a three dimensional three phase reactive flow for ... · into the channel of the blast furnace...

A three dimensional three phase reactive flow for simulating the pulverized coal injection into the channel of the blast furnace raceway

J. A. Castro, A. W. S. Baltazar & A. J. Silva

Post Graduate Program on Metallurgical Engineering-UFF

Abstract

The blast furnace process is a counter current flow reactor whose main purpose is to produce hot metal. This process uses as auxiliary fuel the injection of pulverized coal through the equipment termed the tuyere. However the injection point in the tuyere is of summary importance for the complete combustion of the pulverized coal, which in turn will affect the smooth blast furnace operation. Recently, the price of premium coals became prohibitive for using in the blast furnace, especially in Brazil, where this raw material is imported. Therefore attempts have been made to allow the use of low quality coals partially substituting the premium coals decreasing the production cost of steels. This paper deals with the simulation of the pulverized injection of low-grade coals into the channel of the blast furnace raceway. The analysis was based on a 3D three phase mathematical model, where motion, heat transfer and chemical reactions among chemical species were calculated based on transport equations. Interactions among phases were computed with the help of semi-empirical correlations. The chemical kinetics rates were adapted from the literature by adjusting the constants for representing the industrial process. The finite volume method implemented in a complex computational code written in Fortran 90 was used to solve the highly non-linear system of partial differential equations in a non-orthogonal mesh representing the geometry of a tuyere with different injection points. The comparison between model results for temperature and gas composition and experimental/industrial showed very close agreement. The mathematical model proved to be useful to predict the effect of the injection of different quality coals in the raceway and an efficient tool to evaluate new raw materials for the blast furnace Keywords: mathematical modelling, pulverized coal and multiphase flow.

© 2005 WIT Press WIT Transactions on Engineering Sciences, Vol 50, www.witpress.com, ISSN 1743-3533 (on-line)

Computational Methods in Multiphase Flow III 207

1 Introduction

Ironmaking is a major energy and raw materials consuming process in the metallurgical industry. In an integrated steel plant, the blast furnace consumes about 70% of the energy input and a major part of this energy is obtained from coal and coke. In the majority of blast furnaces coke is the main fuel. As a result of an increase in the steel production in the last years, the world prices for coke and coals that can be processed to coke have increased dramatically [3]. To reduce the use of coke and to allow the use of less noble coals as fuel in blast furnaces, the technique of pulverized coal injection - PCI - was developed. The PCI technology has achieved maturity and several blast furnaces over the world are operated with pulverized coal rates over 200 kg/thm. However, even PCI demands some especial characteristics of coals to be injected. One important characteristic is the low content of volatile substances, which are released during heating and burning. Therefore, there is a large number of coals that are not appropriated to be used in large scale in PCI. This is the case of some Brazilian coals. The combined injection of different coal types could be useful in order to increase the number and amount of coals used in PCI. To implement this technique, the physical and chemical interaction of different coals injected simultaneously in a blast furnace must be evaluated. Mathematical models are useful, reliable and represent chip tools for the analysis of industrial process, whereas trial and error strategies can lead to very high costs in the implementation of a new operational technique in a smooth operating industrial plant. A mathematical modeling of the blast furnace process is available [9] and its results show excellent agreement when compared with industrial data [5-6-9]. In the present work, the main ideas and concepts of the blast furnace model were extended to compute the chemical interactions of a three phase reactive flow comprising the blast and two kinds of coal powders injected at different sequential points in the tuyere of a blast furnace. Each coal type was modeled as a different phase, interacting chemically, thermally and mechanically with the blast and with each other. This two coal phases approach allowed to characterize the coals by different grain sizes, total carbon, thermal properties, etc.., and, very important, different volatile contents as well. All coal properties, together with the coal genesis affect strongly the coal combustion kinetics. The thermal-chemical efficiency of burning of coals along the tuyere was calculated as a function of the injection rate. The influence of oxygen enrichment was also evaluated. In this numerical experiment, two different sequential injection points were simulated. At the first one, high volatile coal was injected. At the second point, forwards in the tuyere, the low volatile coal was introduced. This combined injection scheme showed a higher efficiency for the burning of the low volatile coal, when compared with injection of low volatile coal alone. The burning of the volatile substances released by the first injected coal preheated the low volatile coal, and this was the main cause found for the increase in the thermal efficiency.


208 Computational Methods in Multiphase Flow III

2 Modelling and methodology

The mathematical model is based on differential transport equations of momentum, mass of phases and chemical species, and energy in three phases, which are assumed to co-exist in all points of a calculus domain, representing a blast furnace tuyere, where they interact mutually. All transport equations can be represented by a general form given by Equation (1).

( ) ( ) ( )( )kiki

SgraddivVdivt kikiiii

kiii,, ,,

,φφ φφερ

φερ+Γ=+

∂∂

(1) In all differential balances given by eqn (1), ρi and εi are the absolute density and volume fraction of i’th phase in the whole mixture, respectively, with i varying from 1 to 3. The intensive properties φi,k change their meaning according the type of each differential balance. In balances of momentum, the index k has no meaning and φi, is equivalent to one of components the phase velocity V i. In energy balances, φi correspond to the phase specific enthalpy, again a property of the whole phase. When mass balances are considered, φi,k represent the individual mass fractions of the k’th chemical specie, relative to the mass of the i’th phase. At the right side of eqn (1), Γi,k are diffusive or molecular transport coefficients associated to the intensive property φ. In this manner, in momentum balance equations, Γi is the phase viscosity. In energy equations, Γi represents the i’th phase thermal conductivity, and in mass balance equations, Γφi,k should be interpreted as the mass diffusion coefficient of the k’th specie in the i’th phase. In the case of phases representing particles clouds, as pulverised coals, all Γi,k are set to zero, since no molecular transport is possible, and the transport during collisions of two particles can be neglected. Sφi,k stands for a general non-homogeneous term in the differential balance equations. It can be physically interpreted as a source term of momentum, energy or mass, according the differential balance. Source (or sink) terms are useful to represent several phenomena, including mutual interactions among the phases. In momentum balances, they represent forces per unit of volume as the drag of particles by the gas stream, gravitational forces or pressure gradients

Table 1: Phase contents.

Phase description Chemical species present

Blast Gas CO, CO2, O2, H2, H2O, N2, SiO High Volatile Coal

HVC C, SiO2, high volatile content, SiC, Al2O3, MgO, CaO; CaS; FeS; FeS2

Low Volatile Coal LVC

C, SiO2, low volatile content, SiC, Al2O3, MgO, CaO; CaS; FeS; FeS2



In energy equations, source terms are used to represent the energy exchange between each two phases and the energy release or consumption due to chemical reactions. In mass balances equations, sources terms take into account the mass exchange between phases due to chemical reactions and eventual phase change phenomena like the transfer of volatile material from pulverised coal to the gas stream. Each phase has its own initial chemical composition represented by the initial values of mass fractions φi,k. After the injection, coal composition changes due to the chemical reactions taking place in the tuyere. In this work, three phases were considered: the gas phase, consisting mainly (but not only) of Nitrogen and Oxygen, and the two types of pulverised coal, characterised by their own initial composition and physical properties. The phase contents and coals composition are presented in Tables 1 and 2, respectively.

Table 2: Coal properties.

Coal types High Volatile Coal High Volatile Coal Ash 2,70 10,50 Volatiles 41,20 18,90

Immediate analysis (% dry)

carbon 56,10 70,60 Fuel rate 1,36 3,74

C 75,10 88,40 H 5,20 4,70

Element Analysis (% dry mass, ash free)

N 1,50 0,80 SiO2 50,00 43,40 AL2O3 24,80 26,90 Fe2O3 16,70 9,10 MgO 1,50 7,50

Ash (% mass as oxides)

CaO 1,80 1,30

Table 3: Combustion reactions of carbon.

(1) ( )ggPC COOC →+ )(22/1 - partial combustion

(2) ( )ggPC COOC 2)(2 →+

- full combustion

avePCR

aaR+

=1)1(

; avePC

Ra

R+

=1

1)2(

;

( )1

,

1

222

2

−

+

=

aveiTOi

ii

O

gOggave kShDA

dM

Rave ηϕωρε

ω

−=

iTa

987.112400exp2500

;

−=

avegave

17980exp7260T

RTk; 2

gave

iTTT

+=

; ii

ii d

Aϕε6

=;

−

=

−−− 1

N,O

ave

1

N,O

ave

1

N,O

aveave

22

ave

22

ave

2226

tanh6 T

i

iiT

i

iiT

i

ii

Dkd

Dkd

Dkd

ζδ

ζδ

ζδη

; 1pc =δ

; 2.0pc =ζ



Table 4: Kinetics model for Solution Loss reaction.

(3) ( )ggPC COCOC 2)(2 →+

( )1

)3(,)3(

11

22

2

−

+=

kkAMR

COfilmiCO

gCog

ηωρ

g3

CO3CO2

1)3( 10056,82

12

TPkPk

kk

ii ii−×

++= ωερ

;

−=

iTk

987,166350875,19exp

601

1

;

+−=

iTk

987,121421688,6exp2

;

−=

iTk

987,188168615,31exp3

; ii

iT

dShDkϕ

ave

222 N,COCOfilm, =

j

j MT

P jgg

ωω

ωρ310056,82 −×=

;(j=CO,CO2); ii

ii d

Aϕε6

=;

−

=

−−− 1

N,O

10

1

N,O

10

1

N,O

10

ave

22

ave

22

ave

2226

tanh6 T

i

iiT

i

iiT

i

ii

Dkd

Dkd

Dkd

iii

ζδ

ζδ

ζδ

η

; 2g

aveiTT

T+

=; 1pc =δ ;

2,0pc =ζ

Table 5: Kinetics model for Water Gas Reaction.

(4) ( ) ( ) )(22 gggPC HCOOHC +→+

( )2

2 2

1

(4), (4)

1 1g H O g

H O i film H O

RM Ak k

ρ ω

η

−

= +

( ) g3

COH5CO3CO2

4)4( 10056,82

1 i

22

TPkPkPk

kk ii

−×+++

= ερω; CO

OH2

23,10MM

k =

i

iT

dShDk ave

222 NO,HOHfilm, =;

0,55g5,1 ReShi = ;

−=

iTMM

k 1835024,14exp2

2

CO

OH3

ii

ii d

Aϕε6

=;

−=

iTMk 2632035,22exp

36001

C4

;

−=

iTk 3676059,29exp5

;

j

j MT

P jgg

ωω

ωρ310056,82 −×=

−

=

−−− 1

NO,H

10

1

NO,H

10

1

NO,H

10

ave

22

ave

22

ave

2226

tanh6 T

i

iiT

i

iiT

i

ii

Dkd

Dkd

Dkd

iii

ζδ

ζδ

ζδ

η

; 1pc =δ ;2.0pc =ζ ;

2.1 Chemical models

To simulate the evolution of chemical composition of injected coals, several chemical reactions were considered, which are summarised together with their kinetic models in Tables 3 to 7. For reaction kinetic models from literature [8]



were used. Carbon oxidation was assumed to occur in two ways. In the first one, the oxidation is partial, with generation of CO. In a second stage, CO is fully oxidised to CO2. The solution loss and water gas shift reactions were considered as taking place at temperatures around 900ºC. Coal combustion data reported by Khairil et al. [5] were use to validate the present model in the scope a Master Thesis Baltazar [8].

Table 6: Kinetics model for Water Shift reaction.

(5) ( ) ( )gg)g()g( OHCOHCO 222 +↔+

( ) ( )

−=

)(

OHco

OHCO)(PCs)( kPP

PPkfR5

5252

21013251000 ε

3

g g82,056 10;

j

j

jTP

Mωω

ρ ω−×= (5) 1 3

g

3863,7 7,32exp 3,5414 ; 93,3exp8,3146 10i

k kT T−

−= − + = ×

( ) 2 2

2

CO H(5) 1 3 CO H O 2 3

12 g

7,751 , 0; 136 exp8,3146 10

P Pk k k P P k

K Tα α −

−= + − − ≥ = ×

,;

( )(5) 2 4 (5)1k k k kα α= + − ,

2 2

2

3CO H 5

CO H O 3 312 g

7,84 100; 1,83 10 exp8,3146 10

P PP P k

K T

−−

−

×− < = × ×

;

24 3

g

4,568,83 10 exp8.,146 10

kT

−−

= × ×

Table 7: Kinetics model for volatile combustion.

(6) ( ) ( ) ( ) ( ) ( )g24g23g22g21pc NOHCOOVolatiles α+α+α→α+

αωεωρε

ε

ρ

εµ=

22

O1

MVOgMVPCpcpc

t

t4/1

tg

tg)6( M

M,minkk

6,23R

(7) ( ) ( ) ( ) ( ) ( )g28g27g6g25pc NHCOCOVolatiles α+α+α→α+

( )2

2

1/ 40.52

(7) g5

23,6 min , ; 0.03 ;0.01

g t t MV tpc pc MVPC g CO t t

g t t O

M kR k Uk k MC

µ ε ε ε ρ ω ε ω ερ α

= = =

3 Results and discussions

In order to analyze the behaviour of two different pulverized coal injected into two points within the raceway channel the time evolution of the majors distribution variables were plotted. In figure 1 the pressure field and path lines of the gas phase are shown. The pressure drop along the raceway channel is mainly due to the phase interactions with the pulverized phases. Also in Fig. 1 is observed an asymmetric pressure distribution due to the central inclined of 6 degrees of the pulverized flow injection of the two types of pulverized coals.



Z

X

Y

P: 3.50 3.51 3.52 3.53 3.54 3.55 3.56 3.57 3.58 3.59 3.60 3.70

HighVolatileCoal

LowVolatileCoal

Figure 1: Flow pattern and pressure field for the gaseous phase (time = 0.002 s).

Figure 2 shows the gas temperature pattern for a radial plane and the gas velocity vectors. As can be observed, the gas temperature is increased to around 2000 oC in the vicinity of the injection points due to the highly exothermic reactions of carbon combustion. On the other hand, just at the injection points the gas temperature decreased because of the strong heat transfer among the gas and the pulverized coals phases, which are injected at the temperature of 30 oC, while the gas is preheated to 1200 oC. Figure 3 shows the phase volume fraction of the pulverized coal injected at the first injection point. In figure 4 the temperature distribution of the pulverized coal particle is shown. The temperature of the particle developed very high temperature in the flow stream. This is a technological important parameter since the integrity of the injection device is of fundamental importance for the smooth operation. Therefore the model is an important tool to address the convenient points for the pulverized coal injection without damage of the injection device. At this point it is import to emphasise the transient behaviour of the blast furnace raceway. In the operation the injection amount and the blast rate is strongly influenced by the inner furnace permeability, which in turn, determines the furnace productivity. Therefore, the results obtained in this study were carried out for the initial condition of no injection and the transient behaviour was predited.



Z

X

Y

T: 842 972 1034 1103 1233 1364 1495 1625 1756 1922

HighVolatileCoal

LowVolatileCoal

Figure 2: Gas temperature distribution and gas vectors plot (time = 0.002 s).

Z

X

Y

fv: 1.3E-04 3.0E-04 6.0E-04 9.1E-04 1.2E-03 1.5E-03 1.8E-03 2.1E-03 2.7E-03 3.0E-03 3.6E-03

HighVolatileCoal

LowVolatileCoal

Figure 3: Phase volume fraction for pulverized coal with low volatile matter (time = 0.002 s).

4 Conclusions

A mathematical model for simulating two types of pulverized coal injection has been developed. The model is based on a three phase multi-component system



which interacts with one another exchanging momentum mass and energy. Detailed rate equations for the major chemical reactions taking place in the raceway channel were considered. The governing equations are solved based on the finite volume method for non-orthogonal structured mesh. Transient 3D results were presented for elucidate the flow pattern and temperature distribution of the 3 phases modelled. The model predictions indicted that the inner temperature of the raceway channel could reach around 2000 oC, which is observed in the actual blast furnace operation.

Z

X

Y

T: 248 358 471 694 917 1140 1217 1362 1585 1808 2031 2455

HighVolatileCoal

LowVolatileCoal

Figure 4: Gas temperature distribution within the raceway channel.

5 Symbol table

A- superficial area (m2m-3) ωj- Molar fraction of phase j D- Diffusion coefficient (m2s-1) η- efficiency factor for reaction d- Particle diameter (m) Sφ - Source terms (various) Mj – Molecular weight (kg mol-1) Sh - Sherwood number (-) P- Gas phase pressure (Pa) ϕi- Shape factor of phase i Ri- Reactions rates (mol m -3 s-1) ρ- Phase density (kg m-3)

T-temperature (K) φΓ Transfer coefficient (various)

εi- phase volume fraction(-)

Acknowledgement

(edital Universal 2003 proc: 477240-03-0).



The authors would like to thank CNPq for the financial support for this work

References

[1] Lin, S.Y., Hirato, M., Horio, M., The Characteristics of Coal Char Gasification at around Ash Melting Temperature, Energy & Fuels, 8, pp. 598-606, 1994.

[2] Zolin et al. A comparison of Coal Char Reactivity Determined from Thermogravimetric and Laminar Flow Reactor Experiments, Energy & Fuels, 12, p 268-276,1998.

[3] Castro, J.A., A Multi-dimensional Transient Mathematical Model of Blast Furnace Based on Mult-fluid model, Doctoral Thesis, Tohoku University, Institute for advanced material processing, Japan, 2000.

[4] Austin, P.R., Nogami, H., Yagi, J.I., A mathematical model for blast furnace reaction analysis based on the four fluid model, ISIJ Int., 37(8), pp. 748-755, 1997.

[5] Khairil et al. Fundamental Reaction Characteristics of Pulverized Coal at High Temperature, ISIJ Int., 41(2), pp 136-141, 2001.

[6] Baltazar, A.W.S., Modelamento Matemático e Simulação Computacional de um Ensaio de Combustão de Carvão Pulverizado. Master Thesis, EEIMVR-UFF, Volta Redonda Brazil, 2004.

[7] Castro, J. A., Nogami, H. And Yagi J.: Numerical Investigation of Simultaneous Injection of Pulverized Coal and Natural Gas with Oxygen Enrichment to the Blast Furnace, ISIJ Int., 42, pp 1203-1211, 2002.

[8] Austin, P. R., Nogami, H., And Yagi, J.: A Mathematical Model of Four Phase Motion and Heat Transfer in the Blast Furnace ISIJ Int., 37, pp 458-467, 1997.

[9] Castro, J. A., Nogami, H., And Yagi, J.: Three-dimensional Multiphase Mathematical Modeling of the Blast Furnace Based on the Multifluid Model ISIJ Int. 42, pp. 44-52, 2002.

[10] Austin, P. R, Nogami, H., And Yagi, J.: A Mathematical Model for Blast Furnace Reaction Analysis Based on the Four Fluid Model ISIJ Int., 37,pp.748-755, 1997.

[11] Perry, R. H. And Green, D.: Perry’s Chemical Engineers Handbook, 6th. Ed., McGraw-Hill, New York, Table 3-5, 1984

[12] Kagaku Kogaku Binran (5th ed.), Chemical Engineers Handbook eds. Soc. Chem. Eng of Japan, Maruzen, Tokyo, pp. 232, 1988.

[13] Castro J. A., Nogami, H., And Yagi, J.: Numerical Analysis of Multiple Injection of Pulverized Coal, Prereduced Iron Ore and Flux with Oxygen Enrichment to the Blast Furnace, ISIJ Int. 41, pp. 18-24-, 2001.



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