CN110929445B - Method and system for obtaining temperature distribution in carbomorphism production carbonization chamber - Google Patents
Method and system for obtaining temperature distribution in carbomorphism production carbonization chamber Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 111
- 238000003763 carbonization Methods 0.000 title claims abstract description 63
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 38
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 214
- 238000006243 chemical reaction Methods 0.000 claims abstract description 128
- 239000003245 coal Substances 0.000 claims abstract description 105
- 229910052742 iron Inorganic materials 0.000 claims abstract description 101
- 238000000197 pyrolysis Methods 0.000 claims abstract description 81
- 238000004364 calculation method Methods 0.000 claims abstract description 71
- 230000008569 process Effects 0.000 claims abstract description 68
- 238000007670 refining Methods 0.000 claims abstract description 60
- 238000001704 evaporation Methods 0.000 claims abstract description 59
- 230000008020 evaporation Effects 0.000 claims abstract description 57
- 239000000571 coke Substances 0.000 claims abstract description 54
- 239000000843 powder Substances 0.000 claims abstract description 54
- 238000006722 reduction reaction Methods 0.000 claims abstract description 50
- 239000002244 precipitate Substances 0.000 claims abstract description 43
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000010521 absorption reaction Methods 0.000 claims abstract description 30
- 238000012546 transfer Methods 0.000 claims abstract description 30
- 239000000047 product Substances 0.000 claims description 61
- 238000004939 coking Methods 0.000 claims description 19
- 230000005012 migration Effects 0.000 claims description 18
- 238000013508 migration Methods 0.000 claims description 18
- 230000004913 activation Effects 0.000 claims description 12
- 230000008859 change Effects 0.000 claims description 12
- 238000010276 construction Methods 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 9
- 239000002817 coal dust Substances 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims 1
- 230000009467 reduction Effects 0.000 description 4
- 235000010689 Lufa Nutrition 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
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- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
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- 230000008878 coupling Effects 0.000 description 1
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- 238000011161 development Methods 0.000 description 1
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- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
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- 238000012986 modification Methods 0.000 description 1
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Abstract
A method and a system for obtaining temperature distribution in a carbonization chamber of ferrocoke production, wherein the method comprises the following steps: calculating chemical reaction heat generated in unit time of precipitate in the pyrolysis chemical reaction of the coal, water evaporation absorption heat and heat generated in the reduction reaction of iron ore powder in the ferrocoke refining process; constructing a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in unit time of educts in the pyrolysis chemical reaction of the matched coal, water evaporation absorption heat and heat generated by reduction reaction of iron ore powder in the iron coke refining process; and replacing the heat conduction differential equation with a corresponding difference quotient to obtain a finite difference calculation model in algebraic form, and calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model. The method combines the finite difference model with the heat calculation of main reaction in the production process of the ferrocoke to obtain the method for rapidly obtaining the temperature distribution of the carbonization chamber in the production process of the ferrocoke.
Description
Technical Field
The invention relates to the field of blast furnace ironmaking, in particular to a method and a system for obtaining temperature distribution in a carbonization chamber in iron coke production.
Background
Blast furnace ironmaking is still the main process of ironmaking at present, but with the development of technology and the advancement of operation, the blast furnace is very close to theoretical equilibrium, and improvement of the device or use of new materials are required for further reduction of the fuel ratio of the blast furnace.
The iron coke is a novel blast furnace composite furnace charge with high reactivity, the production of the iron coke can increase the matching proportion of non-coking coal, the reasonable utilization of coal resources is realized, and the reactivity of the iron coke is obviously higher than that of common coke, and the iron coke is used in a blast furnace to reduce the temperature of a heat preservation area of the blast furnace, so that the effects of energy conservation and emission reduction are achieved.
Currently, the production modes of ferrocoke mainly comprise a briquetting-shaft furnace method and a chamber type Jiao Lufa, and published patents CN201180015873.4, CN201080035355.4 and the like introduce a briquetting-shaft furnace method ferrocoke production process, and the chamber type Jiao Lufa is also subjected to industrial experiments by Japanese new day iron. In the production process of the ferrocoke, the temperature distribution in the carbonization chamber has an important influence on the quality of the ferrocoke, but no method for acquiring the temperature distribution in the production process of the ferrocoke exists at present.
Disclosure of Invention
Aiming at the technical problems, the invention provides a method and a system for acquiring the temperature distribution in a carbonization chamber of ferrocoke production, and the specific scheme is as follows:
as a first aspect of the present invention, there is provided a method of obtaining a temperature distribution in a coking chamber in the production of ferrocoke, the method comprising:
calculating chemical reaction heat generated in unit time of precipitate in the pyrolysis chemical reaction of the coal in the process of refining the iron coke;
calculating the evaporation and absorption heat of water in the pyrolysis chemical reaction of the coal in the process of refining the iron coke;
calculating heat generated by the reduction reaction of the iron ore powder in the iron coke refining process;
constructing a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the matched coal, and heat absorbed by evaporation of water in the pyrolysis chemical reaction of the matched coal and generated by reduction reaction of iron ore powder in the iron coke refining process;
and replacing the heat conduction differential equation with a corresponding difference quotient to obtain a finite difference calculation model in algebraic form, and calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model.
Further, calculating the chemical reaction heat generated per unit time of the precipitate in the pyrolysis chemical reaction of the coal in the ferrocoke refining process specifically comprises:
the relationship between the rate of precipitated product and temperature is obtained according to the Arrhenius equation and is expressed as the following formula I:
equation one:
describing the activation energy in the first formula according to a modified Rosin-Rammler equation to obtain the following second formula:
formula II: fi (E) =exp (- ((E-E) 0 )/ε) β )；
The chemical reaction heat generated per unit time of the precipitate calculated from the formulas one and two is expressed as the following formula three:
and (3) a formula III: q (Q) r,i ＝h r,i R r,i m i ；
Wherein delta is the percentage of the volatilized fractional product precipitated at time t, and the unit is; k isPre-finger factor in s -1 The method comprises the steps of carrying out a first treatment on the surface of the E is activation energy, and the unit is kJ/mol; r is a gas constant, and the unit is 8.314 kJ/(mol.K); t is temperature, and the unit is K; subscript i represents the thermolytically precipitated ith product; h is a r,i The unit of the chemical reaction heat of the i-th product which is pyrolyzed out is J/kg; r is R r,i The reaction rate of the ith product which is pyrolyzed out is expressed as s -1 ；m i The mass of the i-th product which is pyrolyzed out is kg, parameter E 0 Epsilon and beta are determined by the coal dust grades.
Further, mass m of the thermally separated i-th product i The calculation method specifically comprises the following steps:
the calculation is performed through a pyrolysis product model of the pulverized coal, and the pyrolysis product model of the pulverized coal is calculated according to product balance and is expressed as the following formula IV:
equation four:
wherein m is coal The unit is kg and m for mixing the mass of the coal i Is the mass of the i-th product which is pyrolyzed out, the unit is kg, w j The element j accounts for the total element mass of all products in percent.
Further, the pyrolysis products are made n, and an equation set of pyrolysis yield is obtained, which is expressed as the following formula five:
formula five:
wherein A is ij Is a constant matrix, m j B) final mass of coke and of the pyrolytically separated component products i Is a constant vector.
Further, calculating the water evaporation and absorption heat in the pyrolysis chemical reaction of the coal in the ferrocoke refining process specifically comprises the following steps:
the method for calculating the evaporation and absorption heat of the water adopts a nonlinear migration model, and the calculation mode is to divide the water drying process into two stages, and the two stages are correspondingly evaporatedA certain amount of moisture, a temperature range [ T ] of the ith stage i1 ,T i2 ]The evaporation capacity of the internal moisture is k i The latent heat of phase change required for temperature change of 1K in this temperature range is expressed as the following formula six:
formula six: q (Q) m ＝h m k i /(T i2 -T i1 )；
K in formula six i Calculated according to the following equation seven:
formula seven: k (k) i ＝R m τ；
Moisture migration Rate R in equation seven m Can be calculated according to the following equation eight:
wherein h is m The unit is J/kg, which is the latent heat of evaporation of water; r is R m The unit is kg/s for moisture migration rate; τ is the heating time in s; r is (r) t The temperature rise rate of coal (coke) is expressed as K/s.
Further, the first stage moisture evaporation amount k 1 85-90%; the evaporation capacity k2 of the second stage is 10-15%.
Further, calculating the heat generated by the reduction reaction of the iron ore powder in the iron coke refining process specifically comprises:
the iron ore powder is reduced by the precipitate X in the production process of the iron coke, and the gradual reduction reaction formula of the iron ore powder is as follows:
3Fe 2 O 3 +X＝2Fe 3 O 4 +XO；
Fe 3 O 4 +X＝3FeO+XO；
FeO+X＝Fe+XO；
and calculating the heat generated by the reduction reaction of the iron ore powder according to a step-by-step reaction formula.
Further, a heat conduction differential equation for constructing heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in a pyrolysis chemical reaction of the blended coal, and heat generated by a reduction reaction of iron ore powder in a ferrocoke refining process by evaporating and absorbing water in the pyrolysis chemical reaction of the blended coal is specifically as follows:
for a two-dimensional unsteady heat transfer process, the heat conduction differential equation is as follows:
wherein ρ is the density of the blended coal, and the unit is kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the c is the specific heat of the blended coal, and the unit is J/(kg.K); lambda is the heat conductivity coefficient of the blended coal, and the unit is W/(m.K); s is an internal heat source with the unit of W/m 3 The internal heat source S comprises chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the blended coal, and heat generated by a reduction reaction of iron ore powder in the refining process of iron coke, wherein the heat is absorbed by evaporation of water in the pyrolysis chemical reaction of the blended coal;
the given boundary conditions are: the inside of the carbonization chamber is treated according to the constant temperature wall surface, namely:
T xc ＝T yc ＝T w0 ；
the center surface of the carbonization chamber is treated according to a symmetrical surface, namely:
further, calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model specifically comprises the following steps: gradually calculating until the temperature of the center point of the carbonization chamber reaches T based on the finite difference calculation model end Until that point.
Further, the T is end The interval range is 900-1050 ℃.
As a second aspect of the present invention, there is provided a system for obtaining a temperature distribution in a coking chamber for the production of ferrocoke, the system comprising: the system comprises a first heat calculation module, a second heat calculation module, a third heat calculation module, a heat transfer model construction module and a temperature distribution calculation module;
the first heat calculation module is used for calculating chemical reaction heat generated in unit time of precipitate in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process;
the second heat calculation module is used for calculating the evaporation and absorption heat of water in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process;
the third heat calculation module is used for calculating heat generated by the reduction reaction of the iron ore powder in the iron coke refining process;
the heat transfer model construction module is used for constructing a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the matched coal, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated by a reduction reaction of iron ore powder in the iron coke refining process;
the temperature distribution calculation module is used for replacing the heat conduction differential equation with a corresponding difference quotient to obtain a finite difference calculation model in algebraic form, and calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model.
Further: the first heat calculation module is used for calculating chemical reaction heat generated in unit time of precipitate in pyrolysis chemical reaction of the matched coal in the ferrocoke refining process, and specifically comprises the following steps:
the relationship between the rate of precipitated product and temperature is obtained according to the Arrhenius equation and is expressed as the following formula I:
equation one:
describing the activation energy in the first formula according to a modified Rosin-Rammler equation to obtain the following second formula:
formula II: fi (E) =exp (- ((E-E) 0 )/ε) β )；
The chemical reaction heat generated per unit time of the precipitate calculated from the formulas one and two is expressed as the following formula three:
and (3) a formula III: q (Q) r,i ＝h r,i R r,i m i ；
Wherein delta is the partial yield of the volatilizationThe percentage of the substance precipitated at time t is expressed in units of; k is a pre-finger factor in s -1 The method comprises the steps of carrying out a first treatment on the surface of the E is activation energy, and the unit is kJ/mol; r is a gas constant, and the unit is 8.314 kJ/(mol.K); t is temperature, and the unit is K; subscript i represents the thermolytically precipitated ith product; h is a r,i The unit of the chemical reaction heat of the i-th product which is pyrolyzed out is J/kg; r is R r,i The reaction rate of the ith product which is pyrolyzed out is expressed as s -1 ；m i The mass of the i-th product which is pyrolyzed out is kg, parameter E 0 Epsilon and beta are determined by the coal dust grades;
the second heat calculation module calculates the water evaporation and absorption heat in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process, and specifically comprises the following steps:
the moisture evaporation and absorption heat is calculated by adopting a nonlinear migration model, wherein the calculation mode is to divide the moisture drying process into two stages, and the two stages correspondingly evaporate a certain amount of moisture, if the temperature range [ T ] of each stage i1 ,T i2 ]The evaporation capacity of the internal moisture is k i The latent heat of phase change required for temperature change of 1K in this temperature range is expressed as the following formula six:
formula six: q (Q) m ＝h m k i /(T i2 -T i1 )；
K in formula six i Calculated according to the following equation seven:
formula seven: k (k) i ＝R m τ；
Moisture migration Rate R in equation seven m Can be calculated according to the following equation eight:
wherein h is m The unit is J/kg, which is the latent heat of evaporation of water; r is R m The unit is kg/s for moisture migration rate; τ is the heating time in s; r is (r) t The heating rate of coal (coke) is K/s;
the third heat calculation module calculates heat generated by the reduction reaction of the iron ore powder in the iron coke refining process, and specifically comprises the following steps:
the iron ore powder is reduced by the precipitate X in the production process of the iron coke, and the gradual reduction reaction formula of the iron ore powder is as follows:
3Fe 2 O 3 +X＝2Fe 3 O 4 +XO；
Fe 3 O 4 +X＝3FeO+XO；
FeO+X＝Fe+XO；
calculating the heat generated by the reduction reaction of the iron ore powder according to a step-by-step reaction formula;
the heat transfer model construction module constructs a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in a pyrolysis chemical reaction of the matched coal, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated by a reduction reaction of iron ore powder in a ferrocoke refining process, and specifically comprises the following steps:
for a two-dimensional unsteady heat transfer process, the heat conduction differential equation is as follows:
wherein ρ is the density of the blended coal, and the unit is kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the c is the specific heat of the blended coal, and the unit is J/(kg.K); lambda is the heat conductivity coefficient of the blended coal, and the unit is W/(m.K); s is an internal heat source with the unit of W/m 3 The internal heat source S comprises chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the blended coal, and heat generated by a reduction reaction of iron ore powder in the refining process of iron coke, wherein the heat is absorbed by evaporation of water in the pyrolysis chemical reaction of the blended coal;
the given boundary conditions are: the inside of the carbonization chamber is treated according to the constant temperature wall surface, namely:
T xc ＝T yc ＝T w0 ；
the center surface of the carbonization chamber is treated according to a symmetrical surface, namely:
the method for calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model specifically comprises the following steps: gradually calculating until the temperature of the center point of the carbonization chamber reaches T based on the finite difference calculation model end Until that point.
The invention has the following beneficial effects:
according to the invention, a heat conduction differential equation of heat transfer inside a carbonization chamber is constructed by calculating chemical reaction heat generated in unit time of educts in a pyrolysis chemical reaction of the matched coal in the ferrocoke refining process, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated by a reduction reaction of iron ore powder in the ferrocoke refining process; and constructing a heat differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of educts in the pyrolysis chemical reaction of the matched coal, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated in a reduction reaction of iron ore powder in the ferrocoke refining process, so as to obtain a algebraic finite difference calculation model, and combining the finite difference model with heat calculation of main reaction in the ferrocoke production process to obtain the method for rapidly obtaining the temperature distribution of the carbonization chamber in the ferrocoke production process.
Drawings
FIG. 1 is a flow chart of a method for obtaining temperature distribution in a coking chamber in iron coke production according to an embodiment of the present invention;
fig. 2 is a finite difference computation model provided in an embodiment of the present invention.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and fully with reference to the accompanying drawings, in which it is evident that the embodiments described are only some, but not all embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
As shown in fig. 1, as a first embodiment of the present invention, there is provided a method of obtaining a temperature distribution in a coking chamber for the production of ferrocoke, the method comprising:
calculating chemical reaction heat generated in unit time of precipitate in the pyrolysis chemical reaction of the coal in the process of refining the iron coke;
calculating the evaporation and absorption heat of water in the pyrolysis chemical reaction of the coal in the process of refining the iron coke;
calculating heat generated by the reduction reaction of the iron ore powder in the iron coke refining process;
constructing a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the matched coal, and heat absorbed by evaporation of water in the pyrolysis chemical reaction of the matched coal and generated by reduction reaction of iron ore powder in the iron coke refining process;
and replacing the heat conduction differential equation with a corresponding difference quotient to obtain a finite difference calculation model in algebraic form, and calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model.
As shown in FIG. 2, the unstable two-dimensional heat transfer model is characterized in that 1/4 of the horizontal cross section of the carbonization chamber is selected for grid division, adjacent two sides of the 1/4 of the horizontal cross section of the carbonization chamber are respectively used as an x axis and a y axis, the intersection points of the adjacent two sides are used as coordinate axis dots, wherein the point A is the center point of the carbonization chamber, namely the center point of the horizontal cross section of the carbonization chamber, the point A of the center point A of the carbonization chamber is positioned on the y axis, the point B is the inner point of the 1/4 of the horizontal cross section of the carbonization chamber, the point C is the boundary point of the 1/4 of the horizontal cross section of the carbonization chamber, namely the intersection point of the x axis and the inner wall of the carbonization chamber, and the grid size is adjusted according to practical conditions.
Preferably, calculating the chemical reaction heat generated per unit time of the precipitate in the pyrolysis chemical reaction of the coal blend in the ferrocoke refining process specifically includes:
the kinetics of volatile precipitation is described by a set of first-order parallel reactions, and the relationship between the rate of precipitated product and temperature is obtained according to the Arrhenius equation, expressed as the following formula one:
equation one:
describing the activation energy in the first formula according to a modified Rosin-Rammler equation to obtain the following second formula:
formula II: fi (E) =exp (- ((E-E) 0 )/ε) β )；
The chemical reaction heat generated per unit time of the precipitate calculated from the formulas one and two is expressed as the following formula three:
and (3) a formula III: q (Q) r,i ＝h r,i R r,i m i ；
Wherein delta is the percentage of the volatilized fractional product precipitated at time t, and the unit is; k is a pre-finger factor in s -1 The method comprises the steps of carrying out a first treatment on the surface of the E is activation energy, and the unit is kJ/mol; r is a gas constant, and the unit is 8.314 kJ/(mol.K); t is temperature, and the unit is K; subscript i represents the thermolytically precipitated ith product; h is a r,i The unit of the chemical reaction heat of the i-th product which is pyrolyzed out is J/kg; r is R r,i The reaction rate of the ith product which is pyrolyzed out is expressed as s -1 ；m i The mass of the i-th product which is pyrolyzed out is kg, parameter E 0 Epsilon and beta are determined by the coal dust grades.
Preferably, mass m of the thermally separated i-th product i The calculation method specifically comprises the following steps:
calculation of m by pyrolysis product model of pulverized coal i The pyrolysis product model of the pulverized coal is calculated according to the product balance and is expressed as the following formula IV:
equation four:
wherein m is coal The unit is kg and m for mixing the mass of the coal i Is the mass of the i-th product which is pyrolyzed out, the unit is kg, w j The element j accounts for the total element mass of all products in percent. In addition, algebraic relational expressions and the relation between coke and volatile matters are defined according to the relation between certain products and elements to form a set of equations for predicting pyrolysis products.
Preferably, the pyrolysis products are n, and the pyrolysis products are n, so as to obtain an equation set of pyrolysis yield, which is expressed as the following equation five:
formula five:
wherein A is ij Is a constant matrix, m j B) final mass of coke and of the pyrolytically separated component products i Is a constant vector.
Preferably, calculating the water evaporation and absorption heat in the pyrolysis chemical reaction of the coal in the ferrocoke refining process specifically comprises the following steps:
the method for calculating the evaporation and absorption heat of the water by adopting a nonlinear migration model is characterized in that the water drying process is divided into two stages, a certain amount of water is correspondingly evaporated in the two stages, and the temperature range of the ith stage is [ T ] i1 ,T i2 ]The evaporation capacity of the internal moisture is k i The latent heat of phase change required for temperature change of 1K in this temperature range is expressed as the following formula six:
formula six: q (Q) m ＝h m k i /(T i2 -T i1 )；
K in formula six i Calculated according to the following equation seven:
formula seven: k (k) i ＝R m τ；
Moisture migration Rate R in equation seven m Can be calculated according to the following equation eight:
wherein h is m The unit is J/kg, which is the latent heat of evaporation of water; r is R m The unit is kg/s for moisture migration rate; τ is the heating time in s; r is (r) t The temperature rise rate of coal (coke) is expressed as K/s.
Preferably, the first stage moisture evaporation amount k 1 85-90%; the evaporation capacity k2 of the second stage is 10-15%.
Preferably, calculating the heat generated by the reduction reaction of the iron ore powder in the ferrocoke refining process specifically comprises:
the iron ore powder is reduced by the precipitate X in the production process of the iron coke, and the gradual reduction reaction formula of the iron ore powder is as follows:
3Fe 2 O 3 +X＝2Fe 3 O 4 +XO；
Fe 3 O 4 +X＝3FeO+XO；
FeO+X＝Fe+XO；
and calculating the heat generated by the reduction reaction of the iron ore powder according to a step-by-step reaction formula.
In addition, in the ferrocoke refining process, the pyrolysis of the blended coal and the reduction of the iron ore powder are not independent reactions, but a pair of mutually coupled reactions, the reaction speeds of the two are required to be corrected, and the coupling coefficients of the pyrolysis product generation rate and the reduction rate of the iron ore powder are required to be corrected
And->
Obtained by experimental analysis.
Preferably, the heat conduction differential equation for constructing the heat transfer inside the carbonization chamber based on the chemical reaction heat generated in the unit time of the precipitate in the pyrolysis chemical reaction of the blended coal, the evaporation and absorption heat of the moisture in the pyrolysis chemical reaction of the blended coal and the heat generated by the reduction reaction of the iron ore powder in the iron coke refining process is specifically as follows:
for a two-dimensional unsteady heat transfer process, the heat conduction differential equation is as follows:
wherein T represents temperature, x and y respectively represent the horizontal and vertical axes of 1/4 cross section of the carbonization chamber, tau represents time, rho represents density of the blended coal, and the unit is kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the c is the specific heat of the blended coal, and the unit is J/(kg.K); lambda is the coefficient of heat conductivity of the coal blendThe unit is W/(m.K); s is an internal heat source with the unit of W/m 3 The internal heat source S comprises chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the blended coal, and heat generated by a reduction reaction of iron ore powder in the refining process of iron coke, wherein the heat is absorbed by evaporation of water in the pyrolysis chemical reaction of the blended coal;
the given boundary conditions are: the inside of the carbonization chamber is treated according to the constant temperature wall surface, namely:
T xc ＝T yc ＝T w0 ；
the center surface of the carbonization chamber is treated according to a symmetrical surface, namely:
wherein T is xc The temperature of the point identical to the abscissa of point C, T yc Represents the temperature of the point which is the same as the ordinate of the point C, T w0 Representing the temperature of the furnace wall of the carbonization chamber, T xo Temperature, T, of point with abscissa 0 yA The temperature at the point having the same ordinate as the point a is shown.
Preferably, calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model specifically comprises: gradually calculating until the temperature of the central point A of the carbonization chamber reaches T based on the finite difference calculation model end Until that point.
Preferably, said T end The interval range is 900-1050 ℃.
As a second embodiment of the present invention, there is provided a system for acquiring a temperature distribution in a coking chamber for production of ferrocoke, the system comprising: the system comprises a first heat calculation module, a second heat calculation module, a third heat calculation module, a heat transfer model construction module and a temperature distribution calculation module;
the first heat calculation module is used for calculating chemical reaction heat generated in unit time of precipitate in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process;
the second heat calculation module is used for calculating the evaporation and absorption heat of water in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process;
the third heat calculation module is used for calculating heat generated by the reduction reaction of the iron ore powder in the iron coke refining process;
the heat transfer model construction module is used for constructing a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the matched coal, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated by a reduction reaction of iron ore powder in the iron coke refining process;
the temperature distribution calculation module is used for replacing the heat conduction differential equation with a corresponding difference quotient to obtain a finite difference calculation model in algebraic form, and calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model.
Preferably: the first heat calculation module is used for calculating chemical reaction heat generated in unit time of precipitate in pyrolysis chemical reaction of the matched coal in the ferrocoke refining process, and specifically comprises the following steps:
the relationship between the rate of precipitated product and temperature is obtained according to the Arrhenius equation and is expressed as the following formula I:
equation one:
describing the activation energy in the first formula according to a modified Rosin-Rammler equation to obtain the following second formula:
formula II: fi (E) =exp (- ((E-E) 0 )/ε) β )；
The chemical reaction heat generated per unit time of the precipitate calculated from the formulas one and two is expressed as the following formula three:
and (3) a formula III: q (Q) r,i ＝h r,i R r,i m i ；
Wherein delta is the percentage of the volatilized fractional product precipitated at time t, and the unit is; k is a pre-finger factor in s -1 The method comprises the steps of carrying out a first treatment on the surface of the E is activation energy, and the unit is kJ/mol; r is a gas constant, and the unit is 8.314 kJ/(mol.K); t is temperature, and the unit is K; subscript i denotes pyrolytically separatedAn ith product; h is a r,i The unit of the chemical reaction heat of the i-th product which is pyrolyzed out is J/kg; r is R r,i The reaction rate of the ith product which is pyrolyzed out is expressed as s -1 ；m i The mass of the i-th product which is pyrolyzed out is kg, parameter E 0 Epsilon and beta are determined by the coal dust grades;
the second heat calculation module calculates the water evaporation and absorption heat in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process, and specifically comprises the following steps:
the moisture evaporation and absorption heat is calculated by adopting a nonlinear migration model, wherein the calculation mode is to divide the moisture drying process into two stages, and the two stages correspondingly evaporate a certain amount of moisture, if the temperature range [ T ] of each stage i1 ,T i2 ]The evaporation capacity of the internal moisture is k i The latent heat of phase change required for temperature change of 1K in this temperature range is expressed as the following formula six:
formula six: q (Q) m ＝h m k i /(T i2 -T i1 )；
K in formula six i Calculated according to the following equation seven:
formula seven: k (k) i ＝R m τ；
Moisture migration Rate R in equation seven m Can be calculated according to the following equation eight:
wherein h is m The unit is J/kg, which is the latent heat of evaporation of water; r is R m The unit is kg/s for moisture migration rate; τ is the heating time in s; r is (r) t The heating rate of coal (coke) is K/s;
the third heat calculation module calculates heat generated by the reduction reaction of the iron ore powder in the iron coke refining process, and specifically comprises the following steps:
the iron ore powder is reduced by the precipitate X in the production process of the iron coke, and the gradual reduction reaction formula of the iron ore powder is as follows:
3Fe 2 O 3 +X＝2Fe 3 O 4 +XO；
Fe 3 O 4 +X＝3FeO+XO；
FeO+X＝Fe+XO；
calculating the heat generated by the reduction reaction of the iron ore powder according to a step-by-step reaction formula;
the heat transfer model construction module constructs a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in a pyrolysis chemical reaction of the matched coal, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated by a reduction reaction of iron ore powder in a ferrocoke refining process, and specifically comprises the following steps:
for a two-dimensional unsteady heat transfer process, the heat conduction differential equation is as follows:
wherein ρ is the density of the blended coal, and the unit is kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the c is the specific heat of the blended coal, and the unit is J/(kg.K); lambda is the heat conductivity coefficient of the blended coal, and the unit is W/(m.K); s is an internal heat source with the unit of W/m 3 The internal heat source S comprises chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the blended coal, and heat generated by a reduction reaction of iron ore powder in the refining process of iron coke, wherein the heat is absorbed by evaporation of water in the pyrolysis chemical reaction of the blended coal;
the given boundary conditions are: the inside of the carbonization chamber is treated according to the constant temperature wall surface, namely:
T xc ＝T yc ＝T w0 ；
the center surface of the carbonization chamber is treated according to a symmetrical surface, namely:
the method for calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model specifically comprises the following steps: gradually calculating the carbon based on the finite difference calculation modelTemperature distribution in the coking chamber until the temperature at the central point of the coking chamber reaches the final temperature T end Until that point.
The foregoing description of the preferred embodiments of the invention is not intended to limit the invention to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the invention are intended to be included within the scope of the invention.
Claims (10)
1. A method for obtaining temperature distribution in a carbonization chamber for producing ferrocoke, which is characterized by comprising the following steps:
calculating chemical reaction heat generated in unit time of precipitate in the pyrolysis chemical reaction of the coal in the process of refining the iron coke;
calculating the evaporation and absorption heat of water in the pyrolysis chemical reaction of the coal in the process of refining the iron coke;
calculating heat generated by the reduction reaction of the iron ore powder in the iron coke refining process;
constructing a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the matched coal, and heat absorbed by evaporation of water in the pyrolysis chemical reaction of the matched coal and generated by reduction reaction of iron ore powder in the iron coke refining process;
and replacing the heat conduction differential equation with a corresponding difference quotient to obtain a finite difference calculation model in algebraic form, and calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model.
2. The method for obtaining the temperature distribution in the coking chamber for producing ferrocoke according to claim 1, wherein calculating the chemical reaction heat generated per unit time of the precipitate in the pyrolysis chemical reaction of the coal in the ferrocoke refining process specifically comprises:
the relationship between the rate of precipitated product and temperature is obtained according to the Arrhenius equation and is expressed as the following formula I:
equation one:
describing the activation energy in the first formula according to a modified Rosin-Rammler equation to obtain the following second formula:
formula II: fi (E) =exp (- ((E-E) 0 )/ε) β )；
The chemical reaction heat generated per unit time of the precipitate calculated from the formulas one and two is expressed as the following formula three:
and (3) a formula III: q (Q) r,i ＝h r,i R r,i m i ；
Wherein delta is the percentage of the volatilized fractional product precipitated at time t, and the unit is; k is a pre-finger factor in s -1 The method comprises the steps of carrying out a first treatment on the surface of the E is activation energy, and the unit is kJ/mol; r is a gas constant, and the unit is 8.314 kJ/(mol.K); t is temperature, and the unit is K; subscript i represents the thermolytically precipitated ith product; h is a r,i The unit of the chemical reaction heat of the i-th product which is pyrolyzed out is J/kg; r is R r,i The reaction rate of the ith product which is pyrolyzed out is expressed as s -1 ；m i The mass of the i-th product which is pyrolyzed out is kg, parameter E 0 Epsilon and beta are determined by the coal dust grades.
3. The method for obtaining the temperature distribution in the coking chamber for producing ferrocoke according to claim 2, wherein the mass m of the i-th product obtained by pyrolysis i The calculation method specifically comprises the following steps:
the calculation is performed through a pyrolysis product model of the pulverized coal, and the pyrolysis product model of the pulverized coal is calculated according to product balance and is expressed as the following formula IV:
equation four:
wherein m is coal The unit is kg and m for mixing the mass of the coal i Is the mass of the i-th product which is pyrolyzed out, the unit is kg, w j The element j accounts for the total element mass of all products in percent.
4. The method for obtaining the temperature distribution in the coking chamber for producing ferrocoke according to claim 1, wherein calculating the water evaporation and absorption heat in the pyrolysis chemical reaction of the coal during the ferrocoke refining process specifically comprises:
the method for calculating the evaporation and absorption heat of the water by adopting a nonlinear migration model is to divide the water drying process into two stages, and the two stages correspondingly evaporate a certain amount of water, and the temperature range of the ith stage [ T ] i1 ,T i2 ]The evaporation capacity of the internal moisture is k i The latent heat of phase change required for temperature change of 1K in this temperature range is expressed as the following formula six:
formula six: q (Q) m ＝h m k i /(T i2 -T i1 )；
K in formula six i Calculated according to the following equation seven:
formula seven: k (k) i ＝R m τ；
Moisture migration Rate R in equation seven m Can be calculated according to the following equation eight:
wherein h is m The unit is J/kg, which is the latent heat of evaporation of water; r is R m The unit is kg/s for moisture migration rate; τ is the heating time in s; r is (r) t The unit is K/s and K is the heating rate of the coal 1 Temperature range [ T ] for stage 1 i1 ,T i2 ]Evaporation of internal moisture, k 2 Temperature range [ T ] for stage 2 i1 ,T i2 ]Evaporation of internal water.
5. The method for obtaining the temperature distribution in the coking chamber for producing iron coke according to claim 1, wherein calculating the heat generated by the reduction reaction of the iron ore powder in the iron coke refining process comprises the following steps:
the iron ore powder is reduced by the precipitate X in the production process of the iron coke, and the gradual reduction reaction formula of the iron ore powder is as follows:
3Fe 2 O 3 +X＝2Fe 3 O 4 +XO；
Fe 3 O 4 +X＝3FeO+XO；
FeO+X＝Fe+XO；
and calculating the heat generated by the reduction reaction of the iron ore powder according to a step-by-step reaction formula.
6. The method for obtaining the temperature distribution in the coking chamber for producing iron coke according to claim 1, wherein the heat conduction differential equation for constructing the heat conduction in the coking chamber based on the chemical reaction heat generated in the unit time of the precipitate in the pyrolysis chemical reaction of the coal, the evaporation and absorption heat of the water in the pyrolysis chemical reaction of the coal, and the heat generated in the reduction reaction of the iron ore powder in the iron coke refining process is specifically:
for a two-dimensional unsteady heat transfer process, the heat conduction differential equation is as follows:
wherein ρ is the density of the blended coal, and the unit is kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the c is the specific heat of the blended coal, and the unit is J/(kg.K); lambda is the heat conductivity coefficient of the blended coal, and the unit is W/(m.K); s is an internal heat source with the unit of W/m 3 The internal heat source S comprises chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the blended coal, and heat generated by a reduction reaction of iron ore powder in the refining process of iron coke, wherein the heat is absorbed by evaporation of water in the pyrolysis chemical reaction of the blended coal;
the given boundary conditions are: the inside of the carbonization chamber is treated according to the constant temperature wall surface, namely:
T xc ＝T yc ＝T w0 ；
the center surface of the carbonization chamber is treated according to a symmetrical surface, namely:
7. the method for obtaining the temperature distribution in the coking chamber for ferrocoke production according to claim 1, wherein calculating the temperature distribution in the coking chamber in the coking process based on the finite difference calculation model specifically comprises: gradually calculating until the temperature of the center point of the carbonization chamber reaches T based on the finite difference calculation model end Until that point.
8. The method for obtaining a temperature distribution in a coking chamber for producing ferrocoke according to claim 7, wherein the T end The interval range is 900-1050 ℃.
9. A system for obtaining a temperature distribution in a carbonization chamber for producing ferrocoke, the system comprising: the system comprises a first heat calculation module, a second heat calculation module, a third heat calculation module, a heat transfer model construction module and a temperature distribution calculation module;
the first heat calculation module is used for calculating chemical reaction heat generated in unit time of precipitate in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process;
the second heat calculation module is used for calculating the evaporation and absorption heat of water in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process;
the third heat calculation module is used for calculating heat generated by the reduction reaction of the iron ore powder in the iron coke refining process;
the heat transfer model construction module is used for constructing a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the matched coal, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated by a reduction reaction of iron ore powder in the iron coke refining process;
the temperature distribution calculation module is used for replacing the heat conduction differential equation with a corresponding difference quotient to obtain a finite difference calculation model in algebraic form, and calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model.
10. The system for acquiring the temperature distribution in the coking chamber for producing ferrocoke according to claim 9, wherein:
the first heat calculation module is used for calculating chemical reaction heat generated in unit time of precipitate in pyrolysis chemical reaction of the matched coal in the ferrocoke refining process, and specifically comprises the following steps:
the relationship between the rate of precipitated product and temperature is obtained according to the Arrhenius equation and is expressed as the following formula I:
equation one:
describing the activation energy in the first formula according to a modified Rosin-Rammler equation to obtain the following second formula:
formula II: fi (E) =exp (- ((E-E) 0 )/ε) β )；
The chemical reaction heat generated per unit time of the precipitate calculated from the formulas one and two is expressed as the following formula three:
and (3) a formula III: q (Q) r,i ＝h r,i R r,i m i ；
Wherein delta is the percentage of the volatilized fractional product precipitated at time t, and the unit is; k is a pre-finger factor in s -1 The method comprises the steps of carrying out a first treatment on the surface of the E is activation energy, and the unit is kJ/mol; r is a gas constant, and the unit is 8.314 kJ/(mol.K); t is temperature, and the unit is K; subscript i represents the thermolytically precipitated ith product; h is a r,i The unit of the chemical reaction heat of the i-th product which is pyrolyzed out is J/kg; r is R r,i The reaction rate of the ith product which is pyrolyzed out is expressed as s -1 ；m i The mass of the i-th product which is pyrolyzed out is kg, parameter E 0 Epsilon and beta are determined by the coal dust grades;
the second heat calculation module calculates the water evaporation and absorption heat in the pyrolysis chemical reaction of the matched coal in the ferrocoke refining process, and specifically comprises the following steps:
the moisture evaporation and absorption heat is calculated by adopting a nonlinear migration model in such a way that the moisture drying process is divided into two stepsA stage, both stages evaporating a certain amount of water, the temperature range [ T ] of the ith stage i1 ,T i2 ]The evaporation capacity of the internal moisture is k i The latent heat of phase change required for temperature change of 1K in this temperature range is expressed as the following formula six:
formula six: q (Q) m ＝h m k i /(T i2 -T i1 )；
K in formula six i Calculated according to the following equation seven:
formula seven: k (k) i ＝R m τ；
Moisture migration Rate R in equation seven m Can be calculated according to the following equation eight:
wherein h is m The unit is J/kg, which is the latent heat of evaporation of water; r is R m The unit is kg/s for moisture migration rate; τ is the heating time in s; r is (r) t The unit is K/s for the temperature rising rate of coal;
the third heat calculation module calculates heat generated by the reduction reaction of the iron ore powder in the iron coke refining process, and specifically comprises the following steps:
the iron ore powder is reduced by the precipitate X in the production process of the iron coke, and the gradual reduction reaction formula of the iron ore powder is as follows:
3Fe 2 O 3 +X＝2Fe 3 O 4 +XO；
Fe 3 O 4 +X＝3FeO+XO；
FeO+X＝Fe+XO；
calculating the heat generated by the reduction reaction of the iron ore powder according to a step-by-step reaction formula;
the heat transfer model construction module constructs a heat conduction differential equation of heat transfer inside the carbonization chamber based on chemical reaction heat generated in a unit time of a precipitate in a pyrolysis chemical reaction of the matched coal, moisture evaporation absorption heat in the pyrolysis chemical reaction of the matched coal and heat generated by a reduction reaction of iron ore powder in a ferrocoke refining process, and specifically comprises the following steps:
for a two-dimensional unsteady heat transfer process, the heat conduction differential equation is as follows:
wherein ρ is the density of the blended coal, and the unit is kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the c is the specific heat of the blended coal, and the unit is J/(kg.K); lambda is the heat conductivity coefficient of the blended coal, and the unit is W/(m.K); s is an internal heat source with the unit of W/m 3 The internal heat source S comprises chemical reaction heat generated in a unit time of a precipitate in the pyrolysis chemical reaction of the blended coal, and heat generated by a reduction reaction of iron ore powder in the refining process of iron coke, wherein the heat is absorbed by evaporation of water in the pyrolysis chemical reaction of the blended coal;
the given boundary conditions are: the inside of the carbonization chamber is treated according to the constant temperature wall surface, namely:
T xc ＝T yc ＝T w0 ；
the center surface of the carbonization chamber is treated according to a symmetrical surface, namely:
the method for calculating the temperature distribution in the carbonization chamber in the ferrocoke production process based on the finite difference calculation model specifically comprises the following steps: gradually calculating until the temperature of the center point of the carbonization chamber reaches T based on the finite difference calculation model end Until that point.
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| WO2018094885A1 (en) * | 2016-11-24 | 2018-05-31 | 武汉科思瑞迪科技有限公司 | Shaft furnace process for producing iron coke |
| CN108531205A (en) * | 2018-03-02 | 2018-09-14 | 武汉科技大学 | A kind of coke production method |
| CN110241273A (en) * | 2019-04-30 | 2019-09-17 | 武汉科技大学 | A kind of iron coke and preparation method thereof using west place in Hubei iron ore and bottle coal preparation |
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| WO2018094885A1 (en) * | 2016-11-24 | 2018-05-31 | 武汉科思瑞迪科技有限公司 | Shaft furnace process for producing iron coke |
| CN108531205A (en) * | 2018-03-02 | 2018-09-14 | 武汉科技大学 | A kind of coke production method |
| CN110241273A (en) * | 2019-04-30 | 2019-09-17 | 武汉科技大学 | A kind of iron coke and preparation method thereof using west place in Hubei iron ore and bottle coal preparation |
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