JP4212493B2 - State analysis method in dry zinc smelting furnace and zinc smelting method - Google Patents

Description

The present invention uses coke to remove zinc from a fired product containing at least zinc oxide, lead oxide, iron oxide and silicon oxide, and in a blast furnace for dry zinc smelting, at least oxidation of each component of sintered ore. The present invention relates to a method for analyzing a reaction state in a region where a reduction reaction of zinc, lead oxide and iron oxide is performed as a main reaction.
The present invention also relates to a zinc smelting method for extracting zinc from a fired product containing at least zinc oxide, lead oxide, iron oxide and silicon oxide using coke.

Modeling and analyzing operating conditions in a smelting process, such as a blast furnace, where it is difficult to accurately measure and grasp the in-furnace conditions is an effective means for improving operations and optimizing processes. . (For example, Patent Document 1)
JP 2003-277845 A

  However, in the ISP (imperial smelting process) method of dry zinc smelting, the reaction system is more complex than steel smelting and copper smelting, so the systematic analysis in the furnace is not progressing. Currently.

  In addition, it is difficult to dispose a thermometer or the like in order to grasp the inside of the furnace because it is eroded by the furnace interior material and the furnace gas. Therefore, during actual operation, in order to stabilize the in-furnace situation and increase the efficiency of operation, it was necessary to respond on the spot based on experience. In order to stabilize the in-furnace situation and increase the efficiency of the operation, and further to automate the operation, it is possible to reproduce the actual operation, and the change in the in-furnace situation accompanying changes in the operating conditions. Development of a state analysis in the furnace that can be followed is desired.

  Therefore, the present invention has been made in view of the above-described circumstances, and can reproduce the actual operation, and can follow the change in the in-furnace situation accompanying the change in the operation condition, by the dry zinc smelting ISP method. It aims at providing the state analysis method which analyzes the inside of a blast furnace, and the new zinc smelting method which operates by applying this analysis method.

The state analysis method in the dry zinc smelting blast furnace according to the present invention is a blast furnace for dry zinc smelting that uses coke to extract zinc from a fired product containing at least zinc oxide, lead oxide, iron oxide and silicon oxide. there are a first region for discharging the zinc produced with dropping the least part of the total introduction amount of the introduced coke, the reducing reaction of at least zinc oxide of each component of the calcined product which has passed through the first region In the second region where the main reaction is carried out, the remainder of the calcined product and coke is introduced, and at least the reduction reaction of zinc oxide, lead oxide and iron oxide and the oxidation reaction of carbon among the calcined product that has passed through the second region A method of analyzing a reaction state in a blast furnace formed continuously with a third region performed as a main reaction using a computer system,
Input the value for specifying the shape of the furnace as the reaction field specific value, input the introduction temperature, the introduction amount and the composition of the coke and the fired product introduced into the first and third regions as the introduction initial value, The composition and flow rate of the gas introduced into the first region, the composition and flow rate of the gas containing purified zinc discharged from the first region, and the temperature, composition and flow rate of the gas introduced into the third region are operated. Operation condition input stage to input as data,
The composition and flow rate of the gas introduced into the first region, the composition and flow rate of the gas introduced into the third region, and the composition of the fired product and coke introduced into the first region, which are input in the operation condition input stage. DOO using, based on the carbon monoxide producing reaction and carbon dioxide production reaction carried out in each region, a front Symbol rate calculation step of calculating a flow rate of carbon monoxide and carbon dioxide produced in the first region,
A temperature setting step for setting and inputting the temperature of the gas discharged from the first region;
The composition and flow rate of the gas introduced into the first region and the composition and flow rate of the gas containing purified zinc discharged from the first region, which are input in the operation condition input step, and obtained in the flow rate calculation step. The mass balance of the reaction in the first region based on the chemical reaction performed in the first region using the flow rate of carbon monoxide and carbon dioxide and the gas temperature set and input in the temperature setting step. And a first region balance calculation stage for calculating a material balance, a heat balance and a composition of a gas containing zinc introduced from the second region,
Mass balance, heat balance and composition of the gas containing zinc discharged from the second region calculated in the first region balance calculation step, the reaction field specific value and the introduction input in the operation condition input step Using the initial value, based on the rate constant and equilibrium constant of each reduction reaction, the flow rate and temperature change of the whole gas component, coke, and calcined product in the vertical section of the second region, The pressure change of each gas composition in the minute section and the change in the reaction rate of each solid composition in the minute section are calculated, and the coke and sintering in the second region are calculated based on the obtained values. A second region balance calculation stage for calculating the mass balance of each of the mineral and gas components, the heat balance and the heat loss of the entire second region;
The temperature, composition and amount of the calcined product and coke introduced into the third region and the temperature, composition and flow rate of the gas introduced into the region, and the second region balance calculation, which are input in the operation condition input step. A third region balance calculation stage for calculating the material balance, heat balance and heat loss in the third region based on the chemical reaction carried out in the third region using the material balance and heat balance obtained in the step; It is characterized by having.
In this method, it is preferable that the first region is configured to drop at least a part of the total introduced amount of coke introduced and the fired product while discharging the generated zinc.
In this method, the second region is such that at least a reduction reaction of zinc oxide and a reduction reaction of lead oxide and iron oxide among the components of the fired product that has passed through the first region are performed as main reactions. It is preferable.

  In this method, it is preferable that the fired product introduced into the third region is 1 to 100% of the whole.

  Further, the coke introduced into the third region is preferably 40 to 60% of the whole.

  The gas introduced into the third region preferably contains 30 to 100% oxygen.

  Moreover, it is preferable to set the reaction represented by the following reaction formula as the reaction performed in the second region:

  In the second region balance calculation stage, the entire gas component, changes in the flow rate and temperature of coke and sinter, and the pressure change of each gas composition in the minute section, and each solid in the minute section As the change in the reaction rate of the composition, it is preferable to use a differential equation represented by a minute change of each change per minute section in consideration of the gas generated in the blast furnace.

  Moreover, it is preferable that the reaction field specific value used in the second region balance calculation stage is a furnace cross-sectional area in each minute section in the height and height directions of the furnace.

  Further, it is preferable to set a chemical reaction represented by the following reaction formula as a chemical reaction performed in the first region:

  In addition, it is preferable to set the chemical reaction represented by the following reaction formula and the reaction of generating slug containing unreacted oxide as the chemical reaction performed in the third region:

Further, the zinc smelting method according to the present invention is a zinc smelting method for taking out zinc from a fired product containing at least zinc oxide, lead oxide, iron oxide and silicon oxide using coke,
With coke is introduced, a first region for discharging the generated zinc, and a second region for delivering the generated zinc to the first region, as the reducing reaction of at least zinc oxide main reaction of the calcined product Using a blast furnace in which a third region in which zinc is produced is continuously formed, and
Introducing at least part of the total introduction amount of the coke in the first region,
It is characterized by introducing the fired product and the remaining coke into the third region.
In this method, it is preferable that the first region is one in which coke and a fired product are introduced and the generated zinc is discharged.
In this method, when at least a part of the total amount of coke introduced is introduced into the first region, it is preferable to introduce at least a part of the total amount of coke introduced and the fired product into the first region.

  In this method, it is preferable that the fired product introduced into the third region is 1 to 100% of the whole.

  Further, the coke introduced into the third region is preferably 40 to 60% of the whole.

  Moreover, it is preferable that a gas containing 30 to 100% oxygen is introduced into the third region.

  ADVANTAGE OF THE INVENTION According to this invention, it becomes possible to analyze the inside of the blast furnace by the ISP method of dry-type zinc smelting which can follow the change of the in-furnace condition accompanying the change of operation conditions which can reproduce actual operation. Therefore, it becomes possible to optimize the operating conditions to improve the operation results of the blast furnace, and to enable effective zinc smelting

  Hereinafter, a state analysis method in a dry zinc smelting blast furnace according to the present invention and an embodiment of a zinc smelting method that operates by applying this analysis method will be described in detail with reference to the drawings. As shown in FIG. 1, a dry zinc smelting blast furnace (hereinafter referred to as a “blast furnace”) 10 is divided into three parts, that is, a furnace top part 11 as a first area, a shaft part 12 as a second area, and a third area. It is divided into the hearth part 13.

  The furnace top portion 11 is heated by a gas introduced into the first region from the second region, at least a part of the total amount of coke introduced, and, if necessary, a fired product containing zinc as a raw material, and dropped onto the shaft portion 12. And is the first area of the blast furnace that discharges the generated zinc. In the furnace top portion 11, an air inlet 41 for introducing a preheated mixed gas of oxygen and nitrogen, a fired material containing zinc as a raw material, and a raw material inlet 42 for introducing coke and generated zinc are used. A zinc-containing gas outlet 43 for taking out the zinc-containing gas is provided, and heat is generated when the carbon monoxide gas contained in the zinc-containing gas causes an oxidation reaction by the mixed gas introduced from the air inlet 41. Then, the gas, coke and fired product introduced into the first region are heated as described above.

  That is, the following reaction proceeds.

  A calcined product containing zinc is obtained by roasting normal zinc concentrate containing at least zinc, lead, iron, silicon oxide and sulfur, and containing at least zinc oxide, lead oxide, iron oxide and silicon oxide. It is a thing. The zinc concentrate contains, for example, 52% zinc, 2% lead, 7% iron, 2% silicon oxide, 30% sulfur, 7% other components such as metals and oxygen. The coke contains at least carbon, aluminum oxide, and silicon oxide. The zinc-containing gas contains gaseous zinc as will be described later, and this gaseous zinc can be isolated and recovered by absorbing it in a lead bath (not shown).

  Moreover, zinc containing gas is discharged | emitted from the shaft part 12 mentioned later to the furnace top part 11. FIG. As described above, the preheated mixed gas from the air inlet 41 is introduced into the furnace top 11 by maintaining the gas in the furnace top 11 at 1000 ° C. or higher so that the zinc in the zinc-containing gas contains the zinc. This is to prevent zinc oxide from being generated by reacting with carbon dioxide contained in the gas.

  The shaft portion 12 performs at least a reduction reaction of zinc oxide, lead oxide and iron oxide among the components of the fired product introduced from the furnace top portion 11 as a main reaction, and the zinc-containing gas generated in the third region is the first. This is the second area of the blast furnace that is sent to the area. The shaft portion is filled with coke and, in some cases, a fired product. The upper limit is defined as a stock line 31, which is a predetermined distance below the stock line 31 and above a tuyere 21 and 22 described later. Up to the boundary line 32 of the height.

  Further, in the shaft portion 12, specifically, coke solution loss reaction (4), and when the fired product is introduced into the furnace top portion 11, volatile reduction of zinc oxide with carbon monoxide gas (2), zinc Steam reoxidation (3), iron oxide reduction (6), (7), lead oxide reduction (5), that is, the following reaction proceeds.

  In the shaft portion 12, the sintered ore continuously drops and moves toward the hearth portion 13 while proceeding with the reaction.

  The hearth part 13 is composed of a reduction reaction of zinc oxide, lead oxide and iron oxide contained in the introduced fired product, and an oxidation reaction of carbon, and in some cases, an oxidation contained in the fired product passed through the shaft part 12. This is the third region in which the reduction reaction of zinc is performed as the main reaction. In the hearth 13, tuyere 21 and 22 for introducing hot air, an inlet 23 for introducing calcined product and coke, a lead outlet 51 for extracting molten lead, and unreacted iron oxide A slug outlet 52 for taking out a molten slug containing at least lead oxide and silicon oxide is provided.

  In the hearth part 13, specifically, the combustion reactions (8) and (10) of the coke from the shaft part 12 and the inlet 23 caused by the hot air from the tuyere 21 and 22 as shown below, the inlet 23 In some cases, the volatile reduction (8) and (9) of zinc oxide contained in the fired product from the shaft portion 12 and the reduction reaction (5) of lead oxide contained in the fired product from the inlet 23 and the iron oxide Reduction reactions (6) and (7) proceed.

  As described above, in the blast furnace 10 shown in FIG. 1, the coke introduced from the raw material introduction port 42 and, if necessary, the fired product are heated by the preheated mixed gas introduced from the air introduction port 41. And is dropped on the shaft portion 12.

  In the shaft portion 12, when a fired product is introduced from the furnace top 11, a reduction reaction of a part of zinc oxide, lead oxide, and iron oxide contained in the fired product proceeds, and gaseous zinc, carbon monoxide, and carbon dioxide are promoted. A zinc-containing gas containing at least carbon is generated and sent to the furnace top 11. On the other hand, the calcined product and coke containing unreacted zinc oxide, lead oxide and iron oxide are sent to the hearth 13.

  In addition, the zinc containing gas sent to the furnace top part 11 is taken out from the zinc containing gas outlet 43, and zinc simple substance is isolated and collected from the taken out zinc containing gas. In the hearth part 13, the calcined product and coke introduced from the introduction port 23 and the coke and optionally the calcined product sent from the shaft part 12 are combusted by hot air introduced from the tuyere 21 and 22, and coke. While more carbon monoxide and carbon dioxide are produced, zinc oxide in the fired product and in the slug from the shaft portion 12 reacts with carbon contained in the coke or generated carbon monoxide, and is volatilely reduced. A zinc-containing gas containing at least zinc gas, carbon monoxide and carbon dioxide is generated and sent to the top 11 of the furnace through the shaft portion 12.

  Here, when introducing the fired material and coke from the hearth part 13, as shown in FIG. 2, a plurality of inlets 23 are provided around the hearth part of the blast furnace 10, and the fired material is provided for each inlet. It is preferable to change the ratio of introduction of coke and coke.

  By doing in this way, it is known that the following oxidation-reduction reaction can be inclined to the zinc production | generation side, and the yield of zinc can be raised.

  Generally, when the concentration of zinc-containing slag is higher than 4%, this oxidation-reduction reaction is inclined toward the zinc production side. Moreover, in the hearth part in the blast furnace 10, a certain distribution can be obtained in the abundance (concentration) of zinc-containing slag (Zn in slag), that is, a region 24 having a high zinc-containing slag concentration is formed in the center of the blast furnace 10. Regions 25 and 26 with low zinc-containing slag concentration are generated at the ends. Therefore, by making the concentration of the zinc-containing slag constant, it becomes possible to perform control so that this oxidation-reduction reaction can always be performed in an optimum environment.

  Therefore, the coke concentration is low and the coke concentration is high in the region 24 with a high zinc-containing slag concentration, while the coke concentration is introduced into the introduction port 23 of the regions 25 and 26 with a low zinc-containing slag concentration at a ratio that the fired product concentration is high. It is preferable to introduce at a ratio that lowers the fired product concentration.

  Moreover, in the hearth part 13, the molten state slug containing at least the molten lead generated in the shaft part 12 and the hearth part 13 and unreacted zinc oxide, lead oxide, iron oxide and silicon oxide is respectively lead. It is taken out from the outlet 51 and the slug outlet 52 and collected. In the blast furnace for dry zinc smelting in which the raw material as in the present embodiment is introduced into the hearth part 13, the reduction reaction of the metal oxide contained in the fired product proceeds particularly in the hearth part 13, and this reduction reaction. Since the zinc produced | generated by gas is obtained with gas, it raises the inside of the blast furnace 10. FIG.

  In particular, in the shaft portion 12, a solution loss reaction in which coke is oxidized occurs. This reaction is an endothermic reaction, which lowers the temperature in the shaft portion 12 and lowers the temperature of the zinc-containing gas, which is preferable from the viewpoint of condensing the gaseous zinc discharged from the furnace top portion 11 into a product. Absent. In the solution loss reaction, coke involved in this reaction is discharged as carbon monoxide (CO) into the gas in the shaft portion 12 without contributing to the reduction reaction of zinc oxide, and wastes expensive coke. It is also not preferable from the point of consumption.

  Therefore, in order to reduce the solution loss reaction, the amount of coke staying in the coke shaft portion 12 is reduced. Therefore, at least a part of the total amount of coke introduced is introduced from the furnace top portion 11 and the rest is introduced from the hearth portion 13, and the fired product is introduced from the hearth portion 13 accordingly.

  From such a viewpoint, the fired product introduced in the hearth part 13 which is the third region is 1 to 100%, preferably 40 to 100% of the total introduction amount, and the rest is the first region. It is made to introduce from the raw material introduction port 42 of the top part 11. On the other hand, the coke introduced at the furnace top 11 is 40 to 60%, preferably 50% of the total introduction amount, and the remainder is introduced from the hearth part 13. The coke and fired product introduced from the furnace top 11 are preferably lumps, but the fired product and coke introduced from the furnace floor 13 are preferably powder. Moreover, it is preferable that the amount of oxygen contained in the hot air introduced from the tuyere 21 and 22 of the hearth part 13 is 30 to 100%.

  By introducing each substance or gas from the furnace top part 11 or the hearth part 13 at such a ratio, zinc can be efficiently generated in the hearth part 13, and in the shaft part 12. The solution loss reaction is suppressed, and the zinc-containing gas generated in the hearth part 13 can be efficiently sent to the furnace top part 11 while maintaining the zinc content.

  Also, in the conventional method of analyzing the state in the blast furnace used for steel smelting, copper smelting, lead smelting, etc., iron and lead produced by the reduction reaction do not rise in the blast furnace. The situation is different from zinc obtained as gas in the blast furnace. Therefore, it is impossible to use the analysis method used for steel smelting as it is for zinc smelting. Also, in dry zinc smelting, the blast furnace was conventionally divided into two areas, but it cannot be said that the obtained analysis results faithfully reproduced the state in the blast furnace. It was insufficient.

  Therefore, in the embodiment of the state analysis method in the dry zinc smelting blast furnace, as shown in FIG. 1, the blast furnace 10 is divided into three regions, that is, the furnace top 11 as the first region, and the shaft portion as the second region. 12 and the hearth part 13 as the third region, the material balance and the heat balance in each region in order from the first region to the third region, and if necessary, the composition of the gas component (hereinafter referred to as “gas composition”) ) And a solid component reaction rate (hereinafter referred to as “solid reaction rate”) indicating a solid composition is calculated using a computer system.

  Specifically, in this state analysis method, as shown in FIG. 3, a value for specifying the shape of the furnace is input as a reaction field specifying value, and coke and firing introduced into the first and third regions. The introduction temperature, the introduction amount and the composition of each product (and the surface area of the powder for coke and fired product introduced from the third region) are input as the initial introduction value, and the composition of the gas introduced into the first region Operation data of the flow rate, the composition and flow rate of the gas containing purified zinc discharged from the first region, and the temperature, composition and flow rate of the gas introduced into the third region, and the amount of slag zinc and lead discharged The operating condition input stage (step S10) to be input as, the composition and flow rate of the gas introduced into the first area input in the operating condition input stage, and the third area Based on the carbon monoxide production reaction and the carbon dioxide production reaction performed in each region using the composition and flow rate of the introduced gas and the composition of the fired product and coke introduced, in the first region In the flow rate calculation step (step S20) for calculating the flow rates of the generated carbon monoxide and carbon dioxide, the temperature setting step (step S30) for setting and inputting the temperature of the gas existing in the first region, and the operation condition input step. The composition and flow rate of the gas introduced into the first region and the composition and flow rate of the gas containing purified zinc discharged from the first region, the carbon monoxide obtained in the flow rate calculation step, and Based on the chemical reaction performed in the first region, using the flow rate of carbon dioxide and the gas temperature set and input in the temperature setting step, the reaction in the first region is performed. A first region balance calculation step (steps S40 and S50) for calculating a material balance, a heat balance and a composition of a gas containing zinc introduced from the second region by calculating a material balance and a heat balance. The mass balance, heat balance and composition of the gas containing zinc discharged from the second region calculated in the one region balance calculation step, the reaction field specific value and the initial introduction value input in the operation condition input step And based on the rate constant and the equilibrium constant of each reduction reaction, the change in the flow rate and temperature of the entire gas component, coke, and calcined product in the fine vertical section of the second region, The change in the pressure of each gas composition in the minute section and the change in the reaction rate of each solid composition in the minute section are calculated, and based on the obtained values, the coke and sintered ore in the second region are calculated. And the second region balance calculation stage (steps S70 and S80) for calculating the mass balance of each of the gas components, the heat balance and the heat loss of the entire second region, and the third region input in the operating condition input step Using the temperature, composition and amount of the introduced calcined product and coke, and the temperature, composition and flow rate of the gas introduced into the region, and the material balance and heat balance obtained in the second region balance calculation stage And a third region balance calculation step (step S90) for calculating a material balance, a heat balance and a heat loss in the third region based on a chemical reaction performed in the third region.

  In step S10, the operation conditions, that is, the reaction field specific value, the introduction initial value, and the operation data are input using an appropriate input device such as a keyboard, and the process proceeds to step S20. Here, the reaction field specific value is a parameter for specifying the shape of the furnace, for example, the height of the blast furnace and the cross-sectional area of the furnace in each minute section in the height direction. The cross sectional area of the furnace in the minute section in the height direction refers to the area A from the position Z in the horizontal direction to the position (Z + dZ) as shown in FIG. Although the blast furnace does not have a uniform cross section from the upper end to the lower end, considering the minute section, the upper surface and the lower surface have substantially the same shape in this section, so the volume in this section is (A XdZ).

  The initial value of the introduction is the coke introduced into the furnace top 11 and, if necessary, the amount of the fired product introduced, the introduction temperature and composition, the preheated mixed gas introduced into the furnace top 11 from the air inlet 41. The composition and the introduction flow rate (and optionally the temperature), the temperature of the hot air gas introduced into the hearth 13 from the tuyere 21 and 22, the composition and the introduction flow rate, and the surface area (preferably the average value) of each powder, And the amount of calcined product and coke introduced from the inlet 23 of the hearth 13 and the introduction temperature and composition.

  The operation data includes, for example, the composition of the purified zinc-containing gas discharged from the furnace top 11 and the discharge flow rate (and optionally the temperature), the amount of zinc and lead in the slag discharged from the hearth 13, and lead Discharge flow rate and temperature.

In step S20, the gas composition discharged from the furnace top 11 is calculated. Specifically, the furnace top, shaft, and hearth are regarded as one reaction system, and the material balance calculation of the reaction system is performed using the operation data input in step S10, and exists as a gas composition. The ratios of constituent elements, ie, carbon (C), oxygen (O), nitrogen (N), and zinc (Zn), are determined, and carbon monoxide (CO) and carbon dioxide (CO ₂ ) Calculate the percentage. Thereby, the composition and flow rate of the gas discharged from the furnace top 11 are calculated.

  In step S30, the gas temperature in the furnace top 11 is input, and the process proceeds to step S40. The gas temperature is arbitrarily selected based on experience. In step S40, the material balance and heat balance at the top 11 are calculated based on the operating conditions input in step S10, the furnace top gas composition calculated in step S20, and the gas temperature input in step S30. The process proceeds to step S50.

  The chemical change performed in the furnace top 11 is a reaction represented by the following formula, and the reaction heat generated by this reaction is 34.1 GJ / hr (the reaction amount of the following formula is calculated by mass balance calculation at the top of the furnace). (The reaction heat was obtained from the reaction amount.) (Junichiro Yagi: Journal of the Japan Mining Association, 93 (1977), pp 889-894).

  Step S50 contains zinc introduced from the shaft portion 12 based on the mass balance and heat balance of the furnace top 11 and the fact that oxygen in the preheated gas mixture is consumed for reaction with 100% carbon monoxide. The material balance, heat balance and composition of the gas to be calculated are calculated (estimated), and the process proceeds to step S60. In step S60, the reaction rate equation, rate constant and equilibrium constant of each reduction reaction performed in the shaft portion are input using the input device, and the process proceeds to step S70. The free energy change of each reduction reaction can be calculated based on values described in literature (for example, D.R.Stull and H.Prophet: JANAF Thermodynamical Tables (1971)).

  Note that the rate constant and the equilibrium constant used here may be arbitrary values such as literature values or measured values. In step S70, a change (vertical distribution) of each parameter in the shaft portion 12 is calculated, and the process proceeds to step S80. Specifically, as shown below, changes in the flow rate and temperature of the entire gas component, coke and fired product, and pressure changes of each gas composition in the minute section, and solids in the minute section As a change in the reaction rate of the composition, a differential equation indicated by a minute change of each change per minute section in consideration of a gas generated in the blast furnace is solved.

The following assumptions are used for other conditions.
(1) Be in a steady state;
(2) The amount of gas and solid in the furnace is a piston flow, that is, the flow in the horizontal direction is constant, and the flow is constant and uniform, and each process variable represented by the following formula is uniformly distributed in the horizontal direction. To do;
(3) The fired product is mixed and introduced;
(4) The fired product is made of ZnO, PbO, Fe ₂ O ₃ , SiO ₂ , and the coke is made of C, Al ₂ O ₃ , SiO ₂ ;
(5) hematite Fe ₂ O ₃ is reduced to wustite FeO via magnetite Fe ₃ O ₄ ;
(6) The molten lead produced in the reduction process should remain inside the fired product;
(7) The reaction heat of the solution loss reaction (C + CO ₂ → 2CO) is given to the coke, and when the fired product is present in the shaft portion 12, the other reaction heat is given to the fired product;
(8) Ignore heat transfer between the calcined product and coke;
(9) The calcined product and coke particle diameter should be constant;
(10) Each porosity in the fired product, coke, and furnace should be constant;
(11) The fired product introduced from the furnace top portion 11 should not be melted at the shaft portion 12.

For example, in the minute section represented by the area Az (m ³ ) and the height dZ (m) as shown in FIG. 4, the gas flow rate (Nm ³ / hr) introduced from below into the minute section is expressed as (F _Gas + dF _Gas ), and the gas flow rate (Nm ³ / hr) discharged upward is F _Gas , the gas (gas) flow rate in this section is dF / dz = -22.4 · (R ₂ + R _3- R ₄ ) · A

In the formula, gas is indicated as “g”, calcined product as “s”, and coke as “c”. F _g represents the volume flow rate of gas (Nm ³ / hr), F _s and F _c represent mass flow rates of fired product and coke (kg / hr), respectively, and T _n represents the temperature of gas or solid (K). X _i represents the mole fraction of component i, and f _i represents the reaction rate of component i. N ⁰ _i indicates the molar flow rate (kmol / hr) of the component i in the charge, ε indicates the porosity in the furnace (−), μ _g indicates the gas viscosity (kg / m hr), G _g represents a gas mass velocity (kJ / m ³ hr), d _ave represents an average particle diameter (m), and g _c represents a gravity conversion coefficient (kg m / kg hr ² ).

Further, ρ _g represents a gas density (kg / Nm ³ ). Q ₁ indicates the heat dissipated in the furnace wall, that is, the heat dissipated by the difference between the gas temperature and the outside temperature (kJ / m hr), and Q ₂ indicates the amount of heat transfer between the gas (Gas) and the calcined product (calcine). kJ / m ³ hr), Q ₃ represents the heat transfer amount between gas and coke (kJ / m ³ hr), and Q ₄ represents the reaction heat (kJ / m ³ hr) applied to the fired product. Q ₅ shows the heat of reaction (kJ / m ³ hr) given to the coke, Q ₆ shows the amount of heat when the components of the calcined product move to the product gas, and Q ₇ moves the component of the coke to the product gas Indicates the amount of heat when Moreover, the balance relationship between the amount of heat Q ₁ to Q _7, shown in FIG.

In the above formula, M _i represents the molecular weight of the i component (kg / kmol), U represents the overall heat transfer coefficient (kJ / m ² hr K) of the furnace wall, and Lz represents the furnace circumference (m) at position z. H _gj represents the heat transfer coefficient (kJ / m ² hr K) from the gas component to the j component, ε _j represents the porosity of the j component, χ _j represents the volume fraction of the j component, φ _j is the j component, shows a solid shape factor as the coefficient for correcting the deviation from spherical particles, d _s indicates the particle diameter of the sintered ore (m), d _c is the particle size of the coke (m) Indicates. H _Rn represents the n-type reaction heat (kJ / kg), and C _i represents the specific heat of the i component (kJ / kg K).

The overall heat transfer coefficient U of the furnace wall is expressed as U = 1 / Σ (x using the furnace wall thickness x _i ^w (m) and the furnace wall thermal conductivity k _i ^w (kJ / m hr K). _i ^w / k _i ^w ). Here, each reaction rate is defined as a ratio between the number of moles reduced by reaction of each component and the initial number of moles, and the heat transfer coefficient between gas and particles is expressed by, for example, the Ranz equation (WERanz: Chem. Eng. Prog., 48 (1952), pp.247-253), and the thermal conductivity of the gas is, for example, the Eucken equation (A. Eucken: Physik. Z., 14 (1952), pp.324- 332). The gas viscosity of a single component is calculated by, for example, the Licht-Stechert equation (W. Licht, Jr. and DGStechert: J. Phys. Chem., 48 (1944), pp. 23-47). Can be determined by the Wilke equation (CRWilke: J. Chem. Phys., 18 (1950), pp. 517-519).

In the above equation, the gas / solid flow rate is based on the mass balance, the gas / solid temperature is based on the heat balance, the gas composition is based on the mass balance of the gas component, and the gas pressure is Ergun's pressure loss equation (S.Ergun: Chem. Eng. Prog., 48 (1952), pp. 89-94), the solid reaction rate can be derived from the reaction amount of each component. R _{2 to} R ₇ represent reaction rates (kmol / m ³ (bed) hr) of reaction formulas (2) to (7) of the reactions in the shaft, respectively.

R ₂ is the overall reaction of reaction formula (2) from the fact that the reduction reaction of zinc oxide in sintered ore proceeds topochemically (Zenjiro Asagi et al .: Resources and Materials '94 (Spring Meeting) pp.322-323). In the velocity equation, an unreacted nuclear model of one interface as described later is applied, and the three processes of mass transfer in the gas film, that is, movement of CO in the gas film, diffusion in the particle, and chemical reaction proceed sequentially. Derived as an irreversible primary reaction.

R ₃ is derived on the assumption that all reoxidation reactions of zinc vapor occur on the surface of the calcined product, and the difference between the zinc partial pressure and the zinc equilibrium partial pressure is the driving force for the reaction. R ₄ considers the mass transfer in the gas film through which gas components pass through the gas film, which is the gas layer from the particle surface to the bulk, that is, the movement of CO ₂ in the gas film and the chemical reaction process. Derived as an irreversible primary reaction.

R ₆ and R ₇ are derived based on the unreacted nucleus model of the two interfaces, taking into account three processes: mass transfer in the gas film, intragranular diffusion, and chemical reaction. Here, the unreacted nucleus model of the two interfaces is, as shown in FIG. 6 b, three layers 61 to 63 are generated in the nucleus 60 due to the difference in the progress of the reaction. This is a reaction nucleus model in which there are two nuclei containing (unreacted nuclei).

Iron oxide Fe ₂ O ₃ is finally reduced to FeO through a two-stage reaction (reaction formulas (6) and (7)). That is, according to FIG. 6 b, the nucleus 60 forms a nucleus composed of only a single layer before the reaction, and an attack of carbon monoxide from the outside of the nucleus first produces a layer of Fe ₃ O ₄ . Become the nucleus. The produced Fe ₃ O ₄ is further reduced at the same time. Furthermore, the outer layer of Fe ₃ O ₄ reacts with carbon monoxide to form an FeO layer on the outside, and three layers containing iron oxides with different reduction stages are formed.

  On the other hand, it is considered that the reaction of zinc oxide proceeds based on the unreacted nucleus model of one interface, and this unreacted nucleus model of one interface is the reaction progress in the nucleus 50 as shown in FIG. This is a reaction nucleus model in which only two layers 51 and 52 are generated due to the difference between them, and the nucleus 50 has only one nucleus containing an unreacted substance (unreacted nucleus). FIG. 6 a shows a model of the reduction reaction of zinc oxide. Zinc oxide is reduced by carbon monoxide, the generated zinc is released as a gas, and other oxides remain in the outer layer 51. The inner layer 52 contains unreacted zinc oxide.

  In addition, since the calculation performed here incorporates various factors relating to each reaction rate and heat / mass transfer, for example, the effect of the furnace size on the reaction can be examined from the calculation results. In step S80, on the boundary line 32 between the shaft portion 12 and the hearth portion 13 based on the gas / solid flow rate, gas / solid temperature, gas composition / pressure, and solid reaction rate in the entire shaft portion calculated in step S70. The material balance and the heat balance at and the heat loss of the entire shaft portion are calculated, and the process proceeds to step S90.

  In addition, a material balance and a heat balance on the boundary line 32 of a zinc-containing gas discharged from the hearth 13 described later are also obtained for the gas generated in the blast furnace considered in the calculation. In step S90, the temperature and flow rate of the gas (hot air) introduced from the tuyere 21 and 22 into the hearth part 13, the introduction amount of the fired product and coke introduced from the introduction port 23, the introduction temperature and composition, and Using the material balance and heat balance in the shaft portion 12 obtained in step S80, the material balance, heat balance and heat loss in the hearth portion 13 are calculated based on the chemical reaction performed in the hearth portion 13, and step Proceed to S100.

  Here, the hot air temperature and flow rate (and composition as necessary), the slug and lead discharge flow rate and temperature discharged from the hearth 13 are the values listed in the operation data input in step S10. . The material balance and heat balance in the shaft portion 12 are the material balance and heat balance of sintered ore and coke discharged from the shaft portion 12, and the zinc content estimated to be discharged from the hearth portion 13 to the shaft portion 12. Examples include a gas mass balance and a heat balance.

  These values are given as boundary conditions, and the mass balance and heat balance in the hearth portion 13 are calculated in consideration of the following reaction performed in the hearth portion 13. The reaction heat of each reaction can be calculated based on the values described in the literature (for example, D.R.Stull and H.Prophet: JANAF Thermodynamical Tables (1971)).

  In addition, the heat of formation of the molten slug is -5.94 GJ / hr (Gotrib, A.D .: calculated based on the values shown in the theory of blast furnace ironmaking, Japan Iron and Steel Institute, pp330). In step S100, the heat loss in the shaft portion 12 calculated in step S80 and the heat loss in the hearth portion 13 calculated in step S90 are summed to calculate the heat dissipated in the blast furnace 10, and the process proceeds to step S110.

In step S110, the heat loss of the hearth 13 calculated in step S90 is compared with the heat loss determined based on the actually measured value and the furnace material. Specifically, it is assumed that the lead and slug discharged from the hearth part 13 and the heat loss of the hearth part 13 are proportional to the gas temperature at the lower end of the shaft part 12 based on the state of actual operation. Actual operation data on the discharge amount and temperature of lead and slug is accumulated in association with the temperature of the gas in the furnace top 11, and for example, the heat balance in the hearth 13 when set to 1400 ° C in step S30. Next, the heat balance in the hearth 13 when the temperature is set to 1500 ° C. in the step is obtained. The heat loss corresponds to the amount of heat obtained by subtracting the amount of heat of lead and slug out of the heat discharged in the heat balance, so the heat balance for each temperature is obtained. Subsequently, it is determined whether or not the heat loss corresponds to the heat loss obtained on the basis of the actual operation, that is, whether or not the calculated heat loss is appropriate. In addition, although it is judgment whether it is appropriate, for example, when the difference between the calculated value and the value based on the actual measurement value is within 10 ⁻² , preferably within 10 ^−6, it is “valid”. Judge.

  Since this heat loss is a value obtained with respect to the furnace top gas temperature set in step S30, whether or not the furnace top gas temperature set in step S30 is appropriate is determined by performing the determination in step S110. Can be determined. If the determination result is NO, that is, if it is determined that the obtained heat loss is not appropriate, the process returns to step S30, a new furnace top gas temperature is set, and the balance calculation from the furnace top 11 is repeated (step S30). S40-S100). When the determination result is YES, that is, when it is determined that the obtained heat loss is appropriate, the process proceeds to step S120, the operation condition used for the analysis is adopted as the operation condition of the blast furnace, and the operation is terminated.

  In addition, although the flowchart shown in FIG. 3 showed about the method of discriminating the operation condition of a blast furnace, if only the state in the blast furnace of an actual operation is analyzed, step S120 in FIG. 3 will be an arbitrary step. Needless to say.

  According to the analysis method as described above, it becomes easy to perform modeling and operation analysis of a process in a dry zinc smelting furnace that has been difficult in the past, and to improve the operation result of the blast furnace. It is possible to optimize the operating conditions. That is, by estimating the amount of zinc obtained by appropriately changing and calculating the operation data, it is possible to know in advance under what conditions it is efficient to operate the entire blast furnace.

  In addition, simulations for state analysis are performed based on the kinetics of reactions occurring in the shaft, and in other areas based on equilibrium theory. In the furnace, especially in the shaft, following changes in operating conditions. It becomes easy to grasp the change of the situation. Needless to say, the present invention is not limited to the above-described matters, and can be changed without departing from the object, operation, and effect of the present invention.

  Hereinafter, although the state analysis method in the dry-type zinc smelting and smelting furnace according to the present invention will be specifically described with reference to examples, it goes without saying that the present invention is not limited to the following examples.

[Reference Example 1]
As shown in Table 1 below, the total amount of the calcined product and coke is introduced from the top 11 of the furnace, and the balance calculation is performed when the amount of zinc produced is 352 t / day, which is the current operating condition, and the results are shown.

  Operating conditions as shown in Table 1, that is, input data relating to the sintered ore to be introduced (raw material Sinter) and coke, input data relating to the preheated mixed gas (Top Air) to be introduced into the top 11 of the furnace, zinc-containing gas ( Input data regarding exhaust gas) and input data regarding hot air (Blast Air) introduced into the hearth part 13 (with regard to the composition, nitrogen N is 79% and oxygen O is 21%), which is discharged from the hearth part 13 Input data relating to molten lead and input data relating to slug (Slag) were input (step S10, FIG. 3).

The balance calculation at the furnace top portion 11 was performed (step S40, FIG. 3), and the heat dissipated at the furnace top portion 11, that is, the heat loss, was calculated as 5.8 GJ / hr. In addition, the temperature of the sintered ore in the stock line was 300 ° C., the heat quantity was 4.9 GJ / hr, the temperature of the coke was 780 ° C., and the heat quantity was 16.9 GJ / hr. The temperature of the zinc-containing gas sent from the shaft portion 12 was assumed to be 793 ° C., the flow rate was 6.87 × 10 ⁴ Nm ³ / hr, and the heat amount was 79.4 GJ / hr (step S50).

Subsequently, the reaction rates R _{1 to} R ₆ (m ³ atm / K mol) shown below are constants k _{1 to} k ₆ (k ₂ , k ₃ , k ₆ , k ₇ : ml / hr; k ₄ : m ³ / kg hr; k ₅ : l / hr) was input (step S60). In the formula, k ₂ is a value described in Ito et al .: Journal of Resources and Materials, 105 (1989), pp.951-957. k ₃ is, JAClarke and DJFray:... . Trans Inst Min Met, using the values described in 91 (1982) C.26-31. k ₄ is, MASherstobitov et. al .: Izv. Bys. Ucheb. Zaved., 8 (1965), was used values described Pp.10-15. k ₅ is, YVTsvetov and DMChizhikov:... Trudy Inst Met, 2 (1957), was used values described Pp.65-77. The values described in Murayama et al .: Iron and Steel, 63 (1977), pp. 1099-1107 were used for k ₆ and k ₇ .

In the formula, N _j represents the number of particles per unit volume (/ m ³ (bed)). P _g represents the gas pressure (atm). K _fi represents the mass transfer coefficient (m / hr) of the i component. ρ _c represents coke density (kg / m ³ (bed)). C ⁰ _PbO represents the initial concentration (kmol / m ³ (bed)) of PbO. d _s represents the particle size (m) of the sintered ore, and d _c represents the particle size (m) of the coke. φ _n represents the shape factor of the solid as a factor for correcting the deviation of the particle from the sphere. R represents a gas constant (m ³ atm / K Kmol). E _fn represents a reaction effectiveness coefficient as a coefficient for correcting the reactivity of particles (in this case, coke) in the reaction of the n formula.

Further, the diffusion coefficient in sintered ore (D _s : m ² / hr), the diffusion coefficient in coke (D _c : m ² / hr) in the formula, and the equilibrium concentration of CO in the reaction of formula (2) (x ^e2 _CO ), Equilibrium concentration of Zn (x ^e3 _Zn ) in the reaction of formula (3), reaction effectiveness factor (E _f4 ) in the reaction of formula (4), A ₁ , A ₂ , B ₁ , B ₂ , C, W, The equilibrium concentrations x ^e6 _CO and x ^e7 _CO of each gas are values calculated by the following formulas.

In the formula, K ₃ , K ₄ , K ₅ , and K ₆ are the equilibrium constants of reactions (3), (4), (5), and (6), respectively. The j component labyrinth ξ _j , the coke effective diffusion coefficient D _c (m ² / hr), and the value η were determined by the following equations.

  Each parameter change of the shaft portion 12 is calculated (step S70), the balance calculation in the shaft portion 12 is performed based on the obtained result (step S80), and the balance calculation in the hearth portion 13 is further performed (step S90). .

In this calculation result, the sintered ore (Sinter) discharged from the shaft portion 12 to the hearth portion 13 has a heat quantity of 20.9 GJ / hr at a temperature of 1100 ° C., a flow rate of 23.1 t / hr, and coke. (Cokes) was estimated to have a calorific value of 28.6 GJ / hr at a temperature of 1263 ° C., a flow rate of 12.1 t / hr. The zinc-containing gas (Gas) discharged from the shaft portion 12 to the furnace top portion 11 is estimated to have a heat amount of 79.4 GJ / hr at a temperature of 793 ° C. and a flow rate of 6.87 × 10 ⁴ Nm ³ / hr. It was done. The heat dissipated in the shaft portion 12, that is, the heat loss, was estimated to be 3.1 GJ / hr.

Subsequently, the zinc-containing gas (Gas) discharged from the hearth part 13 to the shaft part 12 has a heat quantity of 157.3 GJ / hr at a temperature of 1497 ° C. and a flow rate of 6.29 × 10 ⁴ Nm ³ / hr. Was estimated. Further, it was estimated that the heat dissipated in the hearth 13, that is, the heat loss, was 20.0 GJ / hr. Further, the total heat dissipated from the sum of the heat dissipated from the shaft 12 and the hearth 13 was calculated to be 23.1 GJ / hr.

[Example 1]
In analyzing the actual operation using the zinc smelting method according to the present invention, as shown in Table 2 below, the entire amount of the calcined product is introduced from the inlet of the hearth and the entire amount of coke is introduced from the top of the furnace. The balance calculation similar to the balance calculation shown in the reference example 1 is performed except that the condition to perform is input, and the result is shown.

  According to this example, the heat dissipated at the furnace top 11 was 3.1 GJ / hr, the heat dissipated at the shaft 12 was 0.6 GJ / hr, and the heat dissipated at the hearth 13 was 10.8 GJ / hr. This corresponds to about 54%, 22%, and 54% of Reference Example 1, respectively. Thereby, the heat loss concerning zinc refinement can be effectively reduced.

  In addition, the solution loss reaction at the shaft portion 12 and the amount of heat due to the reaction both decreased to about 50% of the system calculated in the reference example. As a result, the amount of coke used can be reduced from 14.2 t / Hr (966 kg / Zn-t) to 13.7 t / Hr (934 kg / Zn-t).

  In addition, since the fired product is not introduced from the furnace top portion 11, no reduction reaction of ZnO occurs in the shaft portion 12. The reduction of the gas temperature at the shaft portion 12 is suppressed by the reduction reaction not occurring and the reduction of the solution loss reaction. As a result, since the internal temperature exceeds 1000 ° C. over the entire shaft portion 12, reoxidation of zinc (Zn) does not occur. In addition, since the gas temperature of the zinc-containing gas sent from the shaft portion 12 to the furnace top portion 11 is sufficiently high, the amount of preheated gas (Top Air) introduced into the furnace top portion 11 can be suppressed, and zinc can be suppressed. Energy saving can be expected in production.

[Reference Example 2]
As shown in Table 3 below, the balance calculation similar to the balance calculation of Reference Example 1 is performed except that the entire amount of the calcined product and coke is introduced from the hearth 13, and the result is shown.

  Compared to Reference Example 1 and Example 1, although the disadvantages due to the solution loss reaction in the shaft portion 12 can be eliminated, the total amount of coke introduced is larger than that in Example 1. This is because the disadvantage that the heat supply to the hearth part 13 corresponding to the temperature rise of the coke sent to the hearth part 13 by the heat exchange in the shaft part 12 exceeds the merit that the solution loss reaction does not occur. Inferred to be the cause.

[Example 2]
In analyzing the actual operation using the zinc smelting method according to the present invention, as shown in Table 4 below, the entire amount of the calcined product is introduced from the inlet of the hearth and half of the coke is introduced from the top of the furnace. In addition, the balance calculation similar to the balance calculation shown in Reference Example 1 is performed except that the condition for introducing the remaining half amount from the inlet of the hearth is input, and the result is shown.

  Compared to Reference Examples 1 and 2, this example can reduce the total amount of coke introduced. For this reason, a solution loss reaction can be effectively suppressed to such an extent that it does not influence zinc production.

  Moreover, since the dissipated heat can be reduced as in the first embodiment, the heat loss for zinc smelting can be effectively reduced. Moreover, since the fall of the gas temperature in the shaft part 12 is suppressed similarly to Example 1, since internal temperature will exceed 1000 degreeC over the whole shaft part 12, reoxidation of zinc (Zn) does not arise. . In addition, since the gas temperature of the zinc-containing gas sent from the shaft portion 12 to the furnace top portion 11 is sufficiently high, the amount of preheated gas (Top Air) introduced into the furnace top portion 11 can be suppressed, and zinc can be suppressed. Energy saving can be expected in production.

It is a figure which shows typically the dry-type zinc smelting blast furnace which performs a state analysis by this invention. It is a figure explaining concentration distribution of zinc content slag in the hearth part of the blast furnace. It is a flowchart for demonstrating one Embodiment of the state analysis method of the dry-type zinc smelting blast furnace which concerns on this invention. In the said embodiment, it is a figure explaining the micro area used as a calculation area. In the said analysis method, it is a figure which represents typically each heat balance of gas, a sintered ore, and coke. It is a figure explaining the unreacted nucleus model of the two interfaces used in the said analysis method, and the unreacted nucleus model of one interface.

Explanation of symbols

11 Furnace Top 12 Shaft 13 Furnace 21, 22 Tuyere 23 Inlet

Claims (17)

Using coke, zinc oxide, lead oxide, a blast furnace for dry zinc smelting retrieve the zinc from calcined product contains at least iron oxide and silicon oxide, at least part of the total introduction amount of the introduced coke a first region for discharging the zinc produced with dropping, a second region at least the reduction reaction of zinc oxide of each component of the calcined product which has passed through the first region is performed as the main reaction, the calcined product and coke In addition to introducing the rest, at least the third region in which the reduction reaction of zinc oxide, lead oxide and iron oxide and the oxidation reaction of carbon are carried out as a main reaction is continuously formed among the baked products that have passed through the second region. A method of analyzing a reaction state in a blast furnace using a computer system,
Input the value for specifying the shape of the furnace as the reaction field specific value, input the introduction temperature, the introduction amount and the composition of the coke and the fired product introduced into the first and third regions as the introduction initial value, The composition and flow rate of the gas introduced into the first region, the composition and flow rate of the gas containing purified zinc discharged from the first region, and the temperature, composition and flow rate of the gas introduced into the third region are operated. Operation condition input stage to input as data,
The composition and flow rate of the gas introduced into the first region, the composition and flow rate of the gas introduced into the third region, and the composition of the fired product and coke introduced into the first region, which are input in the operation condition input stage. DOO using, based on the carbon monoxide producing reaction and carbon dioxide production reaction carried out in each region, a front Symbol rate calculation step of calculating a flow rate of carbon monoxide and carbon dioxide produced in the first region,
A temperature setting step for setting and inputting the temperature of the gas discharged from the first region;
The composition and flow rate of the gas introduced into the first region and the composition and flow rate of the gas containing purified zinc discharged from the first region, which are input in the operation condition input step, and obtained in the flow rate calculation step. The mass balance of the reaction in the first region based on the chemical reaction performed in the first region using the flow rate of carbon monoxide and carbon dioxide and the gas temperature set and input in the temperature setting step. And a first region balance calculation stage for calculating a material balance, a heat balance and a composition of a gas containing zinc introduced from the second region,
Mass balance, heat balance and composition of the gas containing zinc discharged from the second region calculated in the first region balance calculation step, the reaction field specific value and the introduction input in the operation condition input step Using the initial value, based on the rate constant and equilibrium constant of each reduction reaction, the flow rate and temperature change of the whole gas component, coke, and calcined product in the vertical section of the second region, The pressure change of each gas composition in the minute section and the change in the reaction rate of each solid composition in the minute section are calculated, and the coke and sintering in the second region are calculated based on the obtained values. A second region balance calculation stage for calculating the mass balance of each of the mineral and gas components, the heat balance and the heat loss of the entire second region;
The temperature, composition and amount of the calcined product and coke introduced into the third region and the temperature, composition and flow rate of the gas introduced into the region, and the second region balance calculation, which are input in the operation condition input step. A third region balance calculation stage for calculating the material balance, heat balance and heat loss in the third region based on the chemical reaction carried out in the third region using the material balance and heat balance obtained in the step; The state analysis method in the dry-type zinc smelting blast furnace characterized by having. 2. The method according to claim 1, wherein the first region drops at least a part of a total amount of coke introduced and a fired product while discharging generated zinc. The second region is characterized in that at least a reduction reaction of zinc oxide and a reduction reaction of lead oxide and iron oxide among the components of the fired product that has passed through the first region are performed as main reactions. Item 2. The method according to Item 1. The method according to claim 1, wherein the fired product introduced into the third region is 1 to 100% of the whole. The method according to claim 1, wherein coke introduced into the third region is 40 to 60% of the whole. The method according to claim 1, wherein the gas introduced into the third region contains 30 to 100% oxygen. The method according to claim 1, wherein the reaction represented by the following reaction formula is set as a reaction performed in the second region:

In the second region balance calculation stage, the flow rate and temperature change of the entire gas component, coke and sinter, and the pressure change of each gas composition in the micro section, and the solid composition of the micro section The method according to claim 1, wherein a differential equation represented by a minute change of each change per minute section in consideration of a gas generated in the blast furnace is used as the reaction rate change. The method according to claim 1, wherein the reaction field specific value used in the second region balance calculation step is a cross-sectional area of the furnace in each minute section in the height and height direction of the furnace. The method according to claim 1, wherein a chemical reaction represented by the following reaction formula is set as a chemical reaction performed in the first region:

The method according to claim 1, wherein a chemical reaction represented by the following reaction formula and a reaction for producing a slug containing an unreacted oxide are set as chemical reactions performed in the third region:

A zinc smelting method for extracting zinc from a fired product containing at least zinc oxide, lead oxide, iron oxide and silicon oxide using coke,
With coke is introduced, a first region for discharging the generated zinc, and a second region for delivering the generated zinc to the first region, as the reducing reaction of at least zinc oxide main reaction of the calcined product Using a blast furnace in which a third region in which zinc is produced is continuously formed, and
Introducing at least part of the total introduction amount of the coke in the first region,
A zinc smelting method characterized by introducing the fired product and the remainder of coke into the third region.   The method according to claim 12, wherein the first region is configured to discharge the generated zinc while coke and a fired product are introduced. 13. At least a part of the total amount of coke introduced and a fired product are introduced into the first region when introducing at least a part of the total amount of coke introduced into the first region. Method. The method of claim 1 2, characterized in that 1 to 100% of the entire fired product to be introduced into the third region. The method of claim 1 2, characterized in that 40 to 60% of the total coke to be introduced into the third region. The method of claim 1 2 in the third region, oxygen is characterized in that it is introduced 30% to 100% gas contained.

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