuel in the preheating section 10 is supplied to the second reactor 30 through the second transfer pipe 13.

As described above, in the present invention, the moisture separated from the fuel in the preheating portion is supplied to the second reactor having the reaction condition of several hundreds of degrees Celsius or more in the superheated steam state, and is participated in the reforming reaction by steam gasification together with the catalyst material in the second reactor can do.

The first reactor 20 atomizes and injects the water separated from the preheating section 10 through the first transfer pipe 12, mixes the injected fuel with the gasifying agent, and produces a synthesis gas by the combustion reaction .

Generally, the gasification process determines the gasifier and the operating conditions according to the purpose of the reaction and the product, and it is classified into an entrained bed, a fluidized bed, a moving / fixed bed, .

In this embodiment, the first reactor 20 may be provided with a fluidized bed gasifier.

In the fluidized bed gasifier, a layer material such as sand having a size of several hundreds of micrometers is placed in the reactor, and a certain amount of air such as air is introduced at the bottom of the reactor to fluidize the solid or liquid layer material to have a fluid-like behavior.

Of course, the first reactor may be changed to a fractionation bed or a mobile bed / fixed bed gasifier.

The fluidized bed gasifier may differ in the movement of the bed material supplied to the inside of the reactor depending on the amount of the supplied gas and may transfer the bed material when the amount of the gas is appropriately increased.

Such a fluidized bed gasifier has the advantage of being able to use a wide range of fuels, to be applied to various capacities, and to easily control tar and syngas.

The gasifying agent may be a gaseous substance that blows a liquid fuel or a solid slurry fuel together with the fuel for gasification, and may include air, steam, oxygen, carbon dioxide, or a mixture thereof.

On the other hand, the lower oil used as the fuel in the present embodiment is a mixture of hydrocarbon-based fuels having various molecular weights, and is not gasified in the first reactor 20 in the case of a fuel component having a large number of carbon bonds.

Accordingly, the present invention can increase the gasification efficiency through the multi-stage gasification system using the first reactor and the second reactor.

That is, when the lower oil is directly introduced into the first reactor 20, the water and the oil simultaneously evaporate and a large volume expansion occurs. As a result, the residence time of the entire reactant is greatly reduced in the first reactor 20, It causes lowering.

Therefore, the present invention can greatly increase the reaction time by first separating the water from the preheating section and supplying only the fuel component removed moisture to the first reactor to participate in gasification.

A third transfer pipe 21 is connected between the first reactor 20 and the second reactor 30 to transfer the gasified synthesis gas and the unreacted hydrocarbon fuel to the second reactor 30 in the first reactor 20 .

A discharge pipe 32 for discharging the synthesis gas produced in the second reactor 30 may be connected to one side of the second reactor 30.

The third transfer pipe (21) or the discharge pipe (32) may be connected to a heat transfer pipe for transferring the heat of synthesis gas to the preheating unit.

The second reactor 30 is supplied with the moisture in the superheated steam separated from the fuel in the preheater 10 and the synthesis gas and the unreacted hydrocarbon fuel generated in the first reactor 20 using the catalyst layer 31 provided therein It functions to reform (reform).

The catalyst layer 31 may comprise a catalytic material such as activated carbon or dolomite to modify the syngas produced in the first reactor.

The water supplied to the second reactor 30 reacts with char or reacts with carbon monoxide (CO) according to the following reaction formulas 1 and 2 to convert the fuel gas to steam gasification and water gas shift reaction Can be produced.

[Reaction Scheme 1]

C + H ₂ O = CO ₂ + H ₂

[Reaction Scheme 2]

CO + H ₂ O = CO ₂ + H ₂

Low grade oils have low char content and slow steam gasification reaction.

Therefore, when the water in the superheated steam state is introduced into the first reactor 20, if the volume of the first reactor 20 is increased and sufficient residence time is not given, the water acts as an inert material that prevents synthesis gas production Thereby reducing the synthesis gas yield.

Also, since the reaction proceeds with the gasified carbon monoxide (CO), the reaction with the water in the overheated vapor state does not proceed significantly in the first reactor 10 into which the low-level oil in the liquid state is introduced.

On the other hand, when the catalyst material filled in the second reactor 30 is reformed, carbon or tar in the synthesis gas is deposited on the surface of the catalyst, thereby deteriorating the activity.

Therefore, in this embodiment, the catalyst material can be regenerated by supplying moisture in the superheated steam state.

As described above, according to the present invention, water contained in a low-grade oil applied as a fuel is separated and supplied to a second reactor before the gasification reaction, or when moisture content is low in the low-grade oil, Can be reproduced.

The water contained in the second reactor (30), including alcohols, can be supplied together with water-soluble fuel.

That is, as the endothermic reaction is mostly performed in the second reactor 30, it is necessary to supply a heat source having an appropriate temperature.

Alcohol is easily dissolved in water, is easy to supply, and has a characteristic of easily exothermic reaction when a gasifying agent is added.

Therefore, in this embodiment, it is possible to easily adjust the temperature of the second reactor by supplying an appropriate amount of the gasifying agent together with the moisture in the superheated steam state in which the fuel component such as the alcohol is dissolved.

As described above, the present invention can supply the heat source necessary for the endothermic reaction when the endothermic reaction occurs in the second reactor by supplying water and the oxidant in the superheated steam state to the second reactor.

On the other hand, the present invention can increase the residence time by reducing the supply flow rate of the first reactor by supplying the gasifying agent necessary for gasification of the fuel component dissolved in the water to the second reactor.

Accordingly, when air is used as the gasifying agent in the first reactor, the present invention can solve the problem that it is very difficult to control the residence time as a large amount of air is supplied compared to the fuel.

Next, referring to FIG. 2, a multi-stage gasification method according to a preferred embodiment of the present invention will be described in detail.

FIG. 2 is a process diagram for explaining a multi-stage gasification method according to a preferred embodiment of the present invention.

The multi-stage gasification method according to a preferred embodiment of the present invention includes the steps of (a) separating moisture contained in fuel by using a preheating unit, (b) gasifying by burning the water-separated fuel using the first reactor And (c) modifying the syngas produced in step (b) by steam gasification using moisture and catalytic material from the fuel in step (a) using a second reactor.

2, the preheating unit 10 is supplied with the fuel to which the low-grade oil is applied through the supply pipe 11 and is heated to a predetermined low temperature region at a temperature lower than the boiling point of the oil component contained in the fuel, The contained water is separated (S10).

For example, the preheating unit 10 may be configured to preheat the fuel using waste heat generated during the synthesis gas production process of the first reactor 20 or the second reactor 30, that is, sensible heat of the synthesis gas The water can be separated by heating to the set temperature.

The water separated in the preheating unit 10 is transferred to the first reactor 20 through the first transfer pipe 12 and the moisture separated from the fuel is transferred to the second reactor 20 through the second transfer pipe 13 30 (S12).

The first reactor 20 receives the water-separated fuel from the preheating unit 10 through the first transfer pipe 12, atomizes and injects the fuel, mixes the injected fuel with the gasifying agent, and gasifies the mixture by the combustion reaction And a synthesis gas is produced (S14).

At this time, the first reactor 20 can increase the gasification efficiency by greatly increasing the reaction time by burning and reacting only the fuel separated in the preheating section 10 by combustion.

The syngas produced in the first reactor 20 and unreacted hydrocarbon fuel are transferred to the second reactor 30 through the third transfer pipe 21 (S16).

Then, the second reactor 30 reforms the syngas and the unreacted hydrocarbon fuel through the steam gasification and the water gasification reaction using the internal catalytic material and the moisture in the superheated steam state transferred from the preheater 10, (S18).

The water in the superheated steam state supplied to the second reactor 30 reacts with char or reacts with carbon monoxide (CO) to perform steam gasification and water gasification, and carbon or tar in the synthesis gas The catalytic material deposited on the surface to lose activity is regenerated.

At this time, the second reactor 30 may be supplied with a preset amount of oxidizing agent to supply the heat source necessary for the endothermic reaction.

The syngas produced through this process is discharged to the outside of the multistage gasification apparatus through the discharge pipe 32, and may be stored in the storage tank or supplied to the combustion system.

Through the above process, the present invention separates the water contained in the fuel before the gasification reaction and contributes to the gasification by supplying only the fuel component from which moisture has been removed in the first reactor, thereby greatly increasing the reaction time, And the syngas can be reformed by using the catalyst material and moisture in the superheated steam state separated from the fuel.

Although the present invention has been described in detail with reference to the above embodiments, it is needless to say that the present invention is not limited to the above-described embodiments, and various modifications may be made without departing from the spirit of the present invention.

The present invention separates the water contained in the fuel before the gasification reaction and increases the reaction time by supplying only the moisture-removed fuel component in the first reactor and participating in the gasification, It is applied to multistage gasification technology that modifies synthesis gas using catalytic material.

10: preheating part 11: supply pipe
12: first transfer tube 13: second transfer tube
14: heat transfer tube 20: first reactor
21: Third transfer tube 30: Second reactor
31: catalyst layer 32: exhaust pipe

Claims (11)

A preheating unit for separating moisture contained in the fuel,
A first reactor in which the fuel separated from the water in the preheating unit is combusted to be gasified,
And a second reactor for reforming the syngas produced in the first reactor. The method according to claim 1,
A supply pipe for supplying fuel is connected to one side of the preheating unit,
A first transfer pipe for transferring the water separated from the preheating unit to the first reactor is connected between the preheating unit and the first reactor,
A second transfer pipe for transferring moisture separated from the fuel to the second reactor is connected between the preheater and the second reactor,
Wherein the fuel is any one of bio-pyrolysis oil, waste cooking oil, waste lubricating oil, and colloidal fuel. 3. The method of claim 2,
Wherein a heat transfer pipe for transferring the heat of the synthesis gas produced in the first reactor or the second reactor to the preheating unit is connected between the preheating unit and the first reactor or the second reactor. 4. The process according to any one of claims 1 to 3, wherein the first reactor
Wherein the reformer is a reactor which receives the water separated from the preheater, atomizes and injects the fuel, and mixes the injected fuel with the gasifying agent to produce a syngas by a combustion reaction. 5. The process according to claim 4, wherein the second reactor
And a reformer for reforming the synthesis gas and the unreacted hydrocarbon fuel produced in the first reactor by using moisture in the superheated steam state separated from the fuel in the preheater and catalyst material provided therein. (a) separating water contained in the fuel by using a preheating portion,
(b) gasifying the fuels in which moisture is separated in the step (a) by using a first reactor,
(c) modifying the syngas produced in the step (b) by steam gasification using water and a catalyst material from the fuel in the step (a) using a second reactor; and Way. 7. The method of claim 6, wherein step (a)
(a1) receiving a fuel to which a lower oil is applied, heating the fuel to a predetermined low temperature region at a temperature lower than the boiling point of the oil component contained in the fuel to separate moisture contained in the fuel,
(a2) supplying the fuel in which moisture is separated in the step (a1) to the first reactor, and
(a3) supplying the water separated from the fuel in the step (a1) to the second reactor. The method as claimed in claim 6 or 7, wherein the step (a)
Wherein the water is separated by heating the fuel to a predetermined set temperature by using waste heat generated in the synthesis gas production process of the first reactor or the second reactor. 9. The method of claim 8, wherein step (b)
Wherein the synthesis gas is produced by mixing only the fuel component in which water is separated in step (a) with a gasifying agent and gasifying the mixture by a combustion reaction. 9. The method of claim 8, wherein step (c)
(B) and the unreacted hydrocarbon fuel are subjected to steam gasification and water gasification reaction using the catalyst material in the second reactor and the moisture in the superheated steam state separated from the fuel in the step (a) To produce a fuel gas. ≪ RTI ID = 0.0 > 8. < / RTI > 11. The method of claim 10, wherein step (c)
Wherein a fuel component dissolved in moisture separated from the fuel and an oxidizing agent are used as a heat source necessary for an endothermic reaction.

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