WO2019066096A1

WO2019066096A1 - Demineralized biomass, multi-fuel producing system using same and preparation method therefor

Info

Publication number: WO2019066096A1
Application number: PCT/KR2017/010648
Authority: WO
Inventors: 최영찬; 김정근; 이동욱; 박세준; 이영주; 박주형
Original assignee: 한국에너지기술연구원
Priority date: 2017-09-26
Filing date: 2017-09-26
Publication date: 2019-04-04

Abstract

The present invention relates to a demineralized biomass, a multi-fuel producing system using the same and a preparation method therefor and, more specifically, to: a demineralized biomass, which is capable of fundamentally eliminating a problem such as clinker fouling, caused by inorganic materials, by extracting and separating an inorganic component comprising metal ions from herbaceous or lignocellulosic biomass through methods including acid treatment, alkali treatment, hot water treatment and membrane filtration of a cellulose- and hemicellulose-derived solid component and a liquid component comprising ash and lignin, and can be applied to a fuel production process such as coal upgrading, ash-free molded fuel, ash-free torrefacted fuel and bioethanol, and the like by selectively supplying the separated cellulose- and hemicellulose-derived solid component, the liquid component comprising lignin, and/or water to various fuel production systems; a multi-fuel producing system using the same; and a preparation method therefor.

Description

Deionized biomass, complex fuel production system using the same, and production method thereof.

The present invention relates to a denitrifying biomass, a complex fuel production system using the same and a method for producing the same, and more particularly, to a method for producing a denitrifying biomass, which comprises solid phase components originating from cellulose and hemicellulose from an herbaceous or woody biomass, Separating and separating inorganic components including metal ions by using a method including acid treatment, alkali treatment, hydrothermal treatment and membrane filtration, thereby separating the separated cellulose, which is capable of fundamentally eliminating problems such as clinker fouling caused by an inorganic substance A liquid phase component containing hemicellulose, a liquid component containing lignin and / or water is selectively supplied to various fuel production systems to produce a high-quality coal, an ashfree-formed fuel, an ashfree carbonized fuel and a bioethanol Applicable de-mineral biomass, use it To a composite fuel production system and a manufacturing method thereof.

More particularly, the present invention relates to a system for producing a semi-carbonized fuel for a boiler for improving a biomass mixing ratio, and more particularly, to a system for producing a semi-carbonized fuel for a boiler from an herbaceous system, woody system, algae biomass, Etc., which are adversely affecting the surface of the reactor wall, heat exchanger, etc., are removed by physical and chemical methods, and then the solid phase component is applied to the boiler suck as a semi-carbonized solid fuel to remove the biomass solubility And more particularly, to a semi-carbonized fuel production system for a boiler for improving the biomass mixing ratio.

More particularly, the present invention relates to a fuel production system for a boiler in which fouling-inducing components are removed. More particularly, the present invention relates to a fuel production system for a boiler in which a fouling- The fouling inducing components that cause adverse effects on the heat transfer surface such as the wall surface and the heat exchanger are removed by physical and chemical methods, and the solid phase component is used as a solid fuel for burning or burning, and the liquid component containing the fouling inducing component The present invention relates to a fuel production system for a boiler in which a fouling inducing component is removed by applying a water treatment method using a method including an acid treatment, an alkali treatment, a hydrothermal treatment, a membrane filtration, an ion exchange, flocculation, adsorption and centrifugation.

More particularly, the present invention relates to a method for separating and recovering a combustible material by adding a powder to a liquid material obtained by hydrothermally treating the biomass.

The energy source that generates the largest amount of carbon dioxide and which is not competitive with global warming is an energy source based on fossil fuel. As a result, the use of renewable energy is one of the issues that are currently being addressed globally as an energy source. This means that the emission of carbon dioxide is reduced compared to conventional fossil fuels such as petroleum and coal, Because it is an energy source.

In Korea, with the depletion of fossil fuels and the reduction of greenhouse gas (GHG) emissions in response to the international treaty, the United Nations Framework Convention on Climate Change, the number of generators (Renewable Portfolio Standard (RPS)), which mandates that renewable energy should be supplied at a rate of more than a certain percentage of the supply certificate, The penalties were imposed so that penalties could be imposed in consideration of the number of reasons and defaults.

As a result, it is a certificate certifying that the power generation company has produced and supplied electricity using new and renewable energy facilities in order to receive the new and renewable energy. The supply obligator purchases the new and renewable energy supply certificate (REC) Renewable Energy Certificate (REC) that multiplies the new and renewable energy amount of MWh supplied from the equipment subject to the supply certificate by the weight, It is reviewed by the government every three years, considering the impact on technological development and industrial revitalization, cost of development, potential capacity, and effect on greenhouse gas emissions.

Therefore, in order to achieve the share of renewable energy supply in large-scale coal-fired power generation companies, IGCC (Integrated Gasification Combined Cycle) and Ultra (Clean Coal Technology, CCT) and biomass fouling (CO2 capture and storage technology), but there are many areas that need to be overcome to solve fundamental problems. .

Particularly, in the case of biomass coexistence, there is a problem that the power generation efficiency is lowered by burning biomass having a relatively low calorific value as compared with coal.

In addition, since combustion characteristics of biomass and coal injected for confluence are different, multi-stage combustion occurs in existing power plant designed for coal as a raw material, causing problems in facility operation.

Also, there is a problem that clinker fouling occurs due to an inorganic component including a metal component contained in the biomass. In order to solve these problems, in the previous research, a technique of applying a fuel mixed with oil-based biomass to a stone was developed. However, in the case of a fuel simply mixed with coal and oil-based biomass, Or the oil is impregnated into the pores. However, due to the low surface tension of the oil itself and the lack of bonding between the oil-based biomass and the coal surface, coal and biomass retain 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 the oil in the front part of the burner, which eventually inhibits the combustion of coal, thereby increasing the amount of unburned carbon and decreasing power generation efficiency .

The typical aggregation phenomena of ash in the biomass are the slagging and clinker fouling, which is mainly generated in the surface of the combustion furnace and the convection transfer surface in the pulverized coal combustion furnace, and the ash aggregation in the fluidized bed combustion furnace agglomeration).

It is expected that wear of the superheater tube of power plant due to high temperature chlorine erosion, change of flow rate due to condenser tube clogging, tube wear by fluidized bed of fluidized bed combustor, mechanical wear of chute blower, When the chlorine component forms KCl through the chemical bond during the combustion process, the KCl melting temperature is 776 ° C. KCl is a viscous material and is well known to accelerate corrosion by chlorine reaction and the like.

Such a phenomenon in the furnace not only becomes a major cause of the decrease in the efficiency of the process, but ultimately, if such a phenomenon becomes severe, the operation must be stopped, thereby causing a great economic loss. The coagulation phenomena of ash is generally influenced by ash composition, temperature, particle size, gas atmosphere, operating conditions, etc. Especially, when a part of ash is melted at high temperature, such phenomenon accelerates.

Furthermore, when looking at the ultrafine dust generation process by NOx,

● NO ₂ + O ₃ →→ NO ₃ (nitrate) + O ₂

● NO ₃ + NO ₂ →→ N ₂ O ₅ (dinitrogen monoxide)

N ₂ O ₅ + H ₂ O → 2HNO ₃ (nitric acid)

● HNO ₃ + NH ₃ (ammonia) → NH ₄ NO ₃ (ammonium nitrate)

Through the above reaction formula, nitrogen oxides are generated, which is the cause of the secondary fine dust (ultrafine dust). There are thermal NOx and FeuL NOx in the NOx generated when the fuel is burned, and the emission control value of the total exhausted NOx by Fuel NOx reaches 60 ~ 70%.

Meanwhile, a number of known documents for addressing the above problems are as follows.

Korean Patent Laid-Open Publication No. 2012-0077991 discloses a pretreatment apparatus for producing a substrate for ethanol fermentation from lignocellulosic biomass.

Korean Patent No. 10-1171922 discloses a method for manufacturing and treating carbohydrate-containing materials to change their structure and a system for providing structurally modified materials.

Japanese Laid-Open Patent Publication No. 2011-205933 discloses a method for producing a saccharified liquid from an enzyme from biomass.

Korean Patent Publication No. 10-1195416 discloses a method for producing a hybrid of high calorific value, in which the hydrophilic surface present in the lower carbon is coated with the carbon component of the biomass-derived material to modify it to thereby prevent re-adsorption of moisture even after drying have.

In Japanese Patent No. 2688509, the bran is washed with water to remove the water-soluble substance, and then treated with an aqueous alkali solution of 0.1 to 0.4. The fraction mainly composed of hemicellulose is eluted into the aqueous alkali solution. And a method for extracting and purifying hemicellulose.

Korean Patent No. 10-0476239 discloses a process for preparing water soluble and insoluble hemicellulose from rice hulls, comprising the steps of (1) removing protein from rice hulls and washing rice hulls; (2) extracting the rice hulls with a sodium hydroxide solution having a concentration of 0.5 to 1 M and filtering the same; (3) adding phosphoric acid to the alkali extraction solution obtained in step (2) to lower the pH of the solution to recover hemicellulose by precipitation; (4) a step in which the precipitate obtained in step (3) is further washed with phosphoric acid or oxalic acid and then decolorized by treatment with oxalate-potassium permanganate; (5) Separation of water-soluble and insoluble hemicelluloses is possible through pH control of the solution from the decolorized hemicellulose fraction obtained in the above step. In the recovery of water-soluble hemicellulose, phosphoric acid is recovered by precipitation or added with calcium to be insoluble The next recovering step; (6) A process for producing fine powder from a rice husk comprising a step of obtaining a powder by natural drying or spray drying the water-soluble and insoluble hemicellulose obtained through a series of such continuous processes, and then milling and passing the fine- Discloses a process for preparing water-soluble and insoluble hemicellulose.

Korean Patent Laid-Open Publication No. 2002-0017572 discloses a method of mixing and dewatering a waste water treatment sludge, a crushing step, and a manufacturing step of a regenerated sludge.

Korean Patent Publication No. 10-0413384 discloses a process for removing (i) starch and protein from a corn husk; (ii) a step of extracting the corn husk from which the starch and protein have been removed with an alkaline solution and filtering with a filter cloth; (iii) treating the alkali extract obtained in step (ii) with cellulase and cellobiase to react; (iv) a step of treating the enzyme reaction solution obtained in step (iii) with an adsorbent to obtain a filtrate through membrane filtration; and (v) purifying the filtrate. The present invention also provides a method for producing a water-soluble dietary fiber.

Korean Patent Publication No. 10-1457470 discloses a process for extracting hemicellulose from a biomass; b) precipitating and separating hemicellulose from the hemicellulose extract; And c) introducing the separated hemicellulose into a papermaking process, wherein the a) extracting step comprises the steps of: adding NaOH to the bran biomass at 135-160 for 70-180 minutes; To 25% of the total weight of the extract, the extraction ratio is 1: 8 to 1:16. In the step b), acetone is mixed with the hemicellulose extract to precipitate and separate hemicellulose. In the step c), the separated hemicellulose Characterized in that a polydicyanediamide electrolyte having a molecular weight of 300,000 to 700,000 and a cationic charge density of 3 to 7 meq / g using dicyandiamide as a fixing agent is used as a fixing agent for fixing in paper. A paper manufacturing method is disclosed.

Japanese Patent Application Laid-Open No. 11-240902 discloses a method of extracting water from a raw material containing water-soluble hemicellulose at a temperature of 80 or more and 140 or less at a pH of 2 to 7 for extracting water-soluble hemicellulose into an aqueous medium, , And then removing the insoluble matter. The method of producing water-soluble hemicellulose according to claim 1,

Evstigneyev, E., et al., Tappi J., 1992. Vol. 75, no. 5, pp. In 177-182, the influence of alkaline components on the delignification rate in the pulping process is solved by the progress of delignification during the steaming process and the β-alkyl aryl bonds in the remaining lignin component decreases, and the phenolic hydroxyl And the amount of biphenyl structure in dissolved lignin increases when the digestion process is completed. It is reported that the rate of delignification is positively influenced by NaOH and anthraquinone.

Evstigneyev, E., Russian Journal of Applied Chemistry. 2011, Vol. 84, no. 6, pp. In 1040-1045, the solubility of the black liquor in the aqueous solution of NaOH due to the digestion process of spruce and pine was studied under the conditions of molecular weight, temperature, liquid ratio and ionic strength of lignin, and the method of measuring the amount of phenolic hydroxyl in lignin, The solubility of lignin in the solution was calculated.

However, in the prior arts known to date, lignin is removed from biomass and physicochemical treatment is applied to extract hemicellulose, which is a main component of cellulose and xylose, which glucose is a main component, but a drug such as acid or alkali There is a problem in that the process is complicated because it involves a process of recovering used chemicals as well as an increase in the cost of the medicament. In order to apply the separated ingredients to a desired raw material, In many cases. In addition, various contents such as cellulosic, hemicellulose, lignin and the like, as well as the molecular structure, functional group and ash content are present depending on the kind of the raw material of the biomass, and various decomposition enzymes and decomposition conditions must be satisfied during saccharification for the bioethanol process . As a result, the extraction and separation conditions of the desired substance are not reliable.

Therefore, in order to promote the utilization and diffusion of new and renewable energy and secure the supply stability of biomass fuel, it is necessary to remove the inorganic components in the biomass to eliminate the process problems caused by ash, It is urgently required to develop a technology for an ash-free composite fuel production system that effectively extracts and separates and utilizes the same.

SUMMARY OF THE INVENTION The present invention has been conceived in order to solve the above-mentioned problems, and it is an object of the present invention to provide a process for producing a biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable biodegradable, Method, a solid phase component derived from the separated cellulose and hemicellulose, a liquid component including lignin, a metal ion component and / or water are selectively supplied to various fuel production systems to produce biofuel such as bioethanol , A coal high-grade process, and / or a biomass production process for combustion, and the like, and to provide a composite fuel production system using ash-free biomass.

In addition, fusing and high temperature corrosion inducing components, which cause adverse effects on heat transfer surfaces such as reactor walls, heat exchangers, etc., such as fouling, slagging, high temperature corrosion and clinker generation, from boiler operation, are generated from herbaceous, woody, and Algae biomass The present invention provides a system for producing a semi-carbonized fuel for a boiler for enhancing the biomass mixing ratio by which the solid phase component is removed by physical and chemical methods and then the solid phase component is applied to the boiler submerged by the semi-carbonized solid fuel .

Further, the solid phase component after the removal is used as a solid fuel for burning or firing, and the liquid component containing the fouling inducing component includes acid treatment, alkali, hydrothermal treatment, membrane filtration, ion exchange, flocculation, adsorption, The present invention is to provide a fuel production system for a boiler in which a fouling inducing component is removed by applying a water treatment method using a method.

It is another object of the present invention to provide a method for separating and extracting a combustible component from a biomass without using a chemical treatment method.

It is another object of the present invention to provide a method for separating and extracting a combustible component from a biomass that can simplify a separation and extraction process and reduce the cost by applying a simple method of adsorption and sieve separation.

To this end, the present invention provides a composite fuel production system using ash pre-biomass, comprising: a first processing unit (100) for treating the biomass with first treated water containing hot water at a predetermined temperature and pressure; And a second processing unit (200) for generating a liquid component and a solid-phase component from the biomass processed in the first processing unit with a second process water containing hot water at a predetermined temperature and pressure; And a composite fuel production system using ash-free biomass.

The apparatus may further include a third processing unit (300) for selectively adding a pH adjusting agent so that the liquid component processed in the second processing unit has a predetermined pH.

The fourth processing unit (400) further separates the liquid component processed in the third processing unit from the ash-free concentrated component present in the liquid component by using a predetermined solid-liquid separating device .

The fifth processing unit 500 may further include a fifth processing unit 500 for processing the solid-phase components processed in the second processing unit with hot water at a predetermined temperature and pressure.

Further, a hydrothermal treatment unit (600) for treating the solid phase component treated in the second treatment unit or the fifth treatment unit with hot water at a high temperature and a high pressure to produce a liquid fiber component containing hemicellulose and a solid fiber component including cellulose; May be further included.

The first discharge unit 610 discharges and separates the solid fiber component in the process of collecting steam discharged from the low-pressure region of the hydrothermal treatment unit without air contact.

The second discharge unit 620 discharges and separates the fiber liquid fraction in the process of collecting steam discharged from the other end of the hydrothermal treatment unit without air contact in a low pressure region.

In addition, an enzyme saccharification unit (700) for performing an enzymatic saccharification reaction for the production of bioethanol may be further included in the solid fiber component including cellulose discharged from the first discharge unit.

Further, the present invention further includes an extraction unit 800 for extracting acetic acid in a predetermined amount from the fiber liquid fraction containing hemicellulose treated in the hydrothermal treatment unit and recirculating the acetic acid to the fifth treatment unit and / or the hydrothermal treatment unit can do.

The spraying unit may further include a spraying generating unit (900) for generating a spraying solution at a predetermined concentration using the fiber liquid fraction treated in the extracting unit.

Further, a coal pretreatment unit 1000 for impregnating or coating coal having an average particle size of 4 mm or more among coarsely pulverized coals using the spray solution generated through the spraying generating unit; May be further included.

The spray solution is sprayed onto the coal while rotating coal having an average particle size of less than 4 mm among the coarsely pulverized coals using the spray solution generated through the spraying generating unit to granulate the coal while impregnating or coating the coal. A coal granulation unit 1100 for increasing the size of the coal; May be further included.

A forming fuel unit (1200) for producing an ashfree forming fuel by binding the solid phase component processed in the fifth processing unit with an ash-free concentrated component separated in the fourth processing unit; May be further included.

It is also preferable that any one or two of the cleaning unit and the moisture removal unit for cleaning are provided at the rear end of any one of the first processing unit, the second processing unit, the fourth processing unit and the fifth processing unit, A unit can be added.

Further, either one or two units of the cleaning unit and the moisture removal unit for cleaning may be added to the rear end of the hydrothermal processing unit.

Also, a semi-carbonization unit 1300 for producing an ash-free semi-carbonized fuel by heat-treating the solid-phase component processed in the fifth processing unit with the hydrophobic binder from the ash-free concentrated fraction separated from the fourth processing unit; May be further included.

Further, the separation liquid containing sodium separated from the liquid component via the filter unit may further include a recycle unit recirculating the first soaking unit and / or the steam unit.

Further, the ash-free condensed fraction separated from the fourth treatment unit and / or the solid-phase component treated in the fifth treatment unit may be selectively used as a phenol formaldehyde resin extender, a phenol formaldehyde resin extender, In the production of molding compounds, the use of urethane and epoxy resins, antioxidants, sustained release formulations, flow control agents, cement / concrete blends, gypsum board manufacturing, oil excavation, general dispersion, tanning leather, road coverings, vanillin manufacture, (Phenol) monomers, additional diverse monomers, carbon fibers, metal removal from solution, basis of gel formation, polyurethane copolymers, and combinations thereof, in the preparation of polyesters, side-products, phenol resins in polyolefin blends.

Further, the separation liquid containing the inorganic matter separated from the liquid component through the fourth processing unit may further include a recycle unit 1400 that recirculates the first and second processing units to the first processing unit and / or the second processing unit .

In addition, the bio-ethanol produced by the complex fuel production system using the ash-free biomass, which further comprises the enzyme saccharification unit, may be used.

Further, the coal may be manufactured by a composite fuel production system using ash-free biomass, further comprising the coal pretreatment unit.

The coal produced by the composite fuel production system using ash-free biomass, which further comprises the coal granulating unit, may be used.

Also, it may be an ash-free forming fuel produced by a composite fuel production system using ash-free biomass, which further includes the above-mentioned shaped fuel unit.

Also, it may be an ash-free semi-carbonized fuel produced by a composite fuel production system using ash-free biomass, which further includes the above-described semi-carbonization unit.

In addition, the inorganic-liquid-phase liquid component pretreated in the first treatment unit and eluted from the inorganic component containing the metal in the biomass may be supplied to the third treatment unit or the fourth treatment unit.

In the present invention, a grinding unit 101 for forming a biomass into a raw material of a predetermined size; A hopper 201 for storing the raw material; A feedstock supply feeder 211 for feeding the feedstock stored in the hopper to a downstream end of the feedstock; A component separation unit (301) for treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximize the fusion-welding and high-temperature corrosion-inducing components after combustion; A pelletizing unit (401) for pelletizing the separated fuel in the component separating unit; And a semi-carbonization unit (501) for carbonizing the pelletized fuel in the pelletizing unit. The semi-carbonized fuel production system for a boiler for improving the biomass mixture rate may be included.

A grinding unit 101 for forming the biomass into a raw material of a predetermined size; A hopper 201 for storing the raw material; A feedstock supply feeder 211 for feeding the feedstock stored in the hopper to a downstream end of the feedstock; A component separation unit (301) for treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximize the fusion-welding and high-temperature corrosion-inducing components after combustion; A semi-carbonization unit (501) for carbonizing the fuel from which the fusion and high-temperature corrosion-inducing components supplied from the component separation unit have been removed, and a pelletizing unit (401) for pelletizing the semi-carbonized fuel in the semi-carbonization unit; Carbonized fuel production system for a boiler for improving the biomass mixing ratio.

In addition, the liquid component discharged from the component separation unit may include the fusion-bonding and high-temperature corrosion-inducing component.

In addition, the solid phase component discharged from the component separation unit may include a combustible component in which the fusion-bonding and high-temperature corrosion-inducing component are separated.

The pH of the liquid component discharged from the component separation unit may be 6 or less.

Further, the liquid component separated from the organic compound in the liquid component may be recycled to the component separation unit.

In addition, the gaseous component discharged from the semi-carbonization unit may include an organic compound including an acid gas.

In addition, in the semi-carbonized fuel production system for a boiler for improving the biomass mixing ratio, the semi-carbonized fuel may be mixed up to 50 parts by weight or less in a boiler using fossil fuel.

A grinding unit 101 for forming the biomass into a raw material of a predetermined size; A hopper 201 for storing the raw material; A feedstock supply feeder 211 for feeding the feedstock stored in the hopper to a downstream end of the feedstock; A carbonization unit (501) for carbonizing the fuel supplied from the raw material feeder; A pelletizing unit (401) for pelletizing the semi-carbonized fuel in the semi-carbonizing unit; And a component separation unit (301) for treating the raw material supplied from the pelletizing unit with hot water at a predetermined temperature so as to maximally separate the fusion-welding and hot corrosion-inducing components from the raw material supplied from the pelletizing unit. Carbonized fuel production system for a boiler to improve the biomass mixing ratio.

A first step of forming the biomass into a raw material having a predetermined size in the crushing unit 101; A second step of storing the raw material in the hopper 201; A third step of feeding the raw material stored in the hopper to a downstream end of the raw material feeder 211 in a fixed amount; A fourth step of treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximally separate the fusion-induced and high-temperature corrosion-inducing components after combustion in the component separation unit 301; A fifth step of pelletizing the fuel in which the fusing and hot corrosion-inducing components are separated in the component separating unit, in the pelletizing unit (401); And a sixth step of carbonizing the pelletized fuel in the pelletizing unit in a semi-carbonizing unit 501. The semi-carbonized fuel for boiler may be a method for producing a boiler for improving the biomass mixing ratio.

The present invention also includes a grinding unit 102 for forming a feedstock of a predetermined size; A hopper 202 for storing the raw material; A raw material feeder 212 for feeding the raw material stored in the hopper to a downstream end in a fixed amount; And a fouling-inducing component separation unit (302) for treating the fouling-inducing component of the raw material supplied from the raw material feeder with hot water at a predetermined temperature so as to maximally separate the fouling- And a fuel production system in which the ring inducing component is removed.

The fouling inducing component may include the fouling inducing component in the liquid component discharged from the fouling inducing component separating unit.

The solid phase component discharged from the fouling inducing component separating unit may include a combustible component in which the fouling inducing component is separated.

In addition, the pH of the liquid component may be 6 or less.

Further, an aqueous solution having a low pH, from which the organic compound is separated from the liquid component, may be recycled to the fouling-induced component separation unit.

Further, the raw material may be supplied to a pretreatment unit that is pretreated with an alkali solution before being supplied to the fouling-inducing component separation unit.

Also, the pretreatment solid-phase component generated in the pretreatment unit is supplied to the fouling-inducing component separation unit, and the pretreatment liquid-phase component can be separated and discharged.

Further, a molded fuel unit for producing a molded fuel by applying the solid phase component; May be further included.

In addition, a membrane filter unit may be further included for separating the liquid component from the organic compound.

The fouling-inducing component separating unit or the pretreatment unit may further include one or two of a cleaning unit and a moisture removal unit at the rear end thereof.

And a fuel produced in a fuel production system from which the fouling-inducing component for biomass burning and / or confluence in the boiler is removed.

A first step of forming a feedstock from a raw material having a predetermined size by using the crushing unit 102; A second step of storing the raw material in the hopper 202; A third step of feeding the raw material stored in the hopper to a downstream end of the raw material feeder 212 in a fixed amount; And a fourth step of treating the fouling-inducing component separation unit (302) with hot water at a predetermined temperature so that the fouling-inducing component of the raw material supplied from the raw-material feeder is separated at maximum, Or a fouling-inducing component for confluence.

The method for separating the combustible component from the biomass hot water extract of the present invention comprises the steps of S-1 for crushing biomass by crushing means, S-2 for supplying hot water to the crushed biomass, S-3 step of separating the biomass into a liquid phase material and a solid phase material, S-4 step of adding a pulverizer to the liquid phase material, and a mixture of the pulverized and liquid phase material to a first separation means to recover the pulverized coal, And step S-5 of obtaining a filtrate.

Further, in the method according to the present invention, after the step S-5, the filtrate from which the pulverization has been removed is supplied to the second separation means, and the second separation means separates the first concentrate and the first permeate liquid Preferably, the method further comprises S-7 step of recovering the first concentrated liquid and supplying the first permeated liquid to the third separation means, and after step S-7, To obtain a second concentrated liquid and a second permeated liquid, and recovering the second concentrated liquid.

In the method for separating the combustible component from the biomass hot water extract of the present invention, After step S-5, the filtrate from which the flour has been removed is fed to the third separating means, and the second concentrate and the second permeate are obtained by the third separating means, and the second concentrate is fed It is also possible to carry out the step S-8 to recover.

Here, the pulverized coal preferably has a particle diameter of 10 탆 to 10 탆, and more preferably a particle diameter of 70 탆 to 5 탆.

The second separation means may be an ultrafiltration membrane or a microfiltration membrane, and the third separation means may be a nanofiltration membrane or a reverse osmosis membrane.

The method for separating the combustible component from the biomass hot water extraction solution according to the present invention comprises the steps of S-1 for crushing biomass by crushing means, S-2 for supplying hot water to the crushed biomass, An S-3 step of separating the biomass into a liquid phase material and a solid phase material, an S-4 'step of centrifuging the liquid phase material, and an S-5' step of recovering the concentrated slurry and obtaining a supernatant.

According to the composite fuel production system using the ash free biomass of the present invention, it is possible to effectively and easily extract the glucose component and the like from the herbaceous or woody biomass through the high temperature and high pressure reaction condition without using any chemical such as acid or alkali. The raw material for producing bioethanol can be selectively secured.

In addition, by effectively separating inorganic components such as metals contained in the biomass, ash-free fuel can be applied to a power generation fuel, thereby effectively reducing fouling of clinker and alkali corrosion that may occur during operation of the combustion system.

Further, it is possible to prevent re-adsorption of water by impregnating, drying and carbonizing the low-grade coal with the liquid component containing the obtained glucose and / or the solid component including lignin, thereby enabling the supply of coal having a high calorific value It is possible to obtain a high-grade coal with a low grade.

In addition, since the biomass component is impregnated and carbonized after impregnation with low grade coal, it is not necessary to separate biomass undiluted apparatus, which is an important factor that only biomass of less than 3.5 wt% There is an effect that it is possible.

In addition, since the ash-free biomass produces molded fuel and semi-carbonized fuel using cellulose, hemicellulose and lignin, clinker fouling expected from ash due to biomass after combustion and gasification in fluidized bed and undifferentiated combustion furnaces and gasification furnaces, There is an effect that the problem of high temperature corrosion can be fundamentally eliminated.

In addition, by filtering the ash-free lignin in the liquid component of the biomass by applying the filtering process, it is possible to secure the fuel for pulp production and recycle the treated water.

Further, by removing the nitrogen component in the fuel component, it is possible to remove the ultrafine dust due to the reduction of the fuel NOx generated during the combustion.

Further, by removing the sulfur component in the fuel component, there is an effect of reducing SOx generated during combustion.

According to the method of the present invention, the combustible component can be easily separated and recovered from the discarded biomass, thereby contributing greatly to the reduction of greenhouse gas.

According to the method of the present invention, since the combustible component can be selectively separated and recovered by adding the pulverized coal to the hydrothermal reaction liquid with the biomass, the cost of separating and recovering the combustible component can be greatly reduced.

In addition, the coal injection according to the present invention can greatly reduce the concentration of the combustible component contained in the hydrothermal reaction solution, thereby improving the operation performance of the separation membrane, and it is possible to greatly increase the recovery ratio of the combustible component contained in the hydrothermal reaction solution have.

1 is a flowchart showing a composite fuel production system using ash-free biomass according to the present invention.

2 is a flowchart illustrating a system for producing a semi-carbonized fuel for a boiler for improving a biomass mixing ratio according to the present invention.

FIG. 3 is a graph showing changes in the composition of raw materials before and after the fusion and high-temperature corrosion-inducing component separation unit in the semi-carbonized fuel production system for boilers for improving the biomass mixing ratio according to the present invention.

4 is a flowchart illustrating a fuel production system for a boiler in which a fouling inducing component is removed according to the present invention.

FIG. 5 is a graph showing changes in the composition of raw materials before and after the fouling-inducing component separation unit in the fuel production system for a boiler in which the fouling-inducing component is removed according to the present invention.

FIG. 6 shows a state change of a raw material component according to an embodiment of the fuel production system for a boiler from which a fouling-inducing component is removed according to the present invention.

FIG. 7 shows the ash removal rate and the ash composition according to the treatment conditions of the fouling-induced component separation unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed.

8 is a graph showing changes in XMG content and lower calorific value according to processing conditions of the fouling-inducing component separation unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed.

9 is a graph showing the relationship between the amount of ash and XMG in the fouling inducing component separation unit and the amount of XMG in the fouling inducing component separation unit according to the present invention, This shows the change in calorific value.

10 shows the ash removal rate and ash composition according to the treatment conditions of the pretreatment unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed.

11 is a graph showing changes in lignin content and lower calorific value according to processing conditions of the pretreatment unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed.

12 is a graph showing changes in ash content, lignin content and lower calorific value according to the temperature and the treatment time of the pretreatment unit according to an embodiment of the fuel production system for a boiler in which the fouling- will be.

13 is a graph showing fuel NOx reduction amount, heating value increase rate and ash removal rate according to a temperature condition of a fouling-inducing component separation unit according to an embodiment of the fuel production system for a boiler in which the fouling inducing component according to the present invention is removed.

14 is a schematic view showing a process of separating the combustible component from the biomass.

15 is a flowchart showing a method of separating a combustible component according to a third embodiment of the present invention.

16 is a flowchart of a method for separating combustible components according to a fourth embodiment of the present invention.

The terms and words used in the present specification and claims should not be construed as limited to ordinary or dictionary terms and the inventor may appropriately define the concept of the term in order to best describe its invention It should be construed as meaning and concept consistent with the technical idea of the present invention. Therefore, the embodiments described herein are merely the most preferred embodiments of the present invention and are not intended to represent all of the technical ideas of the present invention, so that there are various equivalents and modifications that can be substituted at the time of the present application It should be understood.

Further, the coal used in the present invention means at least one selected from among low grade coal recognized in the art such as peat, lignite, bituminous coal, bituminous coal or anthracite coal.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, a composite fuel production system using ashprobiomass according to the present invention will be described in detail with reference to the accompanying drawings.

A combined fuel production system using ashless biomass, comprising: a first processing unit (100) for treating the biomass with first treated water containing hot water at a predetermined temperature and pressure; And a second processing unit (200) for generating a liquid component and a solid-phase component from the biomass processed in the first processing unit with a second process water containing hot water at a predetermined temperature and pressure; And a composite fuel production system using ash-free biomass.

Lt; RTI ID = 0.0 > biomass < / RTI > supplied to the first processing unit. The physical treatment of biomass is not limited as long as it can achieve the purpose of reducing the size of the biomass, such as crushing, shearing, cutting, and increasing the surface area.

The device for performing the physical treatment of the biomass may be a mill, a mixer, a screw extruder, a rotary knife cutter, but is not limited thereto.

On the other hand, as biomass raw materials, woody plants and herbaceous plants can be used. Woody lines include wood blocks, wood chips, logs, tree branches, wood crumbs, deciduous woods, sawdust, lignin, xylenes, lignocellulosic, palm trees, palm kernel shells, palm kernel fiber, empty fruit bunches ), Fresh fruit bunches (FFB), palm leaves, coconut crumbs, and the like. Herbal products include corn stover, straw straw, canteen, sugar cane, grain (rice, millet, coffee, etc.) husks, candy leaves, bagasse, millet, artichoke, molasses, flax, hemp, Biomass such as starchy maize, potato, cassava, wheat, barley, lime, other starch-based remnants, fruit-bearing avocados, jatropha and their processing residues can be used.

The biomass thus pulverized into an appropriate size is transferred to the first processing unit.

In addition, the biomass refers to lignocellulose-based herbaceous and woody biomass, and the material belonging to the biomass is not limited. It is also apparent that first- or third-generation biomass is also applicable. Cellulose, which is a major component of lignocellulose, is a stable polysaccharide in which glucose is linked by β-1,4 bonds. Another major component is a polymer of xylose, which is a pentane. In addition, it is composed of a polymer such as 5-valent arabinose, 6-valent mannose, galactose, glucose, rhamnose, etc. Of a polymer.

Glucan is a generic term for polysaccharides composed of glucose. There are various types of polysaccharides depending on the binding style of D-glucose. They are largely divided into α-glucan and β-glucan by the arrangement of the adduct carbon atoms. The α-glucan includes amylose (α-1,4 bond), amylopectin (α-1,4 and α-1,6 bonds), glycogen (α-1,4 and α-1,6 bonds), bacterial dextran (-1,6 bond) and the like. Typical examples of? -glucan include cellulose (? -1,4-linked), brown alga laminaran (? -1,3-linked), lichenous lichenan (? -1,3 and? -1,4-linked) have.

Xylene (xylan) is the liquid component containing xylene. Glucuronoxylan, arabinoxylan, glucomannan, xyloglucan, and the like may be included. The liquid component containing xylene as the above-described components is not limited, and various components may be separated depending on the components of the biomass to be injected.

The saccharides are not limited to the above-described compounds and can be variously produced depending on the kind of the second generation biomass. Therefore, it is divided into 2, 3, 4, 5, and 6-carbon sugars according to the number of carbon atoms. Glycoaldehyde, Glyceraldehyde, Dihydroxyacetone, , Erythrose, erythrulose, pentose, ribose, arabinose, xylose, ribulose, and Zylurozu as quaternary sugars. xylulose and 6-carbon sugars can be glucose, glucose, fructose, fructose, galactose and mannose.

Examples of the disaccharide to which two monosaccharides are combined may include lactose, lactose, lactose, glucose, maltose, maltose, sugar, sucrose, trehalose, melibiose and cellobiose.

Examples of the small sugars that are sugar-bonded sugars having 2 to 10 molecules include raffinose, melezitose and maltoriose as three saccharides, starchose and schrodose as four saccharides, And oligosaccharides may be galactooligosaccharides, isomaltooligosaccharides, and fructooligosaccharides.

Examples of the polysaccharides include pentosan, which is a simple polysaccharide with pentoses attached thereto, and may include xylan and araban.

Hexoxanes condensed with 6-valent sugars include starch, starch, polymers of glucose such as amylose, dextrin, glycogen, cellulose, fructan, galactan galactan, mannan, and the like.

Composite polysaccharides may include agar, alginic acid, carrageenan, chitin, hemicellulose, pectin, and the like.

The temperature condition of the first processing unit may be 80 캜 to 140 캜. Preferably 90 < 0 > C to 130 < 0 > C. And more preferably 100 ° C to 120 ° C. The pressure condition of the first soaking unit may be between 1 and 1.5 bar.

If it is lower or higher than the above temperature and pressure conditions, the purpose of air discharge and liquefaction in the biomass, the purpose of securing energy for raising the temperature, the purpose of impregnating the biomass with the organic acid generated in the subsequent step, For the purpose of increasing < / RTI >

The first treated water may be hot water at a predetermined temperature and pressure, and may further include an alkaline liquid. The alkali component may be NaOH, KOH, ammonia, lime, hydrogen peroxide, etc., and is not limited as long as it is water-soluble and can raise the pH of the aqueous solution.

It may further comprise a slightly acidic liquid. The weakly acidic component may be acetic acid, formic acid, and the like, and is not limited as long as it is water-soluble and can lower the pH of the aqueous solution. Additional carbon dioxide can be supplied.

It may further comprise a strongly acidic liquid. The acidic component may be sulfuric acid, nitric acid, hydrochloric acid, and the like, and is not limited as long as it is water-soluble and can lower the pH of the aqueous solution.

In addition, the temperature condition of the second processing unit may be 100 캜 to 300 캜. Preferably from 120 [deg.] C to 250 [deg.] C. And more preferably 150 ° C to 170 ° C. The pressure condition of the second processing unit may be between 1 and 20 bar. Preferably 1.5 to 7 bar. More preferably from 2 to 2.5 bar. The pH condition of the second processing unit may be 8 to 14 hours. Preferably 11 to 13.5. More preferably from 12 to 13 carbon atoms.

If the temperature, pressure and pH conditions are lower or higher than the above-mentioned conditions, the purpose of elution of the lignin component in the biomass, the purpose of discharging air in the biomass and the liquid saturation, the purpose of securing energy for raising the temperature, It is not effective for the purpose of impregnating the mass, and for the purpose of increasing the dry matter in the liquid phase.

And the second treated water of the second processing unit further contains an alkaline liquid in addition to hot water at a predetermined temperature and pressure. The alkali component may be NaOH, KOH, ammonia, lime, hydrogen peroxide, etc., and is not limited as long as it is water-soluble and can raise the pH of the aqueous solution.

Further, the third processing unit adds a pH adjusting agent to lower the pH in order to selectively filter the liquid component containing lignin in the fourth processing unit in the second processing unit. The pH adjusting agent is not limited if the pH can be lowered. Sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, etc. may be added, and hydrogen sulfide, sulfur dioxide, CO ₂ and the like may be added. Additional water may be added. The desired pH through the pH adjusting agent may be from 7 to 12. Preferably from 8 to 11. More preferably from 9 to 10 carbon atoms. If the pH is higher than the above-mentioned pH, the separation membrane may be damaged during the filtering of the liquid component.

Further, the fourth treatment unit is not particularly limited as long as it is capable of selectively separating components containing lignin of the liquid component. It is possible to selectively use one or more of a general filter, a micro filter, an ultrafiltration filter, a nanofiltration membrane, and a reverse osmosis membrane. They can be connected in parallel or in series. In addition, a screen for pretreatment and a micrometer-level particle removal filter can be applied as a pre-treatment filter.

And the inorganic-liquid-containing liquid fraction pretreated in the first treatment unit and eluted from the inorganic component containing the metal in the biomass may be supplied to the third treatment unit or the fourth treatment unit. This process means that the process of eluting the ashfree component in the biomass can be variously combined in process conditions that are optimized.

This is because application of such a process is variously predicted depending on properties of the biomass to be treated, pre-treatment particle size, process temperature, pressure, composition of treated water, acidity to be supplied, alkaline, ionic compound, catalyst and the like.

When the microfiltration membrane and the ultrafiltration membrane are applied, the membrane can be classified into a sheet type plate type, a hollow hollow type hollow fiber type, and a tubular type tubular type.

There is also a housing containment film in which the film is placed in the case and a deposition film in which the film is directly immersed in water. In the water flow method, there are an external pressure type which supplies the substance to be treated from the outside of the membrane and a pressure type which supplies the substance from the inside. The filtration method is a method of filtrating the total amount of feed water, such as sand filtration, a dead-end flow method in which the filtration is continued while discharging the contaminants accumulated on the membrane surface regularly, Cross-flow filtration, which suppresses the accumulation of suspended matter or colloidal material on the membrane surface, is a filtration method in which the membrane module is immersed in a dipping bath, While there is an advantage in that it is easy to operate, when the operation under high pressure conditions is impossible, there is a limit to the operation of high flux (flux).

In the filter unit, as a pretreatment unit, a screen or strainer facility for removing contaminants, a general filter of 1 to 1001 m, a coagulant for improving filtration performance, a solidifying agent, a polymeric absorbent, an injection facility, a sand filtration facility, And chlorine injection equipment for oxidation of manganese.

The membrane filtration facility can be selectively provided with a raw water tank, a pump, a membrane module, and a cleaning unit.

The wastewater treatment facility may perform filtration for the washing wastewater again to recover the desired components or to improve the recovery rate, or to install the concentration tank and perform gravity sedimentation to return the supernatant to the raw water.

When the nanofiltration membrane is applied, a Christmas tree method is used in which the module is arranged in a multi-stage in the separation membrane. The concentrated tree is a Christmas tree method in which the concentrated water is discharged from the end to the system, and the concentrated water is returned to the supply water line. The pump circulation system for discharging the refrigerant to the outside can be applied. Such nanofiltration membranes are also capable of separating minerals such as calcium and magnesium.

When the reverse osmosis membrane is applied, the membrane module may be divided into a spiral type, a hollow-fiber type, a tubular type, and a flat and frame type depending on the structure.

Typically, the molecular weight of a material derived from biomass is selected from the group consisting of glucose 180, xylose 150.13, mannose 180.2, galactose 180, arabinose 150.13, lignin 800-10000, furfural 96.09, levulinic acid 116, It is known as formic acid 46.03, acetic acid 60, Na ₂ O ₃ Si 122.06, NaOH 40, and SiO ₂ 60, so that a separation membrane can be applied for selective separation according to the molecular weight.

Since the atomic weight (g / mol) of inorganic components is known as Na 23, K 40, Mg 24.3, Mn 54.9, Ca 40, Ti 47.86, Cl 35.45, Si 28 and Al 27, can do.

The temperature condition of the fifth processing unit may be 80 캜 to 140 캜. Preferably 90 < 0 > C to 130 < 0 > C. And more preferably 100 ° C to 120 ° C. The pressure condition of the first soaking unit may be between 1 and 1.5 bar.

If the temperature and pressure are lower or higher than the above-mentioned conditions, the purpose of the air discharge and liquid saturation in the solid phase component, the energy securing purpose for the temperature rise, the purpose of impregnating the biomass with the organic acid generated in the subsequent step, For the purpose of increasing < / RTI >

The treated water may be hot water at a predetermined temperature and pressure, and may further include a weak acid liquid. The weak acid component may be acetic acid, formic acid, etc., and is not limited as long as it is water-soluble and can lower the pH of the aqueous solution.

The hydrothermal processing unit is operated so that a predetermined temperature, pressure, and reaction time are maintained. The solid phase components supplied to the hydrothermal treatment unit are broken up into a solid phase containing hemicellulose, a liquid phase containing cellulose and lignin, and a high pressure and temperature, resulting in breakage of the structure.

Among the components separated from the hydrothermal processing unit, the liquid phase containing hemicellulose is finally subjected to glycosylation to obtain xylose. On the other hand, the obtained sugar is not particularly limited as long as it can be obtained from hemicellulose, but it may be preferably Arabinose or Xylose.

Here, the hydrothermal treatment unit is operated so that the reaction is maintained at 160 to 250, 9 to 30 bar, and 1 to 5 hours so that the supplied solid phase component particles are broken and separated into a liquid phase containing hemicellulose and a solid phase containing cellulose and the like do. Preferably 180 to 220, 15 to 25 bar, and 2 to 4 hours. More preferably 190 to 210 ° C, 18 to 22 bar and 1 to 3 hours. Reaction If the temperature is out of the above-mentioned range, the pressure range or the reaction time, it may be preferable to operate under the reaction conditions since the recovery rate of the finally obtained glucose may be lowered, the reaction time may become excessively long, or the operation cost may increase.

On the other hand, conventional known techniques for separating and extracting glucose and xylose from biomass include a physical pretreatment process for crushing and crushing raw materials to a proper size, a chemical pretreatment process using chemicals such as acids and alkalis, And xylose and glucose have been separated and extracted through processes. However, in the present invention, by conducting a high-temperature high-pressure reaction under optimized conditions without using chemicals such as acids or alkalis after the physical pretreatment process, glucose can be effectively extracted and separated, and the recovery rate of glucose can be increased And these configurations and effects can be said to be the main features of the present invention.

In addition, since cellulose and hemicellulose are soluble in acid, lignin is soluble in alkali, and therefore, acid or alkali is pre-treated at a high temperature with a solvent. However, hemicellulose, which is a major component of xylose, has a weak heat characteristic, and when a long time treatment is performed at a high temperature, a part of hemicellulose is changed into a fermentation inhibiting substance to cause not only xylose loss but also fermentation inhibition problem. It is possible to prevent the loss of the xylose and the fermentation degradation problem in advance.

The acid participating in the reaction are sulfuric acid (H ₂ SO _4), hydrochloric acid (HCl), nitric acid (HNO _3), phosphoric acid (H ₃ PO _4), and acetic acid _{_{_{(C 2 H 4 O 3)}}} , oxalic acid (C ₂ H ₂ O ₄ ), and the like. The acid is not limited to the acid described above, and any acid which decomposes hemicellulose and cellulose may be used. Examples of the base involved in the reaction include sodium hydroxide, calcium hydroxide, urea, and the like. The base is not limited to the base described, and any base that promotes the reaction characteristics can be used.

Examples of the ionic liquid participating in the reaction include imidazolium compounds such as 1-ethyl acrylate-3-methylimidazolium chloride, 1-butyl-3-methylimidazolium chloride, Butyl-3-methylimidazolium tetrafluoroborate, 1-butyl-3-methylimidazolium chloride, 1-butyl- Butyl-3-methylimidazolium hexafluorophosphate, 1-butyl-3-methylimidazolium trifluoromethanesulfonate, 1-ethyl-3-methylimidazolium 1-ethyl-3-methylimidazolium acetate, 1-benzyl-3-methylimidazoliumchloride, 1,3-dimethylimidazoliummethylsulfate, sulfate, 1-butyl-3-methylimidazolium chloride, 1- Ethylimidazolium bromide ([EMIM] Br), ethylmethylimidazolium acetate, and the like, and ethylmethylimidazolium chloride ([EMIM] Cl) Ethyl imidazolium bromide, 1-ethyl-3-methyl imidazolium chloride, 1-ethyl imidazolium bromide, 1-ethyl imidazolium iodide, Ethyl-imidazolium chloride, 1,2,3-trimethyl imidazolium methyl sulfate, 1-methyl imidazolium chloride, 1-butyl-3-methyl imidazolium, Ethyl-3-methyl imidazolium hydrogensulfate, 1-butyl-3-methyl imidazolium hydrogensulfate, methylimidazole 1-ethyl-3-methyl imidazolium acetate, 1-butyl-3- Ethyl-3-methyl imidazolium methanesulfonate, methyl-tri- methyl-imidazolium acetate, tris-2- butyl-3-methyl imidazolium chloride, 1-ethyl-3-methyl imidazolium chloride, 1-ethyl-3-methyl imidazolium thiocyanate, 1-butyl- Methylimidazolium nitrate, 1-butyl-3-methylimidazolium acetate, 1-butyl-3-methylimidazolium chloride, Methylimidazolium nitrate, 1-ethyl-3-methylimidazolium acetate, 1- (2-methylimidazolium) acetate, 1- Ethyl-3-methylimidazolium tetrafluoroborate, 1-allyl-3-methylimidazolium chloride, 1-allyl-3-methyl Imidazolium nitrate, 1-methyl-3-Ali are imidazolium acetate, 1-methyl-3-Ali may be a borate as imidazolium tetra flow. The ionic liquid is not limited to the ionic liquid described above, and any ionic liquid can be used as long as it improves the reaction characteristics.

The amount of one or more of the enzyme, acid, alkali, and ionic liquid introduced into the reaction unit may not be supplied depending on the reaction conditions.

In addition, a compound such as furfural may be generated while the solid phase component participates in the high-temperature high-pressure reaction through the hydrothermal processing unit.

In addition, an enzyme saccharification unit 700 for performing an enzymatic saccharification reaction for the production of bioethanol may be further included in the solid fiber component including the cellulose treated in the hydrothermal treatment unit.

In addition, the enzyme saccharification unit is characterized in that any one or two or more of enzyme, acid, alkali, and ionic liquid is added.

Examples of enzymes involved in the degradation of hemicellulose include enzymes such as Endo-1,4-β-D-xylanases, exo-1,4-β-D-xylosidases, endo-1,4- L-arabinofuranosidases, α-galactosidases, and ferulic acid esterases. Endo-glucanase (EG), cellobiogydrase (CBH), and β-mannosidase ), β-glucosidase (BGL), and the like. The enzyme is not limited to the enzymes described, and any enzymes capable of decomposing hemicellulose and cellulose may be used.

Further, it further includes an extraction unit (800) for extracting acetic acid in a predetermined amount from the fiber liquid fraction containing hemicellulose treated in the hydrothermal treatment unit and recycling the acetic acid to the fifth treatment unit and / or the hydrothermal treatment unit .

Wherein the concentration of the spraying solution is selected from the group consisting of a solid phase component containing glucan due to cellulose separated from the hydrothermal treatment unit, a liquid component containing glucan due to cellulose, and a liquid component containing glucose generated through the enzyme saccharification unit A certain amount of moisture is contained in the solid phase containing one or two or more liquid phase components and lignin separated in the fourth treatment unit.

The concentration is expressed as a solution ratio of the liquid component to be added to the total spraying solution, and may be more than 0 and less than 1. Preferably from 0.3 or more to 0.95 or less, and more preferably from 0.5 or more to 0.9 or less.

If the solution ratio is lower than the above-mentioned range, there is a disadvantage in that the amount of water is large and thus the process ratio is large, and when it is higher than the solution ratio, viscosity conditions for spraying and the like are difficult.

It is apparent that the fuel produced through the coal granulation unit may produce fuel in the form of pellets.

The coal pretreatment unit or the coal granulation unit may be operated independently or simultaneously depending on whether or not the coal satisfies the average grain size condition.

Further, as the addition unit, a waste liquid generated in the bleaching unit for pulp production utilizing the solid-phase component generated through the second processing unit may be additionally supplied.

Further, a cleaning unit and a moisture removal unit for cleaning are provided at the rear end of any one or two or more of the first processing unit, the second processing unit, the fourth processing unit, the fifth processing unit and the hydrothermal processing unit, Any one or two units may be added.

The cleaning unit may be any one or more of a cleaning pump, air pressure, back pressure, air stripping, raw water cleaning, and mechanical vibration.

A forming fuel unit (1200) for producing an ashless molding fuel by binding the solid phase component processed in the fifth processing unit with an ash-free condensed fraction separated from the fourth processing unit with a hydrophobic binder; May be further included.

* Separated ash-free concentrates can contain large quantities of lignin and are characterized by hydrophobicity of lignin. Thus, the molded fuel can be produced using a solid phase component containing a large amount of cellulose and / or hemicellulose treated in the fifth treatment unit with a binder as a separated ash-free concentrated fraction.

Such molded fuel can be used in a fluidized bed, grate, undifferentiated boiler, gasifier, and the like. The clogging phenomenon of clinker fouling caused by an inorganic component including a metal element in fuel during combustion and gasification and corrosion caused by alkali metal The origin of the phenomenon can be ruled out.

Wherein the ash-free condensed fraction separated from the fourth treatment unit and / or the solid-phase component treated in the fifth treatment unit are selectively used as a phenol formaldehyde resin extender, a molding compound Cement / concrete mix, gypsum board manufacturing, oil excavation, general dispersing, tanning leather, road coverings, vanillin manufacture, dimethyl sulfide and dimethyl sulfoxide manufacture in the manufacture of urethane and epoxy resins, antioxidants, release agents, flow control agents, , Phenol substitution with phenol resin in a polyolefin mixture, aromatic (phenol) monomers, additional various monomers, carbon fibers, metal removal from solution, basis of gel formation, polyurethane copolymer, and combinations thereof.

Here, in the carbonization process of the present invention, a known carbonyl group can be used, so that the heating temperature for carbonization is preferably 180 to 220, not particularly limited. More preferably, the carbonization can be carried out at a temperature of 190 to 210 ° C. By this carbonization process, moisture can be prevented from being adsorbed again to the surface of the ashfree semi-carbonized fuel powder or into the micropores, and it is possible to facilitate the transportation and storage of the ashfree biomass fuel, An ash-free biomass semi-carbonized fuel having a high calorific value can be obtained.

Further, the separation liquid containing the inorganic matter separated from the liquid component through the fourth processing unit may further include a recycle unit 1400 that recirculates to the first processing unit and / or the second processing unit .

FIG. 2 is a flowchart showing a fuel production system for a boiler in which fusing and hot corrosion-inducing components are removed according to the present invention.

A crushing unit (100) for forming the biomass into a raw material of a predetermined size; A hopper 201 for storing the raw material; A feedstock supply feeder 211 for feeding the feedstock stored in the hopper to a downstream end of the feedstock; A component separation unit (301) for treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximize the fusion-welding and high-temperature corrosion-inducing components after combustion; A pelletizing unit (401) for pelletizing the separated fuel in the component separating unit; And a semi-carbonization unit (501) for carbonizing the pelletized fuel in the pelletizing unit. The semi-carbonized fuel production system for the boiler for improving the biomass mixing ratio may be used.

The biomass may be a herb, cornstalks, wood pellets, or the like.

The biomass may be at least one of second generation, third generation biomass, and combustible solid waste.

The combustible solid waste may include waste paper, agricultural waste, scrap wood, vegetable residue, herbaceous waste, and the like.

Class

2 and 3 Waste wood (Class 2: Waste wood that has been contaminated with or contaminated with adhesives, paints, oils, and concrete during processing, processing, or use (except for halogenated organic compounds and waste wood treated and contaminated with preservatives) ), Class 3: Waste wood that has been or is contaminated with halogenated organic compounds or preservatives during the processing process and quality grade of solid fuel products as defined in Article 20-3, Paragraph 2 of the Enforcement Rule of the Law Concerning the Promotion of Reduction and Recycling of Resources Waste wood chips that do not meet the criteria, and other waste wood that does not fall in classes 1 to 2 above). (Ministry of Environment Notification No. 2012-117)

The predetermined size may be 500 mm or less.

Preferably from 10 mu m to 300 mm or less.

More preferably 20 mm to 50 mm or less.

If the particle size is out of the above range, the pulverization cost may be excessively high, or the efficiency of the fusion and removal of the high temperature corrosion-inducing component may be lowered.

The crushing unit may perform crushing and / or grinding. The crushing unit can use any of physical characteristics such as compression, impact, friction, shearing and bending, and the method is not limited as long as it can achieve the purpose of reducing the size of the biomass such as cutting and enlarging the surface area.

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

The raw material supply feeder is not particularly limited as long as it can supply the raw material quantitatively to the downstream end. Preferably, there are a screw feeder and a lock hopper.

The fusion and high-temperature corrosion-inducing components are physically and chemically adhered to the surface of the reactor wall, the heat exchanger, and the downstream-end flue-gas treating facility of the downstream reaction stage among the inorganic components contained in the biomass used in the combustion reaction to generate fouling, slagging, , Cracking, and the like.

The fusing and hot corrosion-inducing component may be an alkali, alkaline earth metal, or a halogen group element.

Preferably, it may be sodium, potassium or chlorine.

The temperature of the injection water for the hot water treatment at the predetermined temperature may be 0 to 100. And preferably from 40 to 80. [ The time for the feedstock to stay in the fusing and hot corrosion-inducing component separation unit may be 10 minutes to 2 hours.

Beyond the above temperature and time conditions, the efficiency of the removed component is low or the process cost is high.

The amount of heat input per unit feedstock varies depending on the type of biomass, and may be defined as BTW (Biomass to Water, kg / kg). Preferably 0.02 to 0.5, and more preferably 0.11 to 0.18 (based on weight, wood pellet, corn vs. 1/6).

If the BTW ratio is exceeded, the separation efficiency of the induced component becomes low.

The blending condition may be 1 wt% to 50 wt% of the conventional fossil fuel. , Preferably from 3 wt% to 40 wt%, and more preferably from 5 wt% to 30 wt%.

The fusion component and the hot corrosion-inducing component may be included in the liquid component discharged from the fusion-bonding and high-temperature corrosion-inducing component separation unit.

The liquid component may be an aqueous solution containing a small amount of organic compounds and fusion and hot corrosion-inducing components. The organic compound may include carbon, hydrogen, nitrogen, oxygen, and sulfur. Preferably, the liquid component may comprise hemicellulose, organic acid, furfural, 5-hydroxymethylfufural (5-HMF) and inorganic.

The solid phase component discharged from the fusing and high temperature corrosion-inducing component separating unit may include a combustible component in which the fusion-bonding and high-temperature corrosion-inducing component are separated.

The combustible component may be an organic compound. The combustible component may include carbon, hydrogen, nitrogen, oxygen, and sulfur.

The pH of the liquid component may be 6 or less.

More preferably, the pH may be 2.5 to 4 or less.

The pH of the liquid component has a technical feature that the pH is lowered by the organic acid in the raw material. Examples of the organic acid include acetic acid, formic acid, propanoic acid, 4-hydroxybutanoic acid, and 2-butenoic acid.

In addition, acetic acid (C ₂ H ₄ O ₂ ), formic acid (HCOOH), propanoic acid (CH ₃ CH ₂ COOH), 4-hydroxybutanoic acid, It is possible to add at least one of 2-butenoic acid, sulfuric acid (H2SO4), hydrochloric acid (HCl), nitric acid (HNO3), phosphoric acid (H3PO4), peracetic acid (C2H4O3), acetic acid (CH3COOH), oxalic acid (C2H2O4) have.

The added amount of the acid solution may be 10 wt% or less with respect to the total amount of applied heat.

The pH by adding the acid solution may preferably be 4 or less.

More preferably, the pH may be 2.5 to 4 or less.

The aqueous solution having a low pH, from which the organic compound in the liquid component is separated, may be recycled to the fusion and hot corrosion-inducing component separation unit (401).

In order to remove the organic compound from the liquid component, at least one of centrifugal separation, flocculation, adsorption, filtration membrane and ion exchange resin may be applied.

The semi-carbonizing unit may include a fuel storage device, a transfer device, and a raw material collecting part in which the fusing and hot corrosion-inducing components are removed through rotation.

The inside of the rotator may include an inner rotating tube. The ratio of the outer diameter of the inner rotating tube to the inner diameter of the rotating tube may be 0.9 or less. Preferably, the ratio of the outer diameter of the inner rotating tube to the inner diameter of the rotating body may be 0.6 or less. The carbonization efficiency may be effective only within the above-described range of the diameter ratio.

The rotation of the inner rotary tube may be opposite to the rotation direction of the rotary shaft. The inner rotating tube may have a concavoconvex shape or a screw shape. The raw material collecting part may include a pressure and / or temperature sensor.

The raw material collecting portion may include a gas discharge valve.

The raw material collecting unit may include a load cell.

The raw material collecting part may include a gas concentration sensor.

The semi-carbonization temperature of the inner rotating tube of the semi-carbonization unit may be from 150 to 250. Preferably from 180 to 230, and more preferably from 190 to 210. [ Outside the semi-carbonization temperature range, the raw material may be completely carbonized or its volume, calorific value, and crushability may be deteriorated.

The semi-carbonization condition of the semi-carbonization unit may be performed on an inert gas.

And may further comprise a recycle unit for separating the liquid component of the organic compound.

The recycling unit may be any one or more of a microfilter, an ultrafilter, a nanofilter, and a reverse osmosis membrane. In addition, water, an acidic solution, and a basic solution can be injected to the front end or the rear end of the recirculation unit for adjusting pH and concentration. Further, the solid component in the liquid phase component can be separated at the front end or the rear end of the recirculation unit by using at least one of water evaporation, centrifugal separation, precipitation, precipitation, agglomeration, and adsorption. Hemicellulose in the liquid component can be separated and used as dietary fiber.

Any one or two units of the cleaning unit and the moisture removal unit for cleaning may be added to the downstream of the fusion and high-temperature corrosion-inducing component separation unit.

The gas phase component discharged from the semi-carbonization unit may include an organic compound including an acid gas.

The organic compound may be used as a heat source for the semi-carbonized fuel production system for the boiler. The organic compound may include hemicellulose, acid gas, furfural, pyrolysis flammable gas, and the like. The organic compound may be used as a heat source in a semi-carbonized fuel production system for boilers for improving the biomass mixing ratio.

In the semi-carbonized fuel production system for a boiler for improving the biomass mixing ratio, the semi-carbonized fuel may be mixed with less than 50 parts by weight in a boiler using fossil fuel.

The semi-carbonized fuel may be in the range of 0.01 to 0.5 in the boiler using fossil fuel.

Preferably 0.05 to 0.4. More preferably 0.3. If the above horn consumption is exceeded, problems such as fouling, clinker, piping erosion and the like may be caused due to corrosive and low melting point substances present on the coarse fuel.

A first step of forming the biomass into a raw material of a predetermined size in the crushing unit (100); A second step of storing the raw material in the hopper 200; A third step of supplying the raw material stored in the hopper to a downstream end of the raw material feeder 210 in a fixed amount; A fourth step of treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximally separate the fusion-induced and high-temperature corrosion-inducing components after combustion in the component separation unit 300; A fifth step of pelletizing the fuel in which the fusing and hot corrosion-inducing components are separated in the component separating unit, in the pelletizing unit (400); And a sixth step of carbonizing the pelletized fuel in the pelletizing unit in the semi-carbonization unit 500. The method may further include a step of producing a semi-carbonized fuel for boiler for improving the biomass mixing ratio.

A crushing unit (102) for forming feedstock into a raw material of a predetermined size; A hopper 202 for storing the raw material; A raw material feeder 212 for feeding the raw material stored in the hopper to a downstream end in a fixed amount; And a fouling-inducing component separation unit (302) for treating the fouling-inducing component of the raw material supplied from the raw material feeder with hot water at a predetermined temperature so as to maximally separate the fouling- And may be a fuel production system in which the ring inducing component is removed.

The feedstock may be any one or more of fossil fuel, biomass, and combustible solid waste.

Preferably, it may be a mustard, a corn stand, or a wood pellet.

The feedstock may be second generation and / or third generation biomass.

Flammable solid wastes may include waste paper, agricultural waste, scrap wood, vegetable residues, and herbaceous waste.

2 and 3 grade waste wood (grade 2: processing · · treatment · waste wood which has been contaminated with or contaminated with adhesive, paint, oil, concrete etc. during its use (treated with halogenated organic compounds or preservatives · contaminated waste Grade 3: waste wood that has been or is contaminated with halogenated organic compounds or preservatives during processing, and solid fuel products as defined in Article 20-3 (2) of the Enforcement Rule of the "Act on the Promotion of the Reduction and Recycling of Resources" And other waste wood that does not fall within Classes 1-2 of the above). (Ministry of Environment Notification No. 2012-117)

The predetermined size may be 500 mm or less.

Preferably from 10 mu m to 300 mm or less.

More preferably 20 mm to 50 mm or less.

If the particle size is out of the range, the pulverization cost may be excessive or the removal efficiency of the fouling-inducing component may be lowered.

The fouling-inducing component physically and chemically attaches to the surface of the reactor wall, the heat exchanger, and the downstream-end flue-gas treating facility in the downstream of the reaction among the inorganic components contained in the feedstock used for the combustion reaction to form fouling, slagging, And the like.

The fouling-inducing component may be an alkali, an alkaline earth metal, or a halogen group element.

Preferably, it may be sodium, potassium or chlorine.

The temperature of the injection water for the hydrothermal treatment at the predetermined temperature may be 100 to 500. Preferably from 120 to 300, and more preferably from 180 to 220. [ The time for the feedstock to stay in the fouling-inducing component separation unit may be 10 minutes to 2 hours.

The time for the feedstock to stay in the fouling-inducing component separation unit may be 30 minutes.

Beyond the above temperature and time conditions, the efficiency of the removed component is low or the process cost is high. The above effect can be confirmed in FIG.

The amount of heat input per unit feedstock varies depending on the type of biomass, and may be defined as BTW (Biomass to Water, kg / kg). Preferably from 0.02 to 0.5, and more preferably from 0.11 to 0.18 (based on weight, wood pellets, 1 kg / 6 kg of corn).

Additional hot water may be supplied with steam.

The fouling inducing component may be included in the liquid component discharged from the fouling inducing component separating unit.

The liquid component may be an aqueous solution containing a small amount of an organic compound and a fouling-inducing component. The organic compound may include carbon, hydrogen, nitrogen, oxygen, and sulfur. Preferably, the liquid component may comprise hemicellulose, organic acid, furfural, 5-hydroxymethylfufural (5-HMF) and inorganic.

The combustible component may be an organic compound. The combustible component may include carbon, hydrogen, nitrogen, oxygen, and sulfur. The combustible component is characterized in that the carbon fraction of carbon, hydrogen, nitrogen, oxygen and sulfur of the raw material per unit mass is increased and the hydrogen, nitrogen, oxygen and sulfur components are decreased.

The pH of the liquid component may be 6 or less.

More preferably, the pH can be 2.5 to 5 or less.

The pH of the liquid component may be approximately 4.

In order to improve the reactivity of the fouling-inducing component separation unit, acetic acid (C ₂ H ₄ O ₂ ), formic acid (HCOOH), propanoic acid (CH ₃ CH ₂ COOH), 4-hydroxybutanoic acid, 2- at least one of butenoic acid, sulfuric acid (H2SO4), hydrochloric acid (HCl), nitric acid (HNO3), phosphoric acid (H3PO4), peracetic acid (C2H4O3), acetic acid (CH3COOH) and oxalic acid (C2H2O4).

The pH by adding the acid solution may preferably be 4 or less.

More preferably, the pH may be 2.5 to 4 or less.

The aqueous solution having a low pH, from which the organic compound in the liquid component is separated, may be recycled to the fouling-inducing component separation unit (402).

The raw material may be supplied to a pretreatment unit which is treated with an alkali solution before being supplied to the fouling-inducing component separation unit.

The pretreatment solid phase component generated in the pretreatment unit is supplied to the fouling inducing component separation unit, and the pretreatment liquid phase component can be separated and discharged.

The pre-treatment solid phase component may be an organic compound. The combustible component may include carbon, hydrogen, nitrogen, oxygen, and sulfur. The combustible component is characterized in that the carbon fraction of carbon, hydrogen, nitrogen, oxygen and sulfur of the raw material per unit mass is increased and the hydrogen, nitrogen, oxygen and sulfur components are decreased.

The pretreatment liquid phase component may be an aqueous solution containing a small amount of an organic compound and an inorganic substance. The organic compound may include carbon, hydrogen, nitrogen, oxygen, and sulfur. Preferably, the organic compound may be lignin. Preferably, the inorganic material may include at least one of Al, Si, P, Ca, Ti, Mn, and Fe.

And a molded fuel unit for producing the molded fuel by applying the solid phase component.

And may further include a membrane filter unit for separating the liquid component of the organic compound.

The membrane filter unit may be any one or more of a micro filter, an ultrafilter, a nanofilter, and a reverse osmosis membrane. In addition, water, an acidic solution, and a basic solution can be injected to the front or rear end of the membrane filter unit for pH and concentration control. In addition, the solid component in the liquid component can be separated by using one or more methods such as evaporation, centrifugation, precipitation, precipitation, coagulation, and adsorption at the front end or the rear end of the membrane filter unit. Hemicellulose in the liquid component can be separated and used as dietary fiber.

Any one or two units of the cleaning unit and the water removal unit for cleaning may be added to the rear end of the fouling-inducing component separation unit or the pretreatment unit.

And the fuel produced in the fuel production system from which the fouling inducing component for biomass burning and / or confluence in the boiler is removed.

In addition, the biomass refers to lignocellulose-based herbaceous and woody biomass, and the material belonging to the biomass is not limited. It is also apparent that first- or third-generation biomass is also applicable. Cellulose, which is a major component of lignocellulose, is a stable polysaccharide in which glucose is linked by ββ-1,4 bonds. Another major component is a polymer of xylose, which is a pentane. In addition, it is composed of a polymer such as 5-valent arabinose, 6-valent mannose, galactose, glucose, rhamnose, etc. Of a polymer.

Glucan is a generic term for polysaccharides composed of glucose. There are various kinds of polysaccharides depending on the binding style of D-glucose. They are largely divided into α α -glucan and β β-glucan by the arrangement of the adduct carbon atoms. The α α-glucan includes amylose (α α-1,4 bonds), amylopectin (α α-1,4 and α α-1,6 bonds), glycogen (α α-1,4 and α α-1,6 bonds), bacterial dextran (alpha alpha-1,6 linkages) and the like. Representative examples of? beta -glucan include cellulose (beta beta-1,4 linkage), brown alga laminarane beta beta-1,3 linkage, lichen

lignan beta beta

1,3

beta beta beta

1,4 linkage, have.

The liquid component containing xylan includes xylan (xylan). Glucuronoxylan, arabinoxylan, glucomannan, xyloglucan, and the like may be included. The liquid component containing xylan as the above-described components is not limited, and various components may be separated depending on the components of the biomass to be injected.

The acid participating in the reaction are sulfuric acid (H ₂ SO _4), hydrochloric acid (HCl), nitric acid (HNO _3), phosphoric acid (H ₃ PO _4), and acetic acid _{_{_{(C 2 H 4 O 3)}}} , acetic acid (CH ₃ COOH), oxalic acid (C ₂ H ₂ O ₄ ), and the like. The acid is not limited to the acid described above, and any acid which decomposes hemicellulose and cellulose may be used. Examples of the base involved in the reaction include sodium hydroxide, calcium hydroxide, urea, and the like. The base is not limited to the base described, and any base that promotes the reaction characteristics can be used.

The amount of one or more of the enzyme, acid, alkali, and ionic liquid introduced into the fouling-inducing component removing unit may not be injected depending on the reaction conditions.

The fuels from which the fouling-inducing component is removed can be used in a fluidized bed, grate, undifferentiated boiler, gasifier and the like. The clogging phenomenon of clinker fouling due to inorganic components including metal elements in fuel during combustion and gasification, It is possible to eliminate the root cause of the corrosion phenomenon caused by the metal.

The cor stover of FIG. 5 was dried at 45 for storage and crushing of domestic corn borrowed samples. The AHC (200) -1step sample was prepared by 200 hydrothermal reaction of corn stover, water and acetic acid at a ratio of 1: 5.8: 0.6. As a result of industrial analysis, moisture and ash contents (mostly Na, K, Ca, etc.) Were decreased and volatile matter and fixed carbon increased. Elemental analysis showed an increase in carbon, hydrogen, oxygen, nitrogen and sulfur content. The calorific value is characterized by an increase of about 1,200 kcal / kg (based on the lower calorific value) compared to the raw sample.

In the first embodiment, the pretreatment unit is a step of removing ash components such as Si, Al and Ti contained in the biomass. The ratio of biomass: water: NaOH is 1: 7.92: 0.08 and the reaction conditions are 60 and 30 min to be. This 1step can be operated in conjunction or separately according to 2 step process.

Example 2 Step 2 is a step of removing fouling-inducing components such as Na, K, Ca and Cl contained in biomass, wherein the ratio of biomass: water: acetic acid is 1: 7.2: 0.8, 60 min. This 2 step is the main process and may further include a 1step unit.

(Example 1)

It is a process to remove the fouling inducing components such as Na, K, Ca and Cl contained in the biomass. The ratio of water to acetic acid is 1: 7.2: 0.8 and the reaction conditions are 200 and 60 min.

FIG. 7 shows the ash removal rate and the ash composition according to the treatment conditions of the fouling-induced component separation unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed. As a result, it can be seen that ash is reduced by about 62% under the condition of 160-180. The reduced ash content is dominated by NaO, MgO, P ₂ O ₅ , K ₂ O, CaO, MnO and Fe ₂ O ₃ .

8 is a graph showing changes in XMG content and lower calorific value according to processing conditions of the fouling-inducing component separation unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed. As a result, it can be seen that as the temperature increases from 160 to 200, the amount of XMG contained in the solid fuel decreases, while the amount of XMG in the case of 200 is 0%. It can be seen that the calorific value increases as the temperature rises, just like the conditions of other upgraded fuels.

9 is a graph showing the relationship between the amount of ash and XMG in the fouling inducing component separation unit and the amount of XMG in the fouling inducing component separation unit according to the present invention, This shows the change in calorific value. As a result, ash and XMG removal rate and low calorific value increase rate are most suitable for utilization as fuel at 200 and 60 min.

(Example 2)

The pretreatment unit is a process for removing ash components such as Si, Al, and Ti contained in biomass. The ratio of large scale water: water: NaOH is 1: 7.92: 0.08, and reaction conditions are 60 and 30 min.

10 shows the ash removal rate and ash composition according to the treatment conditions of the pretreatment unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed. As a result, it was found that the ash removal was hardly effected under the condition of 40, and the ash was reduced by about 54% under the conditions of 60 and 30 min. The reduced ash content is dominated by Al ₂ O ₃ , SiO ₂ , and TiO ₂ .

11 is a graph showing changes in lignin content and lower calorific value according to processing conditions of the pretreatment unit according to an embodiment of the fuel production system for a boiler in which the fouling-inducing component according to the present invention is removed. As a result, it can be seen that as the temperature increases from 40 to 60, the content of lignin contained in the solid fuel decreases, and the value of calorific value decreases by the loss of lignin as the temperature rises.

12 is a graph showing changes in ash content, lignin content and lower calorific value according to the temperature and the treatment time of the pretreatment unit according to an embodiment of the fuel production system for a boiler in which the fouling- will be. As a result, the ash reduction rate, lignin and low calorific value loss rate are most suitable for utilization as fuel at 60 and 30 min.

FIG. 13 shows NOx, ash removal rate, and heating value increase rate according to the present invention, which is a comparison between solid fuels after being treated with 160 to 200, and it is considered that fuel NOx, ash reduction rate, and heating value increase rate are the most suitable conditions at a temperature of 200 have.

14 and 15, a method for separating a combustible component from a biomass hot-water extract liquid according to a third embodiment of the present invention will be described in detail.

The combustible component through the specification of the present invention means a substance containing carbon such as hemicellulose based polymer material and organic compound extracted from biomass, and the mineral component means a substance which causes corrosion, abrasion and fouling of combustion furnace And represent sodium, potassium and chlorine components representatively.

The method for separating the combustible component from the biomass hot water extract liquid according to the present invention comprises the steps of S-1 for crushing biomass, S-2 for supplying hot water to crushed biomass, S-3 step of separating the solid material into a solid phase material, S-4 step of adding a coal powder to the liquid phase material, S-4 step of supplying the coal and liquid phase material mixture to the first separation means, Step 5, step S-6 of supplying the filtrate from which the coal is removed to the second separating means, obtaining the first concentrate and the first permeate by the second separating means, recovering the first concentrate, And the S-7 step of supplying the permeated liquid to the third separation means, and the S-8 step of obtaining the second concentrated liquid and the second permeated liquid by the third separation means and recovering the second concentrated liquid.

Hereinafter, the configuration of each step will be described in detail.

S-1 step of pulverizing the biomass by crushing means

It is a step of crushing the biomass tissues so that various minerals such as sodium, potassium and chlorine can be easily separated from the biomass.

The crushing means is not particularly limited as long as it can crush the tissues of the biomass to reduce the size and crush the tissues. Preferred examples thereof include a jaw crusher, a gyratory crusher, a roll crusher ), An edge runner, a hammer crusher, a ball mill, a jet mill, and a disk crusher.

Here, the biomass is not particularly limited as long as it contains a soluble component usable as a fuel source, but woody, herbaceous and algae can be preferably used.

Wood chips, wood chips, logs, tree branches, wood crumbs, leaves, wood boards, sawdust, lignin, xylan, lignocellulose, palm kernel, palm kernel shell, palm fiber, empty fruit bunches (EFB) , Fresh fruit bunches (FFB), palm leaves and the like, and herbaceous plants include cornstalks, rice straw, crockery, sugarcane, grain (rice, millet, coffee etc.) husks, candy leaves, bagasse, Bio such as chalk, molasses, flax, hemp, sheep, cotton stalks, tobacco stalks, corn starch, potatoes, cassava, wheat, barley, lime mill and other starch processing residues, avocados, jatropha and their processed residues Mass may be used but is not limited thereto.

The algae may be green algae, cyanobacteria, diatoms, red algae, Chlorella, Spirulina, Dunaliella, Porphyridium, Phaeodactylum and the like.

Step S-2 for supplying hot water to the crushed biomass

In order to separate various minerals such as sodium, potassium and chlorine from the biomass, hot water is supplied to the pulverized biomass.

The biomass contains lignin, cellulose, hemicellulose, and various minerals that cause burning problems. When hot water having a predetermined temperature is supplied to the crushed biomass to be reacted, various kinds of biomass Mineral components are separated into soluble or insoluble state in hot water.

If the minerals can be extracted and separated from the biomass, the temperature of the hot water is not particularly limited, but may be preferably from 100 ° C to 500 ° C, more preferably from 120 ° C to 300 ° C, Lt; 0 > C to 220 < 0 > C.

If the temperature of the hot water is less than 100 ° C, the minerals are not well separated and the reaction time becomes too long. On the contrary, when the temperature exceeds 500 ° C, It is preferable to supply hot water.

The reaction time of the hot water and the biomass is not particularly limited, but is preferably 30 minutes to 2 hours.

And more preferably in a reactor maintained at a high pressure in the step of supplying the hot water.

Step S-3, which separates the biomass supplied with hot water into a liquid phase material and a solid phase material

When the hot water is supplied and reacted, various minerals contained in the biomass are separated. That is, various minerals are present in hot water in a soluble state, but since the biomass from which the mineral components are separated still remains as a solid phase, by separating the biomass from the hot water containing the mineral component and the mineral component, Biomass, a solid material, can be used directly as a heating source.

As a method of separating the solid phase material containing the hydrothermal fluid and the biomass having a greatly reduced content of the mineral component from each other, a known separation method capable of separating the liquid phase material and the solid phase material can be used. For example, Mesh networks smaller than the particle size of the mass may be used, but are not limited thereto.

Step S-4 to add coal to the liquid phase material

On the other hand, the liquid substance containing hot water contains a large amount of carbon components which are useful as heat sources such as hemicellulose based pentose as well as mineral components separated from biomass.

In the present invention, a step of adding a powder to the liquid phase material is carried out in order to separate carbon components such as pentose from the liquid phase material, which causes a problem in combustion and a useful heating source.

It is possible to separate the carbon components such as pentane from the liquid phase material because the carbon components such as pentose are easily adsorbed on the surface or pores of the coal because of high adhesion.

Here, the pulverized coal is preferably 10 탆 to 10 탆, more preferably 70 탆 to 5 탆.

If the particle diameter of the coal powder is less than 10 탆, it is not easy to separate the powder from the liquid material. On the other hand, if the particle diameter exceeds 10 mm, the specific surface area of the coal powder is small, Is preferably in the above range.

The mixing ratio of the pulverized liquid material to the pulverized liquid material is preferably 1: 1 to 1:10. It is very difficult to separate the powder from the slurry when the powder is added in an excessively large amount. On the contrary, when the powder is added in an excessively small amount, the adsorption amount can be greatly reduced. Therefore, .

On the other hand, it is preferable to stir the powder and the liquid material using known agitation means so that the adsorption rate of the combustible component can be increased after the powder is added to the liquid phase material.

S-5 step of supplying the mixture of pulverized and liquid material to the first separation means to recover the pulverized coal and obtaining a pulverized filtrate

And separating and recovering the coal from the mixture of the coal and the liquid phase material. The surface or pores of the pulverized coal are mainly adsorbed by a pentacarbon-containing combustible material containing carbon, but since they contain substantially no mineral components, they can be used directly as a heating source such as a boiler.

Here, it is preferable that the first separation means for separating the pulverized material from the liquid phase material is filtrated through a filter net using the sieve separation effect. In other words, a filter net having a pore size which does not pass through the pulverizer but can pass through the liquid phase material can be used in consideration of the particle size of the added pulverized coal. For example, if the particle diameter of the pulverized coal is 10 μm or more, it is preferable to use a filter net having a size of less than 10 μm. If the coal is 70 μm or more, a filter net having a size of less than 70 μm can be used.

On the other hand, when the pulverized coal is separated from the pulverized liquid material, separation by its own weight. More specifically, the liquid material and pulverized coal can be separated by the own gravity of the water. It is also possible to separate the powder by injecting a mixture of the powder and the powdery material into a closed container provided with the filter net, and then applying pressure to discharge the liquid material out of the closed container. In addition, it is also possible to separate the pulverized coal by injecting a mixture of pulverized material and liquid material into an open container provided with the filter net, and then sucking and discharging only the liquid material.

Conventionally, a separation membrane filtration process has been studied to separate minerals from a mixture of liquid materials. However, since the liquid phase material contains a large amount of a pentane-containing combustible component having a relatively large molecular weight, . On the other hand, in the present invention, it is advantageous to easily recover flammable components per pentane by addition of the pulverized coal and to improve the permeation performance of the separator in the separator coupling process.

Step S-6 for supplying the filtrate from which the pulverized coal has been removed to the second separation means

Although it is possible to recover a certain amount of combustible carbon components from the liquid phase material reacted with the biomass by addition of coal, the flammable material may still be present in the pulverized filtrate.

Therefore, it is preferable to recover the combustible material remaining in the filtrate from which the coal is removed by using the second separation means.

Here, the second separating means is preferably an ultrafiltration membrane or a microfiltration membrane which transmits a mineral component but does not permeate a combustible substance. As described above, it is very easy to recover the combustible material by the second separating means because a large amount of pentane-containing combustible fraction contained in the liquid phase material and having a relatively large molecular weight is recovered by the pulverization.

S-7 step of obtaining a first concentrated liquid and a first permeated liquid by the second separation means, recovering the first concentrated liquid, and supplying the first permeated liquid to the third separation means

When the filtrate from which the coal is removed is supplied to the second separation means, the pentane-like combustible component can not permeate the filtration membrane, while the mineral component permeates the first filtrate containing the combustible component and the first permeate containing the mineral component It is possible to separate.

Since the first concentrate contains substantially no mineral components, it can be used as a heating source. On the other hand, a low-molecular combustible component which is not recovered by the second separating means together with the mineral component may remain in the first permeated liquid.

The third separating means can be used for the purpose of completely recovering the remaining low-molecular-weight combustible components as described above. Preferably, the third separation means is a nanofiltration membrane or a reverse osmosis membrane.

It is very easy to recover the combustible material remaining by the third separating means because a large amount of the pentane peroxide contained in the liquid phase material has a relatively large molecular weight and is recovered by the second separating means.

Step S-8 for obtaining the second concentrated liquid and the second permeated liquid by the third separation means and recovering the second concentrated liquid

When the first permeated liquid is supplied to the third separating means, the remaining combustible components can not pass through the filtration membrane, whereas the mineral component permeates, so that the second concentrate containing the combustible component and the second permeate containing the mineral component are separated It is possible.

The second concentrate can be used as a heating source because it contains substantially no mineral components, while the second permeate contains only minerals, and thus can be used for toilet, washing, and the like.

Hereinafter, with reference to FIG. 16, a method for separating a combustible component that does not substantially contain a metal ion component from a biomass hot water extraction solution according to a fourth embodiment of the present invention will be described in detail.

A method for separating a combustible component according to the fourth embodiment of the present invention comprises the steps of S-1 for crushing biomass as crushing means, S-2 for supplying hot water to the crushed biomass, Step S-3 of separating the biomass into a liquid phase material and a solid phase material, step S-4 'of centrifuging the liquid phase material, and step S-5' of recovering the concentrated slurry and obtaining a supernatant liquid.

Unlike the third embodiment, the fourth embodiment differs from the third embodiment in that a combustible component is recovered by centrifuging the liquid phase material.

That is, steps S-1 to S-3 are the same as those of the first embodiment, but the liquid phase material is centrifuged (step S-4 ') to separate the concentrated slurry corresponding to the combustible component and the supernatant containing the mineral component (Step S-5 ').

Of course, when the combustible component remains in the supernatant obtained in the step S-5 ', it is obvious that the steps S-6 to S-8 of the example 3 can be selectively performed.

Having described specific portions of the present invention in detail, those skilled in the art will appreciate that these specific descriptions are only for the preferred embodiment and that the scope of the present invention is not limited thereby. It will be obvious. It is therefore intended that the scope of the invention be defined by the claims appended hereto and their equivalents.

100: first processing unit

200: second processing unit

300: third processing unit

400: fourth processing unit

500: fifth processing unit

600: hydrothermal treatment unit

610:

620:

700: Enzyme saccharification unit

800: Extraction unit

900: Spraying generating unit

1000: coal pretreatment unit

1100: coal granulation unit

1200: forming fuel unit

1300: Semi-carbonization unit

1400: recirculation unit

101: Crushing unit

201: Hopper

211: feed feeder

301: fusion welding and high temperature corrosion inducing component separation unit

* 401: Pelletizing unit

501: Half Carbonization Unit

102: Crushing unit

202: Hopper

212: feed feeder

302: Fouling inducing component separation unit

402: Membrane filter unit

* In addition, clinker fouling expected from ash due to biomass after combustion and gasification in fluidized bed and undifferentiated combustion furnaces and gasification furnaces, using ash-free biomass cellulose, hemicellulose and lignin to produce molded fuel and semi- And the problem of high temperature corrosion can be basically eliminated.

Claims

In a composite fuel production system using ashfree biomass,

A first processing unit (100) for processing the biomass with first treated water containing hot water at a predetermined temperature and pressure; And

A second processing unit (200) for generating liquid and solid components from the biomass treated in the first treatment unit by second treatment water containing hot water of a predetermined temperature and pressure;

Wherein the ash-free biomass is used to produce a composite fuel.
The apparatus according to claim 1, further comprising: a third processing unit (300) for selectively adding a pH adjusting agent so that the liquid component processed in the second processing unit has a predetermined pH;

Wherein the ash-free biomass is used to produce a composite fuel.
The apparatus according to claim 2, further comprising: a fourth processing unit (400) for separating the liquid component processed in the third processing unit from the ash-free concentrated component present in the processed liquid component using a predetermined solid-liquid separating device;

Wherein the ash-free biomass is used to produce a composite fuel.
The method according to claim 1, further comprising a fifth processing unit (500) for processing the solid-phase components processed in the second processing unit with hot water of a predetermined temperature and pressure Fuel production system.
The method according to any one of claims 1 to 5, wherein the solid-phase component treated in the second treatment unit or the fifth treatment unit is treated with hot water and high-pressure hot water to produce a liquid fiber component comprising a solid fiber component including cellulose and hemicellulose A hydrothermal processing unit (600); Wherein the ash-free biomass is used for producing a composite fuel using the ash-free biomass.
[Claim 6] The method according to claim 5, further comprising a first discharging part (610) for discharging and separating the solid fiber component in a process of collecting steam discharged from the low pressure area of the hydrothermal treatment unit without air contact, Combined fuel production system using prebiomass.
[Claim 6] The method according to claim 5, further comprising: a second discharge unit (620) for discharging and separating the fiber liquid fraction in a process of collecting steam discharged from the other end of the hydrothermal treatment unit Combined fuel production system using prebiomass.
[7] The method according to claim 6, further comprising an enzyme saccharification unit (700) for performing an enzymatic saccharification reaction for the production of bioethanol, the solid fiber fraction containing cellulose discharged from the first discharge unit Composite fuel production system using mass.
8. An extraction unit (800) for extracting acetic acid in a predetermined amount from a fiber liquid fraction containing hemicellulose treated in the hydrothermal treatment unit and recycling it to the fifth treatment unit and / or the hydrothermal treatment unit Wherein the ash-free biomass is used to produce a composite fuel using the ash-free biomass.
The method as set forth in claim 9, further comprising a spraying generating unit (900) for generating a spraying solution at a predetermined concentration using the fiber liquid fraction treated in the extracting unit Composite fuel production system.
The coal pretreatment unit (1000) according to claim 10, wherein the coal pretreatment unit (1000) for impregnating or coating coal having an average particle size of 4 mm or more among coarsely crushed coal using the spray solution produced through the spraying generation unit; Wherein the ash-free biomass is used for producing a composite fuel using the ash-free biomass.
11. The method according to claim 10, wherein the spray solution is sprayed onto the coal while rotating the coal having an average particle size of less than 4 mm among the coarsely pulverized coals using the spray solution generated through the spraying generating unit so that the coal is impregnated or coated, A coal granulation unit 1100 that increases its size through granulation; Wherein the ash-free biomass is used for producing a composite fuel using the ash-free biomass.
The method as claimed in claim 3 or 4, wherein the ash-free concentrated fraction separated from the fourth treatment unit is bound to a solid-phase component processed in the fifth treatment unit with a hydrophobic binder, (1200); Wherein the ash-free biomass is used for producing a composite fuel using the ash-free biomass.
The image forming apparatus according to any one of claims 1, 2, and 4, wherein one of the first processing unit, the second processing unit, the fourth processing unit, and the fifth processing unit, Wherein a cleaning unit and a moisture removal unit for washing are added to one or two units of the ash-free biomass.
The composite fuel producing system using ash pre-biomass according to claim 5, wherein one or two units of a washing unit and a moisture removing unit for washing are added to the rear end of the hydrothermal treatment unit.
The method according to any one of claims 3 and 4, wherein the ash-free concentrated fraction separated from the fourth treatment unit is subjected to heat treatment of the solid phase component treated in the fifth treatment unit with a hydrophobic binder, Unit 1300; Wherein the ash-free biomass is used for producing a composite fuel using the ash-free biomass.
The method according to claim 3 or 4, wherein the ash-free concentrated component separated in the fourth treatment unit and / or the solid-phase component treated in the fifth treatment unit are selectively added to the combustion or gasification fuel, the adhesive, the particle board and the plywood In the manufacture of phenol formaldehyde resin thickeners and molding compounds, the use of urethane and epoxy resins, antioxidants, release agents, flow control agents, cement / concrete blends, gypsum board manufacturing, oil drilling, (Phenol) monomers, an additional variety of monomers, carbon fibers, metal removal from solution, gel formation bases, polyurethane copolymers, polyvinyl chloride, polyvinylpyrrolidone, polyvinylpyrrolidone, And combinations thereof. &Lt; RTI ID = 0.0 > 8. < / RTI >
4. The apparatus of claim 3, further comprising a recirculation unit (1400) recirculating the first liquid to the first processing unit and / or the second processing unit, wherein the liquid separator comprises an inorganic material separated from the liquid component via the fourth processing unit Wherein the biomass-containing complex fuel production system comprises:
The bioethanol produced by the system for producing a complex fuel using ash-free biomass, which further comprises the enzyme saccharification unit of claim 8.
The coal produced by the composite fuel production system using ash-free biomass, further comprising the coal pretreatment unit of claim 11.
A coal produced by a composite fuel production system using ashfree biomass, further comprising the coal granulation unit of claim 12.
An ash-free shaped fuel produced by a composite fuel production system using ash-free biomass, further comprising the shaped fuel unit of claim 13.
An ash-free semi-carbonized fuel produced by a composite fuel production system using ash-free biomass, further comprising the semi-carbonization unit of claim 16.
The method according to any one of claims 2 and 3, wherein the inorganic substance-containing liquid fraction pretreated in the first treatment unit and eluted from the inorganic component containing metal in the biomass is supplied to the third treatment unit or the fourth treatment unit Combined fuel production system using ashfree biomass.
A crushing unit 101 for forming the biomass into a raw material of a predetermined size;

A hopper 201 for storing the raw material;

A feedstock supply feeder 211 for feeding the feedstock stored in the hopper to a downstream end of the feedstock;

A component separation unit (301) for treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximize the fusion-welding and high-temperature corrosion-inducing components after combustion;

A pelletizing unit (401) for pelletizing the separated fuel in the component separating unit; And

And a semi-carbonization unit (501) for carbonizing the pelletized fuel in the pelletizing unit

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
A crushing unit 101 for forming the biomass into a raw material of a predetermined size;

A hopper 201 for storing the raw material;

A feedstock supply feeder 211 for feeding the feedstock stored in the hopper to a downstream end of the feedstock;

A component separation unit (301) for treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximize the fusion-welding and high-temperature corrosion-inducing components after combustion;

A semi-carbonization unit 501 for carbonizing the fuel from which the fusion and hot corrosion-inducing components supplied from the component separation unit are removed,

A pelletizing unit (401) for pelletizing the semi-carbonized fuel in the semi-carbonizing unit; Containing

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
27. The method of claim 25 or 26,

Wherein the liquid phase component discharged from the component separation unit includes the fusion welding and high temperature corrosion inducing component

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
27. The method of claim 25 or 26,

Wherein the solid phase component discharged from the component separating unit comprises a combustible component in which the fusion-bonding and high-temperature corrosion-inducing component are separated

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
27. The method according to claim 25 or 26,

Wherein the pH of the liquid component discharged from the component separation unit is 6 or less

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
30. The method of claim 29,

Characterized in that an organic compound in the liquid component is separated and recycled to the component separation unit

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
27. The method of claim 25 or 26,

The gas phase component discharged from the semi-carbonization unit includes an organic compound including an acid gas

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
27. The method of claim 25 or 26,

Characterized in that the semi-carbonized fuel in a boiler semi-carbonized fuel production system for improving the biomass mixing ratio can be mixed up to 50 parts by weight or less in a boiler using fossil fuel.
A crushing unit 101 for forming the biomass into a raw material of a predetermined size;

A hopper 201 for storing the raw material;

A feedstock supply feeder 211 for feeding the feedstock stored in the hopper to a downstream end of the feedstock;

A carbonization unit (501) for carbonizing the fuel supplied from the raw material feeder;

A pelletizing unit (401) for pelletizing the semi-carbonized fuel in the semi-carbonizing unit; And

A component separation unit (301) for treating the raw material supplied from the pelletizing unit with hot water at a predetermined temperature so as to maximally separate the fusion-welding and high-temperature corrosion-inducing components from the raw material supplied from the pelletizing unit;

Containing

A system for the production of semi - carbonized fuel for boilers for improving the biomass mixing rate.
A first step of forming the biomass into a raw material of a predetermined size in the crushing unit 101;

A second step of storing the raw material in the hopper 201;

A third step of feeding the raw material stored in the hopper to a downstream end of the raw material feeder 211 in a fixed amount;

A fourth step of treating the raw material supplied from the raw material supply feeder with hot water at a predetermined temperature so as to maximally separate the fusion-induced and high-temperature corrosion-inducing components after combustion in the component separation unit 301;

A fifth step of pelletizing the fuel in which the fusing and hot corrosion-inducing components are separated in the component separating unit, in the pelletizing unit (401); And

And a sixth step of carbonizing the pelletized fuel in the pelletizing unit in the semi-carbonizing unit (501)

Production method of semi - carbonized fuel for boiler for improving biomass mixing ratio.
A crushing unit (102) for forming feedstock into a raw material of a predetermined size;

A hopper 202 for storing the raw material;

A raw material feeder 212 for feeding the raw material stored in the hopper to a downstream end in a fixed amount;

And a fouling-inducing component separation unit (302) by treating the fouling-inducing component of the raw material supplied from the raw material feeder with hot water of a predetermined temperature so as to maximally separate the fouling-

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
36. The method of claim 35,

And the fouling inducing component is contained in the liquid component discharged from the fouling inducing component separating unit

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
36. The method of claim 35,

And the solid phase component discharged from the fouling-causing component separation unit includes a combustible component in which the fouling-inducing component is separated

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
37. The method of claim 36,

Wherein the pH of the liquid component is 6 or less

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
39. The method of claim 38,

Characterized in that an aqueous solution having a low pH, from which the organic compound is separated from the liquid component, is recycled to the fouling-induced component separation unit

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
36. The method of claim 35,

Characterized in that the raw material is supplied to a pretreatment unit (402) which is treated with an alkali solution before being fed to the fouling-inducing component separation unit

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
39. The method of claim 38,

Wherein the pretreatment solid-phase component generated in the pretreatment unit is supplied to the fouling-inducing component separation unit,

The pretreatment liquid phase component is separated and discharged.

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
39. The method of claim 37,

And a molded fuel unit for producing the molded fuel by applying the solid phase component

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
40. The method of claim 39,

Characterized by further comprising a membrane filter unit (402) for separating the organic component of the liquid component

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
The washing machine according to claim 35 or 39, wherein one or two units of the washing unit and the water removing unit for washing are added to the rear end of the fouling-inducing component separating unit or the pretreatment unit

A fuel production system that removes fouling-inducing components for biomass burning and / or combustion in a boiler.
45. The fuel according to any one of claims 35 to 44, wherein the fuel produced in the fuel production system has been removed from the boiler for fossil fuels for biomass burning and / or fogging.
A first step of forming a feedstock from a raw material having a predetermined size by using the crushing unit 102;

A second step of storing the raw material in the hopper 200;

A third step of feeding the raw material stored in the hopper to a downstream end of the raw material feeder 212 in a fixed amount; And

And a fourth step of treating the fouling-inducing component separation unit (302) with hot water at a predetermined temperature so that the fouling-inducing component of the raw material supplied from the raw material feeder is separated to the maximum, and / or a biomass burner A method for producing fuel by removing the fouling inducing component for coma.
S-1 step of pulverizing the biomass as a crushing means;

S-2 step of supplying hot water to the crushed biomass;

S-3 step of separating the biomass supplied with hot water into a liquid phase material and a solid phase material;

Adding S-4 to the liquid phase material; And

A method for separating a combustible component from a biomass hot-water extraction liquid, the method comprising: supplying a mixture of coal and a liquid-phase material to a first separation means to recover the coal and obtain a filtrate from which the coal is removed.
49. The method of claim 47,

After the step S-5,

S-6 step of supplying the filtrate from which the pulverized coal is removed to the second separation means; And

And S-7 step of obtaining the first concentrated liquid and the first permeated liquid by the second separation means, recovering the first concentrated liquid, and supplying the first permeated liquid to the third separation means And separating the combustible component from the biomass hot water extract.
49. The method of claim 48,

After the step S-7,

And S-8 step of obtaining a second concentrated liquid and a second permeated liquid by the third separation means and recovering the second concentrated liquid.
49. The method of claim 47,

After the step S-5,

S-7 step of supplying the filtrate from which the pulverized coal is removed to the third separation means; And

And S-8 step of obtaining a second concentrated liquid and a second permeated liquid by the third separation means and recovering the second concentrated liquid.
50. The method according to any one of claims 47 to 50,

Wherein the pulverized coal has a particle diameter of 10 탆 to 10 탆.
52. The method of claim 51,

Wherein the pulverized coal has a particle size of 70 탆 to 5 탆.
50. The method of claim 48 or 49,

Wherein the second separation means is an ultrafiltration membrane or a microfiltration membrane.
51. The method according to any one of claims 48 to 50,

Wherein the third separation means is a nanofiltration membrane or a reverse osmosis membrane.
S-1 step of pulverizing the biomass as a crushing means;

S-2 step of supplying hot water to the crushed biomass;

S-3 step of separating the biomass supplied with hot water into a liquid phase material and a solid phase material;

S-4 'for centrifuging the liquid material; And

Wherein the concentrated slurry is recovered and comprises a step S-5 'to obtain a supernatant.