KR102270504B1 - Open-type high-Ash fusion temperature Kenaf fueling system that does not require heating energy using room temperature water - Google Patents

Abstract

The present invention removes components that adversely affect heat transfer surfaces such as reactor walls and heat exchangers, such as fouling, slagging, high-temperature corrosion, and clinker generation during boiler operation from Kenaf, through physical and chemical methods and removes Kenya It relates to an open-type high-temperature ash-melting point Kenyaf fueling system that does not require energy to heat room-temperature water, which is used as a solid fuel for incineration or co-firing, and the reaction water can be intermediately treated without neutralization treatment.

Description

Open-type high-Ash fusion temperature Kenaf fueling system that does not require heating energy using room temperature water

The present invention relates to an open high-temperature ash-melting-point Kenyaf fueling system that does not require heating energy using room temperature water, and more particularly, to a reactor such as fouling, slagging, high-temperature corrosion, and clinker generation from Kenyaf during boiler operation. After removing and removing components that adversely affect the heat transfer surface such as walls and heat exchangers through physical and chemical methods, Kenyaf is used as a solid fuel for incineration or co-firing. It relates to an open high temperature ash melting point Kenyaf fueling system that does not require energy to heat room temperature water.

Energy sources that generate the largest amount of carbon dioxide and have a weak competitiveness against global warming are fossil fuel-based energy sources. Therefore, one of the current global issues as an energy source is the use and dissemination of new and renewable energy, which reduces carbon dioxide emissions compared to existing fossil fuels such as petroleum and coal, which can respond to global warming and climate change. Because it is an energy source.

In Korea, with the depletion of fossil fuels and the rise of greenhouse gas reduction in response to the international treaty on climate change, the total amount of power generation is provided to power generation companies (obligated to supply) with power generation facilities (excluding renewable energy facilities) of a certain size (500 MW) or more. The Renewable Portfolio Standard (RPS) was introduced, which made it mandatory to supply more than a certain percentage of the supply using new and renewable energy. For non-fulfillment of this mandatory supply, the reason for non-compliance is within 150% of the average transaction price of the supply certificate. The law was enacted so that a penalty surcharge could be imposed in consideration of the number of non-compliance, etc.

Accordingly, in order to be recognized by supplying new and renewable energy, it is a certificate that proves that the power generation business has produced and supplied electricity using new and renewable energy facilities. The new and renewable energy supply certificate (REC, Renewable Energy Certificate), which is given by multiplying the amount of new and renewable energy based on MWh supplied from the facility subject to the supply certificate issuance, is being implemented. It is financed by the government and reviewed every three years in consideration of the impact on industrial revitalization, power generation cost, the potential to exist, and the effect on the reduction of greenhouse gas emissions.

As a result, large-scale coal-fired power generation companies have integrated gasification combined cycle (IGCC), ultra-supercritical pressure (IGCC), Supercritical (USC) technology, _{Clean Coal Technology (CCT) such as CO 2} capture and storage technology, and biomass co-firing are being attempted, but there are many areas that need to be improved and overcome in solving the fundamental problem. It exists.

In particular, in the case of biomass co-firing, there is a problem in that power generation efficiency is lowered by burning biomass having a relatively low calorific value compared to coal.

In addition, since the combustion characteristics of biomass and coal input for co-firing are different, multi-stage combustion of coal occurs in an existing power generation facility designed for a target biomass combustion furnace, thereby causing a problem in facility operation.

In addition, there is also a problem that clinker or fouling occurs due to the inorganic component including the metal component contained in the biomass. In order to solve this problem, prior research has developed a technology for applying a fuel in which oil-based biomass is mixed with coal. As such, in the case of a fuel in which coal and oil-based biomass are simply mixed, the surface of the coal is usually coated with oil or the oil is partially impregnated into the pores. However, due to the low surface tension of the oil itself and the lack of bonding strength between the oil-based biomass and the coal surface, coal and biomass each maintain their existing combustion characteristics, resulting in different combustion characteristics. Therefore, when this is applied to a power plant, oxygen is preferentially consumed excessively due to the low-temperature combustion pattern of oil in the front part of the burner, and eventually inhibits the combustion of coal, increasing the amount of unburned carbon and reducing power generation efficiency. .

In addition, typical agglomeration phenomena of ash in biomass are slagging, clinker, fouling, and fluidized bed combustion, which are mainly generated on the radiative and convection transfer surfaces of the pulverized coal combustion furnace, respectively. ash agglomeration of

High-temperature chlorine corrosion of superheater tube in power plant, wear caused by flow rate change due to economizer tube ash clogging, tube wear caused by fluidized sand in fluidized bed combustor, and mechanical wear of chute blower are expected. When potassium and chlorine components generate KCl through chemical bonding in the combustion process, KCl (melting temperature 776℃) is a viscous material that adheres well and is known to accelerate corrosion by chlorine reaction.

When this phenomenon occurs in the combustion furnace, it is not only a major cause of reducing the efficiency of the process, but ultimately, if such a phenomenon worsens, the operation must be stopped, which causes enormous economic loss. Aggregation of ash is generally affected by ash composition, temperature, particle size, gas atmosphere, operating conditions, etc. In particular, when a part of ash is melted at high temperature, this phenomenon is accelerated.

On the other hand, it is disclosed in a number of known documents for responding to the above problems.

However, in the prior art known so far, there is a problem that the water treatment process is complicated after the reaction in Kenyaf, and in order to apply the separated component to the intended Kenyaf, there are many cases where the condition is high and the side reactants must be removed as much as possible. . In addition, since the treatment process is performed at a high temperature of 100° C. or more, there is a disadvantage in that energy costs are high.

Therefore, in low-temperature conditions to fundamentally rule out process problems caused by ash, the components that lower the ash melting temperature in Kenyaf are selectively removed while maintaining the existing Kenyaf components as much as possible, and the reaction wastewater generated at room temperature can be used as an intermediate treatment resource as long as possible. There is an urgent need to develop a technology for a Kenyaf fuel upgrading system to which an open reactor is applied.

Korean Patent No. 10-1945186 Korean Patent No. 10-1838293 Korean Patent No. 10-1879862

The present invention was devised to solve the above problems, and it is an invention that adversely affects the heat transfer surface such as the reactor wall and heat exchanger, such as fouling, slagging, high-temperature corrosion, and clinker generation during boiler operation from Kenaf. After removing the components through physical and chemical methods, Kenyaf is used as a solid fuel for incineration or co-firing. After the reaction, the reaction water is heated to room temperature water that can be treated intermediately, such as in a digester, without neutralization. To provide Kenyaf fueling system.

To this end, in the present invention, an open-type reactor that is treated with a weak acid under a predetermined reaction condition so that the minerals of Kenyaf are eluted; a pH adjustment tank for supplying a weak acid to the open-type reactor; a reaction water storage tank for supplying reaction water to the open type reactor; and a Kenyaf supply device for supplying Kenyaf to the open-type reactor; may include an open-type high-temperature ash-melting-point Kenyaf fueling system that does not require energy to heat room temperature water, including.

In addition, the predetermined reaction conditions are the weak acid is acetic acid, the pH is within 4 to 5.2, the reaction temperature is room temperature, the reaction time is within 20 minutes, and the pH of the reaction water after the reaction may be 7.6.

In addition, the predetermined reaction conditions are the weak acid is acetic acid, the pH is 4 to 4.2, the reaction temperature is room temperature, the reaction time is within 20 minutes, and the pH of the reaction water after the reaction may be 6.9.

In addition, the predetermined reaction conditions are the weak acid is acetic acid, the pH is 5 to 5.2, the reaction temperature is room temperature, the reaction time is within 20 minutes, and the pH of the reaction water after the reaction may be 7.6.

In addition, the predetermined reaction conditions are the weak acid is acetic acid, the pH is 4 to 5.2, the reaction temperature is room temperature, the reaction time is within 20 minutes, and the pH of the reaction water after the reaction may be in the range of 7.6.

In addition, the open-type reactor may be open to the atmosphere.

In addition, a dehydrator for separating the Kenyap and the reaction water after the reaction; may further include.

In addition, the reaction water after the reaction separated in the dehydrator may be discharged without physical and chemical water treatment.

In addition, the Kenyap separated from the dehydrator was analyzed through ASTM D1857.

SST (Start Softening Temperature) may be 1200 °C to 1400 °C.

In addition, the Kenyaf separated in the dehydrator may have a DT (Deformation Temperature) of 1400° C. to 1500° C. through ASTM D1857 analysis.

In addition, the Kenyaf separated in the dehydrator may have a Sphere Temperature (ST) of 1450° C. to 1500° C. through ASTM D1857 analysis.

In addition, the Kenyaf separated in the dehydrator may have a Hemisphere Temperature (HT) of 1500° C. or higher through ASTM D1857 analysis.

In addition, the Kenyaf separated in the dehydrator may have a flow temperature (FT) of 1500° C. or higher through ASTM D1857 analysis.

According to the open-type high-temperature ash-melting-point Kenyaf fueling system that does not require energy to heat room-temperature water of the present invention, it is possible to effectively and easily separate a component that lowers the ash-melting-point temperature from Kenyaf, for biomass burning and/or co-firing in a boiler. You can optionally secure Kenyaf.

In addition, by treating with weak acid under low temperature conditions in the present invention, there is no need for neutralization treatment in the wastewater treatment process of the reaction water after the reaction, thereby contributing to cost reduction and excluding the elution of carbon-based components such as cellulose, hemicellulose, and lignin as much as possible. .

In addition, it can effectively reduce clinker, fouling, and alkali corrosion problems that may occur during combustion system operation when applied to power generation fuel by effectively removing ash-causing components such as alkali and alkaline earth metals and halogen elements contained in biomass. .

1 is a flowchart illustrating an open-type high-temperature ash-melting point Kenyaf fueling system that does not require energy to heat room-temperature water according to an embodiment of the present invention.
2 is an SST and DT temperature test report after ASTM D1857 analysis after converting room temperature water into an open type high temperature ash melting point Kenyaf fuel that does not require heating energy according to an embodiment of the present invention.
3 is a cone shape photograph according to ASTM D1857 analysis conditions before converting room temperature water into an open high-temperature ash-melting point Kenyaf fuel that does not require energy to heat room temperature water according to an embodiment of the present invention.
4 is a photograph taken before and after the reaction temperature and PH in an open-type reactor according to an embodiment of the present invention.
5 is an open-type high-temperature ash-melting point Kenyaf fuel that does not require energy to heat room temperature water according to an embodiment of the present invention, and then a Kenyaf pellet ash-melting point test report according to ASTM D1857 analysis conditions.
6 is a graph showing the Fe-based corrosion characteristics according to the temperature and pH conditions of the present invention.

The terms or words used in the present specification and claims should not be construed as being limited to their ordinary or dictionary meanings, and the inventor may properly define the concept of the term in order to best describe his invention. It should be interpreted as meaning and concept consistent with the technical idea of the present invention based on the principle that there is. Therefore, since the embodiment described in this specification is only the most preferred embodiment of the present invention and does not represent all the technical spirit of the present invention, there are various equivalents and modifications that can be substituted for them at the time of the present application. It should be understood that

Hereinafter, a fuel production system in which ash-causing components are removed from biomass under low-temperature conditions in connection with dehydration drying and pelleting processes according to the present invention will be described in detail with reference to the accompanying drawings.

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1 is a flowchart illustrating a Kenyaf fuel upgrading system to which an open reactor is applied according to an embodiment of the present invention.

The reactor body may include a reactor heat insulating material (101). The insulating material is not limited to the material as long as it can have a warming effect.

The reactor thermal insulation material may be any one or two or more of glass wool, rubber foam, PE foam, Perlite, and urethane.

The low-temperature weak acid may be supplied independently or mixed with water.

The weak acid may be supplied to the room temperature weak acid water inlet.

The reaction water may be introduced into the reaction water inlet. The reaction water may be mixed and supplied to the weak acid.

The open-type reactor may include a reaction temperature increase facility for temperature control in winter. It is obvious that the type of the reaction temperature increase facility is not limited as long as the reaction temperature riser can control the temperature of the open type reactor. The reaction temperature increase facility may have a temperature increase rate of 1°C to 5°C/min.

If the above conditions are exceeded, the effect of increasing the temperature cannot be obtained.

The open-type reactor is operated in an open state in the atmosphere under atmospheric pressure and room temperature conditions.

After the metal ion removal reaction of the Kenyap and the dehydration process, it may be discharged through a solid fuel discharge unit for discharging fuel.

The pH adjusting tank is a device for supplying a weak acid to be supplied to the open-type reactor. The pH adjusting tank may include a treated water supply unit for supplying water for mixing with the weak acid. A catalyst weak acid storage tank for supplying the weak acid to the pH adjusting tank may be formed, and the weak acid may be supplied to the pH adjusting tank. A weak acid supply unit may be formed.

The pH adjusting tank may be provided with a stirrer for internal weak acid mixing characteristics. The pH adjustment tank may include a temperature increase facility for temperature control in winter. It is obvious that the type of the temperature increase facility is not limited as long as the temperature increase facility can control the temperature of the open reactor. The reaction temperature riser may have a temperature increase rate of 1 ℃ to 5 ℃ / min.

If the above conditions are exceeded, the effect of increasing the temperature cannot be obtained.

The pH adjustment tank may include a thermal insulation material. The insulating material is not limited to the material as long as it can have a warming effect.

The insulating material may be any one or two or more of glass wool, rubber foam, PE foam, Perlite, and urethane.

A treated water supply unit for additionally supplying water to the pH adjusting tank may be formed.

A low-temperature weak acid water discharge unit for supplying the weak acid water to the open-type reactor may be formed.

A pH adjusting tank drain unit for discharging the excess weak acid water may be formed.

A reaction water supply unit for supplying water to the reaction water storage tank may be formed.

A water level gauge for checking the liquid level may be additionally formed in the open reactor, the pH adjusting tank, and the reaction water storage tank.

The Kenyap inlet device includes a grinding unit for forming the biomass into Kenyap of a predetermined size; a hopper for storing the Kenyaf; It may include a;

The predetermined size of the Kenyap may be 50 mm or less.

Preferably, it may be 10 μm to 50 mm or less.

More preferably, it may be 1 mm to 10 mm or less.

If the particle size is out of the above particle size, the grinding cost may be excessively required, or the removal efficiency of the ash-causing component may be reduced.

The grinding unit may perform crushing and/or grinding. The pulverizing unit may use any one or more physical properties of compression, impact, friction, shear, and bending, and if it can achieve the purpose of reducing the size of biomass such as cutting and increasing the surface area at the same time, the method is not limited.

The crushing unit includes a jaw crusher, a gyratory crusher, a roll crusher, an edge runner, a hammer crusher, a ball mill, and a jet mill. mill), and may be any one of a disk crusher.

The Kenyaf supply feeder is not particularly limited as long as it is a device capable of quantitatively supplying the Kenyaf to the rear end.

The low-melting-point-inducing component is physically and chemically attached to the reactor wall, heat exchanger, and rear-end exhaust gas treatment facility among the inorganic components included in the biomass used for the combustion reaction, resulting in fouling, slagging, corrosion, and clinker. It means the ash-inducing ingredient that causes the production, etc.

The low melting point component may be an alkali, an alkaline earth metal, or a halogen element.

Typical low-melting components in combustion may be sodium, potassium, and chlorine.

The predetermined temperature may be room temperature water. Preferably, the room temperature water may be 20 ℃ to 30 ℃, more preferably 25 ℃.

If the temperature condition is exceeded, the ash-causing component is not sufficiently separated in the Kenyap. The temperature conditions may be changed according to Kenyaf.

The residence time of the feed Kenyan in the open reactor may be within 10 to 20 minutes depending on the reaction temperature. More preferably, the residence time may be within 10 minutes. When the residence time is exceeded, the acid reaction of the ash-inducing component in the alkali reaction product occurs again in the Kenyap, and a reverse reaction occurs in which the wastewater, which is the reaction product, becomes a weak acid.

The difference by pH concentration is that the pH concentration in the wastewater after the reaction is different, and the reaction temperature and pH concentration can be changed as needed.

The residence time conditions may vary depending on Kenyap.

In the fuel processing apparatus, the fuel may be carbonized or torrefied through the low-temperature treatment reaction at the predetermined temperature.

In the existing hydrothermal reaction, the amount of low-temperature catalyst weak acid water input per unit supply Kenya varies depending on the type of biomass, and can be defined as WTB (Water to Biomass, kg/kg). Preferably for each biomass the number of kenafs may be 1 to 4, preferably 4 to 6 more preferably 8, very preferably no washing process is necessary, very preferably for each biomass. A range of ± 10 % is acceptable.

If it is out of the WTB ratio, there is no problem in the separation efficiency of the induced component and the amount of reaction water is increased.

However, in an open-type reactor, there is a point of absorbing a lot of low-temperature water and weak acid into biomass rather than the ratio of biomass to water. Since there is no energy consumption or small amount in room-temperature water, and neutralization treatment is unnecessary, the mixing ratio of biomass and room-temperature weak acid water has the advantage of adapting to the site conditions of fuel production

Water and acidic solution may be injected for controlling the shear separation efficiency of the open reactor.

The room temperature catalyst water may be heated water or steam heated in a boiler when the reaction temperature is increased or indirect heating is performed by using low temperature hot water.

The acidic solution may be any one or two or more of acetic acid, nitric acid, hydrochloric acid, sulfuric acid, hydrofluoric acid, and formic acid.

The co-firing ratio condition may be 1wt% to 50wt% compared to conventional fossil fuels. Preferably it may be 3wt% to 40wt%, more preferably 5wt% to 30wt%.

The solid component of Kenyap discharged after the reaction in the open reactor may be an organic compound. The combustible component may include carbon, hydrogen, nitrogen, oxygen, and sulfur as a main component. The combustible component is characterized in that the carbon fraction in the carbon, hydrogen, nitrogen, oxygen, and sulfur of Kenyap per unit mass increases, and the hydrogen, nitrogen, oxygen, and sulfur components decrease.

The reaction water component discharged through dehydration in the open reactor may be an aqueous solution containing a small amount of organic compounds and inorganic substances. The organic compound may include carbon, hydrogen, nitrogen, oxygen, and sulfur as main components. Preferably, the organic compound may be lignin. Preferably, the inorganic material may include any one or more of Al, Si, P, Ca, Ti, Mn, and Fe.

The fuel processing apparatus may further include a molded fuel unit for manufacturing a molded fuel by applying the solid component.

6 is a graph showing the Fe-based corrosion characteristics according to the temperature and pH conditions of the present invention.

In addition, looking at the boiler use technology standard KBO 4248 issued by the Korea Energy Agency, it is known that the corrosion rate increases with an exponential function to the temperature in terms of chemical reaction kinetics.

In addition, regarding the effect of pH on the corrosion of pipes and reactors containing Fe as the main component, in KBO-4248.2, the flat part appearing near the neutral is in the pH4~pH10 range at 22℃, but when the temperature is 40℃, the hydrogen overvoltage is reduced in the acidic region. Corrosion increases and passivation becomes easy by the increase in the activity of OH ions in the basic region, so the flat part becomes narrower and becomes pH4.5~pH8.5 range.

Therefore, if the Kenyaph reaction is performed under room temperature conditions and mild pH conditions, corrosion of the reactor and economic efficiency can be improved.

100: open reactor
200: pH adjustment tank
300: reaction water storage tank
400: Kenyaf supply device
500: dehydrator

Claims (11)

an open-type reactor 100 for treating with a weak acid under predetermined reaction conditions so that the minerals of Kenyaf are eluted;
a pH adjusting tank 200 for supplying a weak acid to the open reactor;
a reaction water storage tank 300 for supplying reaction water at room temperature to the open type reactor; and
Includes; Kenyaf supply device 400 for supplying Kenyaf to the open-type reactor;
The predetermined reaction condition is that the weak acid is acetic acid and the pH is within 5 to 5.2,
The reaction temperature is room temperature, the reaction time is within 20 minutes,
After the reaction, the pH of the reaction water is 7.6
The number of reactions at room temperature is less than 20 to 30 °C,
WTB (Water to Biomass, kg/kg) is 8,
After the reaction, a dehydrator 500 for separating the Kenyap and the reaction water; further comprising
The open reactor is open to the atmosphere,
Kenyaf separated from the dehydrator is DT (Deformation) through ASTM D1857 analysis.
Temperature) is 1200 ℃ to 1400 ℃,
The Kenyaf separated from the dehydrator has an open high temperature ash melting point Kenyaf fueling system using room temperature water, characterized in that the ST (Sphere Temperature) through ASTM D1857 analysis is 1400°C to 1500°C.
delete delete delete delete delete According to claim 1,
Kenyaf separated from the dehydrator, characterized in that the SST (Start Softening Temperature) through ASTM D1857 analysis is 1200 ℃ to 1400 ℃
Open type high temperature ash melting point Kenyaf fuel conversion system using room temperature water.
delete delete According to claim 1,
Kenyaf separated from the dehydrator, characterized in that the HT (Hemisphere Temperature) through ASTM D1857 analysis is 1500 ℃ or more
Open type high temperature ash melting point Kenyaf fuel conversion system using room temperature water.
According to claim 1,
Kenyaf separated from the dehydrator is characterized in that the FT (Flow Temperature) through ASTM D1857 analysis is 1500 ℃ or more
Open type high temperature ash melting point Kenyaf fuel conversion system using room temperature water.

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