ABSTRACT

The article is dedicated to the issues of heat transfer, radiant heat transfer in particular, between fluidized bed of coke and water-cooled panels arranged inside it in a staggered order. The model by A.F. Chudnovsky describing radiant heat transfer in a porous body (disperse medium) as applied to coke bed has been updated.

Keywords:

Coke Cooling, Heat Transfer Coefficient, Angular Radiation Coefficient, Pore Body Model, Water-Cooling Panel, Heat Tubes

1. Introduction

Earlier publications by the author give a description of an energy technological boiler (ETB) for cooling coke and thermal preparation of coal blend in which use is made of heat tubes (Figure 1) for cooling coke at the expense of solid heat-carrier and heat transfer from hot coke to coal blend. ETB is key unit of improved technology “combine process of coal blend thermal preparing and coke dry cooling”. This technology initially has been offered by B.I. Babanin and V.I. Babanin in 1980 and proposed heat transfer from cooling coke to warmed coal blend in drum heat changer. This technology has one defect: coke obstruction by coal dust because of heat transfer of two discrete environments by means of mix. With purpose to avoid this defect author in common with E.I. Dorman proposed to carry out heat transfer between coke and coal blend by means of heat tubes (closed two-phase thermosiphons) [1] .

2. Construction ETB and Model Description

The ETB design is described in detail in [2] , detailed investigation of heat trans-

fer [3] , both in coke cooling and in coal blend heating chambers, was generalized in [4] . ETB schematic construction has shown on Figure 1. Heat transfer in a coke cooling chamber between coke bed and water panels with heat tubes inside was studied both experimentally and theoretically, while for the case of a coal blend heating chamber, the study was only theoretical. The issue of the heat transfer level is of paramount importance, since it benchmarks ETB efficiency as a heat changer, and its dimensions, particularly in an ETB integrated with an operating coke-oven battery, which may impose restrictions on a built-in unit.

Considered in the present publication is heat transfer in the coke cooling process as a factor defining the ETB vertical dimensions. The coal blend heating chamber provides an opportunity to intensify heat exchange, in particular at the expense of counter-flow of cold (280˚C) coke-oven gas present in the flue of a coke-oven battery. This method was patented by the author in co-authorship with V.M. Ljapunov [5] . However use of the same gas in a coke cooling chamber is problematic, first, because of the impermeable solid bed used in this camera, secondly, because of potential ability of such gas being taken aside from the chamber top part to exert negative influence on the quality of coke leaving the ETB, and thirdly, due to danger of deteriorating the environment near the ETB. The presence of high CO concentration in the atmosphere in the vicinity of the USTK (Coke Dry Cooling Plant) utilizing coke-oven gas was proved.

Initial findings on coke heat transfer coefficients at its contact with water- cooled panels were made in an experiment conducted with the participation of the author in a pilot plant at the Krivorozhsky Coking Plant [6] . The heat transfer coefficient values after the experiment in [6] are shown in plots of ${\alpha }_c=f\left(t_{\text{coke}}\right)$ in Figure 2.

These results were included in the thermal design, the first variant of the ETB

technical project with a plan to utilize a flowing heat changer for heating water and generating superheated steam in a combined process. The technical project has developed by the Belgorodenergomash Company in 1993. According to this variant, heat transfer to coal blend was ensured by mixing coke and coal blend in a drum-type heat changer.

3. Research Method

The parabolic nature of experimental curves in Figure 2 testifies to the radiant component making a decisive contribution to total heat exchange. According to A.F. Chudnovsky’s model [7] of heat transfer in a porous solid, the radiant component must be proportional to $T_c^3$ :

${\lambda }_{c.\text{eff}}=2{\epsilon }^2\sigma d_{\text{eff}}{T}_c^3,$ (1)

where ${\lambda }_{c.\text{eff}}$ is effective coefficient of heat conductivity, radiant heat transfer for the most part, in a disperse medium bed;

$\epsilon$ is bed particles emissivity factor (blackness degree);

$\sigma$ is Stefan-Boltzmann constant;

$T_c$ is average coke bed absolute temperature, ˚К;

$d_{\text{eff}}$ is effective particle size;

2 = φ―is total angular radiation coefficient of a prismatic pore computed by Chudnovsky for his interlump void model presented in the form of an oblong parallelepiped.

In passing over to the outer (near-wall) row of particles in coke bed, and assuming as a hypothesis that the entire temperature gradient between coke and panel wall is accounted for by the near-wall row of particles of thickness d_eff, then Formula (1) may be rearranged as follows:

${\alpha }_{c.\text{eff}}={\lambda }_{c.\text{eff}}/d_{\text{eff}f}=2{\epsilon }^2\sigma T^3$ (2)

where ${\alpha }_{c.\text{eff}}$ is effective coefficient of coke heat transfer.

In Krivorozhsky pilot plant a coke piece (scrab) effective size was d_eff = 55 mm.

In further profound analysis of simulation environment of heat transfer in a pilot plant it was established that the ETB heat-exchange element model implemented in the pilot plant at the Krivorozhsky Coking Plant was slightly different from the designed (full-scale) heat changer in shape of the surface exposed to radiant heat flow: that of the panels with heat tubes and flowing heat changer tubes. Panel surface of full-scale heat changer makes by polished steel sheet (see section AA, Figure 1).

In the pilot plant model, the panel surface is formed of channel bars welded in row, with welding joints interrupting the heat exchange receiving surface, and so, instead of a continuous sheet (in full-scale variant) there is present a row of relatively narrow plates (see below, Figure 4). Reference-books on radiant heat exchange give essentially different values for angular radiation coefficient φ pre- sent in the radiant heat exchange formula:

${\alpha }_{c.\text{eff}}=\phi {\epsilon }_1{\epsilon }_2\sigma T_1^3$ (3)

where φ angular radiation coefficient;

${\epsilon }_1,{\epsilon }_2$ ―blackness degree of coke and steel sheet.

The results of ${\alpha }_{c.\text{eff}}$ calculations by formula (2) are shown in Figure 3 (curve 1). Curve 4 in the same figure shows the experimental values of ${\alpha }_{c.\text{eff}}$ according to studies [4] . The divergence of curves 1 and 4 at up to t = 920˚C is as large as 45% of the greatest (calculated) value of ${\alpha }_{c.\text{eff}}$ according to Formula (3), however becoming to zero at 400˚C.

Let us consider the causes of this divergence. The main cause is the following. In Formula (1) the value emissivity factor $\epsilon$ are assumed to be equal for two opposite planes of a pore, since the formula has been derived for a closed pore inside bed. However, for an open pore located at bed edge, ${\epsilon }^2$ should be substituted for the product of ${\epsilon }_1{\epsilon }_2$ , where ε₁ is coke emissivity factor, and ε₂ is panel material emissivity factor.

For polished steel sheet in the temperature range of $t=500\text{-}900˚\text{C}$ , the reference-book gives the value of ${\epsilon }_2=0.50\text{-}0.53$ , and for coke, ${\epsilon }_1=0.80\text{-}0.86$ . Thus the product of values ${\epsilon }_1{\epsilon }_2=0.43$ , instead of ${\epsilon }_1^2=0.69$ according to Chudnovsky’s canonical formula, which is 1.6 times less. Plot α_c.calc (τ) recalculated with account for this relation is shown on curve 2 (Figure 3). It is considerably closer here to the experimental values (curve 4, see Figure 3).

Let us consider further, in accordance with Chudnovsky’s model [7] , coefficient 2 in Formulas (2) and (3) as a sum of angular coefficients of radiation φ from five planes of pore, including bottom, onto the sixth plane located opposite to the bottom. For internal pore in Chudnovsky’s model, it is

$\phi =4\left({\phi }_0+4\psi \right)=4\left(0.2+4\cdot 0.075\right)=2$ (4)

where ${\phi }_0$ ―angular coefficient of radiation from bottom of pore to 6-th plane;

$\psi$ ―angular coefficient of radiation from side planes of pore to 6-th plane.

Let us consider $\phi$ as angular coefficient of radiation from bottom, with taking into account mutually disposition and sizes of two parallel planes: pore bottom (coke) and steel panel wall (Figure 4 and Figure 5). In our case of coke-to- metal heat exchange, coefficient ${\phi }_0$ should be slightly increased following the considerations below.

In consideration of our case, in passing to the outer (near-wall) row of coke particles, let us note also that the interlump pore becomes open from the side of the parallelepiped sixth plane, which is the surface of the water-cooled panel. Here small gap h may appear between coke and the panel due to coke particles scuffing on panel surface, mainly on coating sheet welding joins (see Figure 4).

Radiation from bottom of an open pore prevails among other kinds of heat exchange between coke and panel, first, due to bottom high temperature Т₁ which is approximately 100˚C - 200˚C higher than temperature Т₂ of the ridge contacting the water-cooled panel (see Figure 2, and calculations in [4] ), and secondly, due to a smaller surface exposed to other types of heat transfer (contact heat transfer-point heat transfer; convective heat transfer in the high-tem- perature part is practically absent due to small gaps).

In the reference-book [8] , for two parallel long-length plates (of a full-scale, or industrial, heat changer), there is given the value of angular radiation coefficient φ₁₂ = 0.6, while the classical work by R. Ziegel and G. Howell [9] gives the value of φ₁₂ = 0.42 for similar surfaces. We take the average value of φ_12,full-sc = 0.51.

In the pilot plant model where the flat bottom of a pore radiates upon a system of narrow metal strips interrupted with welding joints, coefficient φ₁₂ varies

for different sizes of rectangular strips from 0.2 to 0.5 [8] , i.e., on the average, φ₁₂ = 0.35. This coefficient corresponds to the physical model geometry in the pilot plant experiment. Then the full-scale/model ratio of angular radiation coefficients for bottom ${\phi }_{12\text{нат}}/{\phi }_{12\text{мод}}=0.51/0.35=1.457$ .

Coefficient φ₀ in formula (3) will be equal to ${\phi }_0=0.2\cdot 1.457=0.291$ . By substituting this value in Formula (4), we obtain the total (integral) angular radiation coefficient $\phi =4\left(0.291+4\cdot 0.075\right)=2.364$ , instead of 2.0, i.e., φ increases by 18% (assuming that the for porous surface angular radiation coefficients $\psi$ of the pore side planes remain unchanged). Proportionally with φ, heat transfer coefficient α_c.eff (average for all stages) also increases by 18%. This is the primary factor of heat transfer coefficient increase in final calculations as compared with that in publication [10] .

4. Research Outcome

The calculated radiation coefficients for model and full-scale plants, also for the resulting similarity constants heat transfer coefficients for all heat changer stages, are given in Table 1.

With new input data, emissivity factor ${К}_2={\epsilon }_1{\epsilon }_2/{\epsilon }^2=1.07$ ; and, according to the known formula, with same areas of parallel surfaces radiating upon one

another, the reduced emissivity factor is: ${\epsilon }_{п}=1/\left(1/{\epsilon }_1+1/{\epsilon }_2-1\right)=0.746$ for model and 0.784 for full-scale plant. Similarity constant ${{К}^{″}}_2={\epsilon }_{\text{full}-\text{scale}}/{\epsilon }_{\text{model}}=1.05$ , which closely approximates К₂.

The temperature factor for first stage ${К}_3={\left({Т}_{\text{full}-\text{scale}}/{Т}_{\text{mod}}\right)}^3=1.374$ (see Table 1). Thus, the value of α_c.eff included in the heat transfer equation increases 2.11 times in the heat changer first stage and 1.25 times in the second and subsequent stages, as compared with the values adopted in the industrial heat exchanger thermal design [10] . Heat balance calculations accounting for new values of heat transfer coefficients allow reduction by 1 to 2 of the number of heat transfer stages, i.e., by 2.5 to 5 meters in height, and reduction by 15% - 25% of the specific amount of metal per ETB.

Note: By fraction the maximum and minimum values are shown.

The total heat flux, as per the above outlay, is equal to

$Q=a_{c\text{eff}}F\left(T_c-T_w\right)=\phi {\epsilon }_1{\epsilon }_2\sigma T^{3}F\left(T_c-T_w\right)$ (5)

where F is effective area of coke radiating surface;

$\left(T_c-T_w\right)$ is temperature gradient between the outer (near-wall) row of coal pieces and the water-cooled panel wall.

For other designations see above.

By substituting the average values of coefficients included in Formula (5), we obtain the ETB stage 1 thermal consumption of 17.4 MW which, at steam turbine plant and turbo-generator efficiency of about 30%, converts to the ETB stage 1 electrical output of ~5.2 MW, with the aggregate stage 1 and stage 2 electrical output of about 7.2 MW. Thus the energy saving is also a feature of the given technology, that essentially increase its economic efficiency.

5. Discussion

Into conclusion, we compare our results with other author’s experimental data (Table 2).

As it can see, results of comparison with experiments by other authors are quite satisfactory.

6. Conclusions

1) Heat engineering calculations (inclusive heat balance) show that building of ETB is possible, and ETB highly effective as a heat changer. All calculations carried out using in our researching received heat transfer coefficients. There is represented comparison with Russian, Ukrainian and German author’s data about heat transfer coefficients of coke.

2) Besides coke making advantages there is profit at energy saving: attached to ETB, steam turbine plant can generate electric power about 5 - 7 MW by coke battery productivity 100 t/h.

3) Ecologic advantages of this technology are combining process of coal blend thermal preparation and coke cooling in one hermetic corpus, issued from a minimum number of overloads [3] .

*Coke dry cooling plant.

4) Economic evaluations show [3] that full compensation of capital expenditures will be expected for 5.5 years after investment begins or 3 - 5 months from plant starting on full power.

Cite this paper

Zabezhinskiy, L.D. (2017) Simulation of Radiant Heat Transfer on the Border of Coke Bed and Metal Surface of Heat Transfer Passage. Journal of Applied Mathematics and Physics, 5, 83-91. http://dx.doi.org/10.4236/jamp.2017.51009

References