KR101739859B1 - Coal briquettes, method for manufacturing the same and method for manufacturing molten iron - Google Patents

Abstract

A method for producing the same, and a method for manufacturing molten iron. The briquettes are charged into the dome portion of the melter-gasifier and rapidly heated in a molten steel making apparatus including i) a melter-gasifier furnished with reduced iron and ii) a reducing furnace connected to the melter-gasifier furnace and providing a reduced iron. The method for producing molded coal comprises the steps of: i) providing pulverized coal, ii) mixing powdered cellulose ether compound with pulverized coal to provide a mixture, iii) adding water to the mixture and mixing, and iv) And molding the resulting mixture to provide a molded charcoal. In the step of providing the molded charcoal, the amount of the cellulose ether compound contained in the molded charcoal is 0.7 wt% to 2.0 wt%.

Description

TECHNICAL FIELD [0001] The present invention relates to a method for producing molten iron,

The present invention relates to a briquette, a method of manufacturing the same, and a method of manufacturing a molten iron. More particularly, the present invention relates to a method of manufacturing a shaped coal using a powdered cellulose ether compound as a binder, a method for producing the same, and a method for producing a molten iron.

In the melt reduction steelmaking method, a melting furnace for melting iron ores and a reduced iron ore is used. When molten iron ore is melted in a melter-gasifier, molten coal is charged into the melter-gasifier as a heat source for melting iron ore. Here, the reduced iron is melted in a melter-gasifier, converted to molten iron and slag, and then discharged to the outside. The briquetted coal charged into the melter-gasifier furnishes a coal-filled bed. Oxygen is blown through the tuyere installed in the melter-gasifier, and then the coal-packed bed is combusted to generate combustion gas. The combustion gas is converted into a hot reducing gas while rising through the coal packed bed. The high-temperature reducing gas is discharged to the outside of the melter-gasifier and supplied to the reducing furnace as a reducing gas.

Molded coal is produced by mixing pulverized coal and binder and then compressing. It is necessary to produce briquettes having excellent cold strength and hot strength in order to use them in the manufacture of molten iron. Therefore, a molded product is produced using a binder having an excellent viscosity such as molasses.

A cellulose ether compound is used as a binder to provide a molded coal having excellent hot strength and cold strength. Further, a method for producing the above-described molded charcoal is provided. And a method for manufacturing molten iron including the above-described method for producing molten iron.

The briquette according to one embodiment of the present invention is charged into a dome portion of a melter-gasifier in a molten iron manufacturing apparatus including i) a melter-gasifier furnished with reduced iron, and ii) a reducing furnace connected to a melter- And rapidly heated. The method for producing molded coal comprises the steps of: i) providing pulverized coal, ii) mixing powdered cellulose ether compound with pulverized coal to provide a mixture, iii) adding water to the mixture and mixing, and iv) And molding the resulting mixture to provide a molded charcoal. In the step of providing the molded charcoal, the amount of the cellulose ether compound contained in the molded charcoal is 0.7 wt% to 2.0 wt%.

More preferably, the amount of the cellulose ether compound may be from 0.8 wt% to 1.5 wt%. In the step of providing the briquette, the amount of moisture contained in the briquette may be 5 wt% to 15 wt%. More preferably, the amount of moisture contained in the briquette may be from 7 wt% to 12 wt%.

The ratio of the amount of water contained in the briquettes to the amount of the cellulose ether compound contained in the briquette may be from 5 to 40. Further, the ratio of the amount of water contained in the briquette to the amount of the cellulose ether compound contained in the briquette may be 7 to 20.

In the step of providing the mixture, the average particle size of the cellulose ether compound may be 50 탆 to 100 탆. More preferably, in the step of providing the mixture, the ratio of the average particle size of the pulverized coal to the average particle size of the cellulose ether compound may be 7 to 30. The ratio of the average particle size of the pulverized coal to the average particle size of the cellulose ether compound may be 10 to 20.

The mixing time in the step of providing the mixture is less than the mixing time in the step of adding and mixing water to the mixture, and the mixing time in the step of providing the mixture for the mixing time in the step of adding water to the mixture May be from 2 to 5. The cellulose ether compound is at least one selected from the group consisting of methyl cellulose (MC), hydroxyethyl cellulose (HEC), hydroxypropyl cellulose (HPC), hydroxypropyl methyl cellulose (HPMC) and hydroxyethyl methyl cellulose Or < / RTI >

The cellulose ether compound may not contain carboxymethyl cellulose (CMC). The viscosity of the cellulose ether compound may be from 4,000 cps to 80,000 cps. The method for producing a blast furnace according to an embodiment of the present invention may further include drying the mixture after adding water to the mixture and mixing.

A method of manufacturing molten iron according to an embodiment of the present invention comprises the steps of: i) providing a blast furnace produced according to the method described above, ii) providing reduced iron reduced in a reduction furnace, and iii) And charging the gasification furnace to provide molten iron. In the step of providing reduced iron, the reducing furnace may be a fluidized bed type reducing furnace or a packed bed type reducing furnace.

The briquette according to one embodiment of the present invention is charged into a dome portion of a melter-gasifier in a molten iron manufacturing apparatus including i) a melter-gasifier furnished with reduced iron, and ii) a reducing furnace connected to a melter- And rapidly heated. The blast furnace comprises from 0.7 wt% to 2.0 wt% of a cellulose ether compound, from 5 wt% to 15 wt% of water, and the remaining pulverized coal. More preferably, the amount of the cellulose ether compound may be from 0.8 wt% to 1.5 wt%.

By using the cellulose ether compound as a binder, the hot strength and the cold strength of the briquette can be greatly improved. Further, the cellulose ether compound can be used to prevent the alkali from being deposited on the fluidized-bed reduction reactor.

Fig. 1 is a schematic flow chart of a method of manufacturing a briquette according to an embodiment of the present invention.
FIG. 2 is a schematic view of a molten iron manufacturing apparatus using the shaped coal produced in FIG.
FIG. 3 is a schematic view of another molten iron manufacturing apparatus using the shaped coal produced in FIG. 1. FIG.

The terms first, second and third, etc. are used to describe various portions, components, regions, layers and / or sections, but are not limited thereto. These terms are only used to distinguish any moiety, element, region, layer or section from another moiety, moiety, region, layer or section. Thus, a first portion, component, region, layer or section described below may be referred to as a second portion, component, region, layer or section without departing from the scope of the present invention.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the invention. The singular forms as used herein include plural forms as long as the phrases do not expressly express the opposite meaning thereto. Means that a particular feature, region, integer, step, operation, element and / or component is specified and that the presence or absence of other features, regions, integers, steps, operations, elements, and / It does not exclude addition.

Unless otherwise defined, all terms including technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Commonly used predefined terms are further interpreted as having a meaning consistent with the relevant technical literature and the present disclosure, and are not to be construed as ideal or very formal meanings unless defined otherwise.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 schematically shows a flow chart of a method of manufacturing a briquette according to an embodiment of the present invention. The flow chart of the method of manufacturing the briquette of Fig. 1 is merely for illustrating the present invention, and the present invention is not limited thereto. Therefore, the method of manufacturing the briquette can be variously modified. Meanwhile, the structure of the apparatus for manufacturing a briquette for the method of manufacturing the briquette of FIG. 1 can be easily understood by those skilled in the art, and thus a detailed description thereof will be omitted.

As shown in FIG. 1, the method for producing molded coal includes the steps of providing pulverized coal (S10), providing a mixture (S20) of powdery cellulose ether compound, adding water to the mixture and mixing (S30), and molding the mixture to provide a blast (S40). In addition, if necessary, the method of manufacturing the molded coal may further include other steps.

First, in step S10, pulverized coal is provided. As the pulverized coal, raw materials containing carbon such as bituminous coal, subbituminous coal, anthracite, and coke can be used. The particle size of the pulverized coal can be adjusted to 4 mm or less.

Next, in step S20, a mixture is provided by mixing the pulverized coal with the cellulose ether compound. That is, after the cellulose ether compound is added to the pulverized coal, the mixture is mixed well so as to be uniformly mixed.

Here, a powdery cellulose ether compound, not a liquid phase, is used. When a binder solution is used, a carboxymethyl cellulose (CMC) solution having a low viscosity of the binder itself may be used in order to improve flowability. However, since a binder having a low viscosity is used, there is a problem in that the strength of the briquette is lowered. In addition, the binder in the form of a solution has a disadvantage in that it is difficult to uniformly maintain the binder component due to the layer separation, and a special transportation vehicle such as a tanker is required for transportation, which leads to a high shipping cost. Further, since the binder solution is freezing in the winter, it is not easy to store.

In contrast, when a powdery cellulose ether compound is used as a binder, since the viscosity of the cellulose ether compound itself is high, a molded coal having excellent strength can be produced. In addition, since the cellulose ether compound is used in a powder form, its volume can be minimized to facilitate storage, and transportation is advantageous. Furthermore, there is no need to worry about freezing in winter. Therefore, it is suitable to use a powdery cellulose ether compound.

The viscosity of the cellulose ether compound may be 4,000 cps to 80,000 cps. The viscosity of the cellulose ether compound refers to a value obtained by measuring the viscosity of an aqueous solution of a cellulose ether compound having a concentration of 2% by weight at 20 ± 0.1 ° C using DV-II + Pro (spindle HA) from Brookfield. When the viscosity of the cellulose ether compound is too low, the viscosity of the solution containing the cellulose ether compound, for example, the aqueous solution is too low, and the binding force to the pulverized coal is lowered. As a result, the strength of the briquette can be lowered. On the other hand, when the viscosity of the cellulose ether compound is too high, the molecular weight of the cellulose ether compound is too high and the water solubility is lowered, so that the binding force to the pulverized coal is not sufficient. Therefore, it is preferable to adjust the viscosity of the cellulose ether compound to the above-mentioned range.

The cellulose ether compound may include methyl cellulose (MC), hydroxyethyl cellulose (HEC), hydroxypropyl cellulose (HPC), hydroxypropyl methyl cellulose (HPMC) or hydroxyethyl methyl cellulose (HEMC).

Methylcellulose (MC) has a degree of methyl group substitution of 18 to 32 wt%, and hydroxyethyl cellulose (HEC) has a hydroxyethyl substitution degree of 20 to 80 wt%. And hydroxypropyl cellulose (HPMC) has a degree of substitution of hydroxypropyl groups of 20 to 80 wt%, hydroxypropylmethyl cellulose (HPMC) has a degree of methyl group substitution of 18 to 32 wt% and a hydroxypropyl group Degree of substitution. In addition, hydroxyethylmethylcellulose (HEMC) may have a degree of methyl group substitution of 18 to 32 wt% and a degree of substitution of hydroxyethyl group of 2 to 14 wt%.

On the other hand, the average particle size of the powdery cellulose ether compound may be 50 탆 to 100 탆. When the particle size of the powdery cellulose ether compound is too small, the production process ratio is increased. In addition, when the particle size of the cellulose ether compound is too large, the specific surface area of the cellulose ether compound becomes small, and the water solubility thereof lowers, so that the strength of the molded battery produced using the cellulose ether compound may be lowered. Therefore, it is preferable to adjust the particle size of the powdery cellulose ether compound to the above-mentioned range. On the other hand, more specifically, the average particle size of the powdery cellulose ether compound may be 78 탆. In this case, the particle size of the powdery cellulose ether compound may be 97% or more at 0.18 mm or less.

The ratio of the average particle size of the pulverized coal to the average particle size of the cellulose ether compound may be 7 to 30. More specifically, the ratio of the average particle size of the pulverized coal to the average particle size of the cellulose ether compound may be 10 to 20. When the ratio of the average particle size is too large or too small, the cellulose ether compound may not sufficiently exhibit binding ability in the pulverized coal as a binder. Therefore, it is preferable to keep the ratio of the average particle size within the above-mentioned range.

Next, in step S30, water is added to the mixture and mixed. When water is added to a mixture in which the powdery cellulose ether compound is uniformly distributed, the cellulose ether compound dispersed in the pulverized coal is dissolved in water. As a result, the dissolved cellulose ether compound exerts the bonding force with the pulverized coal, and the strength of the molded coal produced in the subsequent process can be greatly improved. As described above, without mixing the liquid binder directly into the pulverized coal, the blended mixture of the pulverized cellulose ether compound and the pulverized coal is mixed with water, and the respective steps are separated to obtain the molded coal having excellent strength and minimizing the processing cost Can be manufactured.

On the other hand, the mixing time in step S30 is larger than the mixing time in step S20. That is, since the pulverized coal and powdered cellulose ether compound are used in step S20, it is possible to uniformly mix even a short time by mixing solid and solid. On the other hand, in step S30, it is necessary to inject the liquid water into the powder-type cellulose ether compound mixed with the pulverized coal to dissolve uniformly in the pulverized coal, so that mixing for a longer time than the step (S20) desirable. More preferably, the ratio of the mixing time in step S30 to the mixing time in step S20 may be from 2 to 5. When the above-mentioned ratio is too small, the powdered cellulose ether compound mixed with the pulverized coal may not sufficiently contact with water, so that the strength of the molded coal may be lowered. Conversely, when the above-mentioned ratio is too large, it is not preferable from the viewpoint of process efficiency. Therefore, it is preferable to appropriately adjust the above-mentioned ratio.

On the other hand, although not shown in Fig. 1, a step of drying the mixture after step S30 may be added. That is, when it is necessary to control the formability of the mixture containing the pulverized coal, the powdery cellulose ether compound and water, the mixture may be dried to remove some moisture. As a result, the strength of the briquettes produced in the subsequent process can be greatly improved.

Finally, in step S40, the mixture is molded to provide a molded charcoal. For example, it is possible to manufacture molded pockets or strips by charging the mixture between a pair of rollers and pressing them. As a result, it is possible to produce briquette having excellent hot strength and cold strength. Here, the amount of the cellulose ether compound contained in the briquette may be 0.7 wt% to 2.0 wt%. More preferably, the amount of the cellulose ether compound may be from 0.8 wt% to 1.5 wt%. If the amount of the cellulose ether compound is too large, the cost of producing the molded-in-a-bobble increases. In addition, when the amount of the cellulose ether compound is too small, sufficient bonding force can not be exhibited, and the strength of the molded-in-fire decreases. Therefore, it is preferable to adjust the amount of the cellulose ether compound to the above-mentioned range.

On the other hand, the amount of moisture contained in the briquette may be 5 wt% to 15 wt%. More preferably, the amount of moisture can be from 7 wt% to 12 wt%. When the amount of water is too large, molding of the mixture is difficult. Further, when the amount of moisture is too small, the cold strength of the briquette can be lowered. Therefore, the amount of water is adjusted to the above-mentioned range.

The blast furnace produced by the above-mentioned method contains 0.7 wt% to 2.0 wt% of a cellulose ether compound, 5 wt% to 15 wt% of water, and the remaining fine coal. More specifically, the amount of the cellulose ether compound may be from 0.8 wt% to 1.5 wt%. Here, when the amount of the cellulose ether compound is too large, the production cost of the briquette is greatly increased. Further, when the amount of the cellulose ether compound is too small, the strength of the briquette is lowered. Therefore, it is preferable to adjust the amount of the cellulose ether compound to the above-mentioned range. In addition, when the amount of water is too large, the moldability of the briquette is deteriorated. Further, when the amount of moisture is too small, the cold strength of the briquette can be lowered. Therefore, the moisture content of the briquettes is regulated to the above-mentioned range.

Fig. 2 schematically shows a molten iron manufacturing apparatus 100 using the shaped coal produced in Fig. The structure of the apparatus for manufacturing molten iron 100 of FIG. 2 is merely for illustrating the present invention, and the present invention is not limited thereto. Therefore, the molten iron manufacturing apparatus 100 of FIG. 2 can be modified into various forms.

The molten iron manufacturing apparatus 100 of FIG. 2 includes a melter-gasifier 10 and a packed-bed reduction reactor 20. Other devices may also be included if desired. In the packed-bed reduction reactor (20), iron ore is charged and reduced. The iron ores to be charged into the packed-bed reduction reactor 20 are pre-dried and then made into reduced iron while passing through the packed-bed reduction reactor 20. The packed-bed reduction reactor (20) is a packed-bed reduction reactor and receives a reducing gas from the melter-gasifier furnace (60) to form a packed bed therein.

Since the briquettes produced by the production method of Fig. 1 are charged into the melter-gasifier 10, a coal-filled layer is formed inside the melter-gasifier 10. A dome portion 101 is formed on the upper portion of the melter-gasifier 10. That is, a larger space is formed compared with other portions of the melter-gasifier 10, and a high-temperature reducing gas is present therein. Therefore, the briquettes charged into the dome portion 601 by the reducing gas at a high temperature are converted into air by the thermal decomposition reaction. The gas generated by the pyrolysis reaction of the blast furnace moves to the lower part of the melter-gasifier 10 and exothermically reacts with the oxygen supplied through the tuyere 30. As a result, the briquettes can be used as a heat source for keeping the melter-gasifier 10 at a high temperature. On the other hand, since the ladle provides air permeability, a large amount of gas generated in the lower portion of the melter-gasifier 10 and the reduced iron supplied from the packed-bed reduction reactor 20 can more easily and uniformly make the coal packed bed in the melter- It can pass.

The lump gasification furnace 10 may be charged with lumpy carbonaceous material or coke as needed in addition to the above-mentioned shaped coal. A tuyere (30) is installed on the outer wall of the melter-gasifier (10) to blow oxygen. Oxygen is blown into the coal packed bed to form a combustion zone. The briquettes can be burned in the combustion zone to generate reducing gas.

Fig. 3 schematically shows a molten iron manufacturing apparatus 200 using the shaped coal produced in Fig. The structure of the molten iron manufacturing apparatus 200 of FIG. 3 is merely for illustrating the present invention, and the present invention is not limited thereto. Therefore, the molten iron manufacturing apparatus 200 of FIG. 3 can be modified into various forms. The structure of the molten iron manufacturing apparatus 200 of FIG. 3 is similar to the structure of the molten iron manufacturing apparatus 100 of FIG. 2, and thus the same reference numerals are used for the same parts, and detailed description thereof is omitted.

3, the molten iron manufacturing apparatus 200 includes a melter-gasifier 10, a fluidized bed reduction reactor 22, a reduced iron compactor 40, and a compacted iron storage tank 50. Here, the compressed reduced iron storage tank 50 may be omitted.

The produced briquettes are charged into the melter-gasifier (10). Here, the briquette generates a reducing gas in the melter-gasifier (10), and the generated reducing gas is supplied to the fluidized-bed reduction reactor (22). The minute iron ores are supplied to a plurality of reduction furnaces 22 having a fluidized bed and are made of reduced iron while flowing by the reducing gas supplied from the melter-gasifier 10 to the fluidized bed reduction reactor 22. The reduced iron is compressed by the reduced iron compactor 40 and then stored in the compacted iron storage tank 50. The compressed reduced iron is charged into the melter-gasifier (10) from the compressed-reduced iron storage tank (50) together with the blast furnace and melted in the melter-gasifier (10). A large amount of gas generated in the lower portion of the melter-gasifier 10 and the compressed reduced iron make the coal filler layer in the melter-gasifier 10 more easily and uniformly distributed in the melter-gasifier 10, To provide good quality molten iron.

On the other hand, as the binder, a cellulose ether compound is used instead of molasses as a binder, so that the alkali component can be remarkably reduced. Therefore, the molasses containing a high alkali component can prevent the clogging of the dispersion plate (not shown) or the cyclone (not shown) in the fluidized-bed reduction reactor 22 by clogging with alkali such as potassium.

Hereinafter, the present invention will be described in more detail with reference to experimental examples. These experimental examples are only for illustrating the present invention, and the present invention is not limited thereto.

Experiment to measure hot and cold strength of briquette

Experimental Example

Pulverized coal having a diameter of 3.4 mm or less and cellulose ether compound having a diameter of 0.2 mm or less were uniformly mixed for 1 minute, then water was added and mixed again for 3 minutes to prepare a mixture. As the pulverized coal, a hard carbon, a tin-free coal and a minute coke were mixed and used. The cellulose ether compound was a product of Samsung Fine Chemical Co., Ltd., hydroxypropyl methylcellulose (HPMC). Then, the mixture was charged into a pair of rolls to produce a blast furnace. In this case, the pair of rolls were pressurized with a pressure of 20 kN / cm to produce a pillow-shaped molded charcoal having a size of 64.5 mm x 25.4 mm x 19.1 mm. The detailed manufacturing process of the remaining briquettes can be easily understood by those skilled in the art, so that detailed description thereof will be omitted.

Experimental Example 1

100 g of pulverized coal having a moisture content of 7.6% and an average particle size of 1.1 mm and 1 g of HPMC powder having an average particle size of 78 탆 and a viscosity of 28,000 cps were first mixed and then added with 10 g of water to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as the above-mentioned experimental example.

Experimental Example 2

100 g of pulverized coal having a moisture content of 7.7% and an average particle size of 1.1 mm and 0.8 g of HPMC powder having an average particle size of 78 탆 and a viscosity of 28,000 cps were mixed first and then 10 g of water was added and mixed again to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Experimental Example 3

100 g of pulverized coal having a moisture content of 1.4% and an average particle size of 1.1 mm and 1 g of HPMC powder having an average particle size of 78 탆 and a viscosity of 28,000 cps were mixed first and then 10 g of water was added and mixed again to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Experimental Example 4

100 g of pulverized coal having a moisture content of 0.1% and an average particle size of 0.9 mm and 1 g of HPMC powder having an average particle size of 78 탆 and a viscosity of 28,000 cps were mixed first and then 10 g of water was added and mixed again to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Experimental Example 5

100 g of pulverized coal having a moisture content of 5.7% and an average particle size of 1.0 mm, 1 g of HPMC powder having an average particle size of 82 탆 and a viscosity of 60,000 cps were mixed first, and then 10 g of water was added and mixed again to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Experimental Example 6

100 g of pulverized coal having a moisture content of 6.0% and an average particle size of 1.0 mm and 1 g of HPMC powder having an average particle size of 75 탆 and a viscosity of 12,200 cps were mixed first and then 10 g of water was added and mixed again to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Experimental Example 7

100 g of pulverized coal having a moisture content of 6.1% and an average particle size of 1.0 mm, 1 g of HPMC powder having an average particle size of 77 탆 and a viscosity of 49,000 cps were mixed first, and then 10 g of water was added and mixed again to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Comparative Example 1

100 g of pulverized coal having a moisture content of 7.6% and an average particle size of 1.1 mm and 0.6 g of HPMC powder having an average particle size of 78 탆 and a viscosity of 28,000 cps were first mixed and then added with 10 g of water to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Comparative Example 2

100 g of pulverized coal having a moisture content of 5.7% and an average particle size of 1.0 mm and 0.2 g of HPMC powder having an average particle size of 82 탆 and a viscosity of 60,000 cps were first mixed and then added with 10 g of water to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Comparative Example 3

100 g of pulverized coal having a moisture content of 1.4% and an average particle size of 1.1 mm and 1 g of HPMC powder having an average particle size of 75 탆 and a viscosity of 2,080 cps were first mixed and then added with 10 g of water to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Comparative Example 4

100 g of pulverized coal having a moisture content of 0.1% and an average particle size of 1.0 mm and 1 g of carboxymethyl cellulose (CMC) (ASHILAND Co., AQUALONTM) powder having an average particle size of 70 μm and a viscosity of 6,000 cps were first mixed and then 12 g of water was added And mixed again to prepare a mixture. And the mixture was charged between a pair of rolls to produce a blast furnace. The remaining experimental procedure was the same as Experimental Example 1 described above.

Experiment result

The falling strength and the compression load of the briquettes produced according to the above-described Experimental Examples 1 to 6 were measured. The falling strength of the briquettes was determined from the ratio of the briquette having a particle size of not less than + 20 mm after 2 kg of the briquettes were freely dropped 4 times at a height of 5M. In addition, the compression load of the briquettes was measured as the maximum load when compressed at a speed of 50 mm / min, and the average value of the samples of the 20 shaped samples was measured. The results are shown in Table 1 below.

As shown in Table 1, when the HPMC having a viscosity of 12,200 cps to 60,000 cps was used in the range of 0.8 part by weight to 1.0 part by weight in Experimental Examples 1 to 7, the falling strength and the compressive load of the molded carbon were excellent. Therefore, it was found that it is preferable to adjust the viscosity of HPMC to the above-mentioned range. In contrast, it was confirmed that the drop strength and the compression load of the briquette produced according to Comparative Examples 1 to 4 were much smaller than the drop strength and the compression load of the briquettes produced according to Experimental Examples 1 to 7. Therefore, it was confirmed that the molded cans made using HPMC were much better in terms of falling strength and compressive load than those made using CMC.

Ash production test

Experimental Example 8

The briquettes prepared in Experimental Example 1 were pulverized into fine powders, and about 7 g of undifferentiated shaped briquettes were placed in a 30-ml magnetic crucible and heated at 850 ° C in a box furnace for 10 hours for combustion. The remaining experimental procedures can be easily understood by those skilled in the art, and detailed description thereof will be omitted.

Experimental Example 9

HPMC and CMC solution were uniformly mixed with pulverized coal to prepare a mixture. 100 g of pulverized coal having a moisture content of 0.1% and an average particle size of 1.0 mm, 7.5 g of a 4% aqueous solution of hydroxypropylmethylcellulose (HPMC, Samsung Fine Chemicals, Methylcellulose, viscosity 28,000 cps) and 7.5 g of carboxymethylcellulose CMC, ASHILAND, AQUALON (TM), viscosity 6,000 cps) 6% aqueous solution was used. Then, the mixture was charged into a pair of rolls to produce a blast furnace. In this case, the pair of rolls pressurized the mixture at a pressure of 20 kN / cm to produce pillow shaped pellets of 64.5 mm ㅧ 25.4 mm ㅧ 19.1 mm size. The briquettes thus produced were pulverized into fine powders, and about 7 g of undifferentiated shaped coal was put into a 30-ml magnetic crucible and heated at 850 ° C in a box furnace for 10 hours to be burned. The remaining experimental procedures were the same as those of Experimental Example 8 described above.

Comparative Example 5

The briquettes produced in Comparative Example 4 were pulverized into fine powders, and about 7 g of undifferentiated shaped coal was placed in a 30-ml magnetic crucible and heated at 850 ° C in a box furnace for 10 hours to be burned. The remaining experimental procedures were the same as those of Experimental Example 8 described above.

Experiment result

The remaining ash components were analyzed according to Experimental Example 8, Experimental Example 9 and Comparative Example 5. The experimental results of Experimental Example 8, Experimental Example 9 and Comparative Example 5 described above are shown in Table 2 below. Table 2 shows the ash components contained in the briquettes prepared according to Experimental Examples 8, 9 and 5.

As shown in Table 2, in Experimental Example 8, the Na ₂ O content in the alkaline contained in the ash was low at 0.39, while in Comparative Example 5, the Na ₂ O content was as high as 2.64. In Experimental Example 9, the content of Na2O was 1.59, which was somewhat higher. This suggests that when sodium carbonate is bonded to the functional group of CMC, when alkali metal is included in the reducing gas, the operation of the fluidized-bed reduction reactor may be adversely affected when the CMC solution is used to produce the shaped coal.

It will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the following claims.

10. Melting and gasification furnace
20. Packed bed type reduction furnace
22. Fluidized Bed Type Reduction Furnace
30. Tungus
40. Reduction iron compression unit
50. Compressed reduced iron storage tank
101. Dome
200. Welding equipment

Claims (18)

A melter-gasifier furnished with reduced iron, and
A reducing furnace connected to the melter-gasifier and providing the reduced iron;
Wherein the molten iron is charged into a dome of the melting and gasifying furnace and rapidly heated,
Providing pulverized coal,
Mixing the pulverized coal with a pulverulent cellulose ether compound to provide a mixture,
Adding and mixing water to the mixture, and
Molding the mixture to provide a blast furnace
Lt; / RTI >
In the step of providing the mixture, the average particle size of the cellulose ether compound is 50 탆 to 100 탆,
The cellulose ether compound is at least one selected from the group consisting of methyl cellulose (MC), hydroxyethyl cellulose (HEC), hydroxypropyl cellulose (HPC), hydroxypropyl methyl cellulose (HPMC) and hydroxyethyl methyl cellulose It contains one kind of compound, does not contain carboxymethyl cellulose (CMC)
Wherein the amount of the cellulose ether compound contained in the briquette is 0.7 wt% to 2.0 wt% in the step of providing the briquette. The method of claim 1,
And the amount of the cellulose ether compound is from 0.8 wt% to 1.5 wt%. The method of claim 1,
Wherein the amount of moisture contained in the briquette is 5 wt% to 15 wt% in the step of providing the briquette. 4. The method of claim 3,
And the amount of moisture contained in the molded boll is 7 wt% to 12 wt%. The method of claim 1,
Wherein the ratio of the amount of water contained in the molded bell to the amount of the cellulose ether compound contained in the molded bell is in the range of 5 to 40. The method of claim 1,
Wherein the ratio of the amount of water contained in the molded bell to the amount of the cellulose ether compound contained in the briquette is 7 to 20. delete The method of claim 1,
Wherein the ratio of the average particle size of the pulverized coal to the average particle size of the cellulose ether compound is 7 to 30 in the step of providing the mixture. The method of claim 1,
Wherein the ratio of the average particle size of the pulverized coal to the average particle size of the cellulose ether compound is 10 to 20. The method of claim 1,
Wherein the mixing time in the step of providing the mixture is less than the mixing time in the step of adding and mixing water to the mixture and providing the mixture for the mixing time in the step of adding and mixing water to the mixture Wherein the ratio of the mixing time in the step (a) to the mixing time in the step (b) is 2 to 5. delete delete The method of claim 1,
Wherein the viscosity of the cellulose ether compound is 4,000 cps to 80,000 cps. The method of claim 1,
Further comprising the step of adding water to the mixture and then mixing and drying the mixture. Providing a briquette made according to claim 1,
Providing reduced iron reduced in a reduction furnace; and
Charging the reduced-shaped coal and the reduced iron into a melter-gasifier to provide molten iron
≪ / RTI > 16. The method of claim 15,
Wherein the reducing furnace is a fluidized bed type reducing furnace or a packed bed type reducing furnace in the step of providing the reduced iron. delete delete

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