# A Novel Parabolic Trough Concentrating Solar Heating for Cut Tobacco Drying System

Authors: Jiang Tao Liu; Ming Li; Qiong Fen Yu; De Li Ling
Journal: International Journal of Photoenergy
 (2014)

---

## Abstract

A novel parabolic trough concentrating solar heating for cut tobacco drying system was established. The opening width effect of V type metal cavity absorber was investigated. A cut tobacco drying mathematical model calculated by fourth-order Runge-Kutta numerical solution method was used to simulate the cut tobacco drying process. And finally the orthogonal test method was used to optimize the parameters of cut tobacco drying process. The result shows that the heating rate, acquisition factor, and collector system efficiency increase with increasing the opening width of the absorber. The simulation results are in good agreement with experimental data for cut tobacco drying process. The relative errors between simulated and experimental values are less than 8%, indicating that this mathematical model is accurate for the cut tobacco airflow drying process. The optimum preparation conditions are an inlet airflow velocity of 15 m/s, an initial cut tobacco moisture content of 26%, and an inlet airflow temperature of 200°C. The thermal efficiency of the dryer and the final cut tobacco moisture content are 66.32% and 14.15%, respectively. The result shows that this parabolic trough concentrating solar heating will be one of the heat recourse candidates for cut tobacco drying system.


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## Body

## 1. Introduction

Solar energy currently represents the most abundant inexhaustible, nonpolluting, and free energy resources that could have a positive meaning in alleviating the global energy shortage and environmental pollution. There are abundant solar energy resources and good economic tobacco industry in Yunnan Province, located in the southwest of China. However, drying cut tobacco of the production process in cigarette factory needs a large amount of heat energy (150°C~300°C). If abundant solar energy resources are used for drying cut tobacco of the production process in cigarette factory, we can not only save a large amount of fossil energy but also widen the field of utilization of solar energy. In this paper, solar energy drying cut tobacco process will be investigated.However, the solar energy is intermittent in nature and that received on earth is of small flux density due to atmospheric scattering and abortion, making it necessary to use large surfaces to collect solar energy for drying cut tobacco process utilization. The major technologies used for solar energy conversion to heat are thermal processes comprising of solar collectors. There are two basic types of solar collectors, the flat-plate and the concentrating solar collectors. The flat-plate collector has advantage of absorbing both beam and diffused radiation and, therefore, still functions when beam radiation is cut off by the cloud. The area absorbing solar radiation is the same as the area intercepting solar radiation. However, flat-plate collectors are designed for applications requiring energy delivered at temperatures quite lower than 100°C, indicating that they are not suitable for drying cut tobacco process. The concentrating collector utilizes optical systems like reflectors, refractors, and so forth to increase the intensity of solar radiation incidents on energy-absorbing surfaces. It has the main advantage of generating high temperatures and may be used for drying cut tobacco process.Parabolic trough solar collector (PTC) is one type of the intermediate/high concentrating collectors, being widely used in the field of electricity generation, air-conditioning, heating, desalination, and so on. Conventional receiver used in PTC is the vacuum tube. Because of different expanding coefficients between the metallic tube and the glass tube, the cost of vacuum tube receiver is relatively high, and its useful life is short. Therefore, many researches focus on investigation of cavity absorbers. Boyd et al. [1] firstly developed a receiver that consists of an annular cylindrical tube with an aperture parallel to the axis of the cylinder. The aperture is illuminated by means of a focusing concentrator, such as a lens, and the radiation energy is scattered inside the cavity, absorbed by the walls and transmitted, as heat, to the working fluid flowing axially inside the annulus. To reduce radiative losses the tube is surrounded by a layer of a thermal insulator. Principal advantages of this design lie in exclusive use of commonly available materials and current fabrication technology. In order to minimize the heat loss, this annular cylindrical tube was improved by Barra and Franceschi [2]. Eight small cylindrical tubes were scattered inside the big cylindrical tube and used for fluid transferring. Qiaoli et al. [3] proposed the scheme of tightly connecting cluster and the inner wall of pipe. Moreover, Zhang et al. [4] established a series of absorbers with triangular, circular, hemispherical and square, and simulated the optical performance and thermal property using the software programs TracePro and Fluent. The results showed that the triangular cavity absorber structure owned the best optical performance and thermal property, which could gain collecting efficiency above 40%, under the condition of collecting temperature 150°C. Based on these above studies, a novel cavity absorber was investigated by this paper. PTC system with V type metal cavity absorber similar to triangle structure would be used for drying cut tobacco process and the thermal loss is constrained by the cavity radiation. In order to lower the absorber cost, aluminum alloy was selected as the material of absorber.Because of the coupling effect among the heat transfer, mass transfer, and energy, air drying process became complex. In order to analyze air drying cut tobacco process, simulation model was discussed. Fukuchi et al. [5] regarded the cut tobacco as equal volume sphere and simulated the motion characteristics, indicating the simulation results agreed well with the experimental results. The model equivalent sphere was established to simulate drying process of superheated steam by Pakowski et al. [6]. The result showed the moisture content of shredded tobacco simulated and the outlet temperature simulated agreed well with the experimental values. Based on these simulation results, simulation model of air drying cut tobacco process was studied and the process parameters of process of drying cut tobacco were optimized in this research.In this paper, parabolic trough concentrating system with V type metal cavity absorber was used for providing heat for cut tobacco drying system. In order to reduce the incident light energy loss and prevent cavity absorber from deformation, the width of V type metal cavity absorber was calculated, ensuring that stable heat energy provided by the PTC system is enough for cut tobacco drying process. Moreover, a mathematical model of cut tobacco drying process was calculated by using fourth-order Runge-Kutta numerical solution method and the accuracy of the model compared with the experimental results was analyzed.


## 2. Materials and Methods

### 2.1. Materials

Before solar energy drying process, the cut tobacco samples were pretreated by humidifier and equilibrated water content for 24 h in conditions of temperature20
±
2°C and relative humidity 60
±
2
%. Moisture content of cut tobacco samples was determined by YC/T31-1996 standard test methods [7].


### 2.2. Experimental Equipment

#### 2.2.1. Parabolic Trough Concentrating Solar Heating for Cut Tobacco Drying System

Diagram of parabolic trough concentrating solar heating for cut tobacco drying system was shown in Figure1(a). The main parameters of the design are given in Table 1. The parabolic trough concentrating solar heating for cut tobacco drying process was illustrated as follows. Firstly, when sunlight arrived at the parabolic trough concentrator mirror, the solar tracker was adjusted to make the metal V cavity body coincide with focal length of the PTC. Because of photothermal conversion, heat transfer oil was used to exchange heat with the cavity body and then heated to the predetermined temperature. Secondly, the circulating fan was opened and the hot air exchanged with heat transfer oil was transferred into the drying pipe. When temperature of the hot air reached target temperature in the drying pipe, cut tobacco pretreated was put into the drying pipe for drying process. Thirdly, when finishing the drying process, product of cut tobacco dried was followed with airflow into the whirlwind separator and separated from the airflow. Fourthly, part of airflow was recycled into next drying process and the left airflow was supplied by the valve S2. The electric heater was used to keep the output temperature of heat conduction oil stable when solar irradiance changed.Table 1
Main parameters of cut tobacco drying system.
Parabolic trough concentrator mirror
Reflectivity
0.9
Opening width
3.2 m
Lighting area
30 m2
Length
10 m
Metallic V cavity absorber
Opening width
4 cm, 7 cm
Internal surface coating
Aluminum anodic oxide film
Absorptivity
0.85~0.9
Emissivity
0.1~0.2
Variable diameter drying pipe
Part 1
Height: 1.2 m, diameter: 200 mm
Part 2
Height: 2 m, diameter: 300 mm
Total height
3.25 mParabolic trough concentrating solar heating for cut tobacco drying system.
(a)
Diagram of parabolic trough concentrating solar heating for cut tobacco drying system
(b)
Photograph of parabolic trough concentrating solar heating for cut tobacco drying system


#### 2.2.2. Test Schematic of Energy Flux Density Distribution

In order to analyze the effect of cavity opening width on energy flux density distribution, the test schematic was shown in Figure2. As shown in Figure 2, the width and the focal length of parabolic trough concentrator mirror were 3.2 m and 117 cm, respectively. There were a width of 10 cm Lambert target, neutral density attenuator (ND-filter), CCD industrial cameras, computers and solar tracking control system, and other parts. Test method was detailed by our previous work [8].Figure 2
The measurement schematic of focal line energy flux density distribution.


## 2.1. Materials

Before solar energy drying process, the cut tobacco samples were pretreated by humidifier and equilibrated water content for 24 h in conditions of temperature20
±
2°C and relative humidity 60
±
2
%. Moisture content of cut tobacco samples was determined by YC/T31-1996 standard test methods [7].


## 2.2. Experimental Equipment

### 2.2.1. Parabolic Trough Concentrating Solar Heating for Cut Tobacco Drying System

Diagram of parabolic trough concentrating solar heating for cut tobacco drying system was shown in Figure1(a). The main parameters of the design are given in Table 1. The parabolic trough concentrating solar heating for cut tobacco drying process was illustrated as follows. Firstly, when sunlight arrived at the parabolic trough concentrator mirror, the solar tracker was adjusted to make the metal V cavity body coincide with focal length of the PTC. Because of photothermal conversion, heat transfer oil was used to exchange heat with the cavity body and then heated to the predetermined temperature. Secondly, the circulating fan was opened and the hot air exchanged with heat transfer oil was transferred into the drying pipe. When temperature of the hot air reached target temperature in the drying pipe, cut tobacco pretreated was put into the drying pipe for drying process. Thirdly, when finishing the drying process, product of cut tobacco dried was followed with airflow into the whirlwind separator and separated from the airflow. Fourthly, part of airflow was recycled into next drying process and the left airflow was supplied by the valve S2. The electric heater was used to keep the output temperature of heat conduction oil stable when solar irradiance changed.Table 1
Main parameters of cut tobacco drying system.
Parabolic trough concentrator mirror
Reflectivity
0.9
Opening width
3.2 m
Lighting area
30 m2
Length
10 m
Metallic V cavity absorber
Opening width
4 cm, 7 cm
Internal surface coating
Aluminum anodic oxide film
Absorptivity
0.85~0.9
Emissivity
0.1~0.2
Variable diameter drying pipe
Part 1
Height: 1.2 m, diameter: 200 mm
Part 2
Height: 2 m, diameter: 300 mm
Total height
3.25 mParabolic trough concentrating solar heating for cut tobacco drying system.
(a)
Diagram of parabolic trough concentrating solar heating for cut tobacco drying system
(b)
Photograph of parabolic trough concentrating solar heating for cut tobacco drying system


### 2.2.2. Test Schematic of Energy Flux Density Distribution

In order to analyze the effect of cavity opening width on energy flux density distribution, the test schematic was shown in Figure2. As shown in Figure 2, the width and the focal length of parabolic trough concentrator mirror were 3.2 m and 117 cm, respectively. There were a width of 10 cm Lambert target, neutral density attenuator (ND-filter), CCD industrial cameras, computers and solar tracking control system, and other parts. Test method was detailed by our previous work [8].Figure 2
The measurement schematic of focal line energy flux density distribution.


## 2.2.1. Parabolic Trough Concentrating Solar Heating for Cut Tobacco Drying System

Diagram of parabolic trough concentrating solar heating for cut tobacco drying system was shown in Figure1(a). The main parameters of the design are given in Table 1. The parabolic trough concentrating solar heating for cut tobacco drying process was illustrated as follows. Firstly, when sunlight arrived at the parabolic trough concentrator mirror, the solar tracker was adjusted to make the metal V cavity body coincide with focal length of the PTC. Because of photothermal conversion, heat transfer oil was used to exchange heat with the cavity body and then heated to the predetermined temperature. Secondly, the circulating fan was opened and the hot air exchanged with heat transfer oil was transferred into the drying pipe. When temperature of the hot air reached target temperature in the drying pipe, cut tobacco pretreated was put into the drying pipe for drying process. Thirdly, when finishing the drying process, product of cut tobacco dried was followed with airflow into the whirlwind separator and separated from the airflow. Fourthly, part of airflow was recycled into next drying process and the left airflow was supplied by the valve S2. The electric heater was used to keep the output temperature of heat conduction oil stable when solar irradiance changed.Table 1
Main parameters of cut tobacco drying system.
Parabolic trough concentrator mirror
Reflectivity
0.9
Opening width
3.2 m
Lighting area
30 m2
Length
10 m
Metallic V cavity absorber
Opening width
4 cm, 7 cm
Internal surface coating
Aluminum anodic oxide film
Absorptivity
0.85~0.9
Emissivity
0.1~0.2
Variable diameter drying pipe
Part 1
Height: 1.2 m, diameter: 200 mm
Part 2
Height: 2 m, diameter: 300 mm
Total height
3.25 mParabolic trough concentrating solar heating for cut tobacco drying system.
(a)
Diagram of parabolic trough concentrating solar heating for cut tobacco drying system
(b)
Photograph of parabolic trough concentrating solar heating for cut tobacco drying system


## 2.2.2. Test Schematic of Energy Flux Density Distribution

In order to analyze the effect of cavity opening width on energy flux density distribution, the test schematic was shown in Figure2. As shown in Figure 2, the width and the focal length of parabolic trough concentrator mirror were 3.2 m and 117 cm, respectively. There were a width of 10 cm Lambert target, neutral density attenuator (ND-filter), CCD industrial cameras, computers and solar tracking control system, and other parts. Test method was detailed by our previous work [8].Figure 2
The measurement schematic of focal line energy flux density distribution.


## 3. Cut Tobacco Drying Mathematical Model

### 3.1. Assumption

In this work, a relatively simple one-dimensional model [9, 10] was adopted assuming no radial or axial dispersion of flow. The shape of cut tobacco particles was considered as equal volume sphere and had a uniform size. Diameter and density variations of cut tobacco particles were ignored in the drying process. The wall of drying pipe has good insulation and there was no heat exchange with the atmospheric environment.


### 3.2. Mathematical Model of the Drying Process

The momentum equation of cut tobacco particle was as follows:(1)
d
v
p
d
z
=
3
4
ξ
ρ
g
(
v
g
-
v
p
)
2
v
p
d
p
ρ
p
-
(
1
-
ρ
g
ρ
p
)
g
v
p
-
0.1
D
.The relationship betweenξ and Re in (1) was shown in Table 2 [11].Table 2
The relationship betweenξ and Re.
Parameter
Numerical value
Re
0-1
1–500
500–15000
ξ
24/Re
24/Re0.5
0.44The movement equation of air stream was as follows:(2)
d
v
g
d
z
=
-
d
P
ρ
g
v
g
d
z
-
g
v
g
-
3
N
ξ
(
v
g
-
v
p
)
2
4
v
g
d
p
-
λ
v
g
2
D
.The parameterN of (2) was the number of particles per unit volume in the drying pipe and identified according to the experimental conditions.The differential equations of cut tobacco particles and airflow humidity distribution were as follows:(3)
G
p
d
X
+
G
g
d
Y
=
0
(4)
G
P
d
X
+
W
d
d
A
=
0
.
The equation of dry mass transfer rate was as follows:
(5)
W
d
=
K
y
(
Y
eq
-
Y
)
.
The differential equation of cut tobacco particles humidity was as follows:
(6)
d
X
d
z
=
-
6
K
y
(
Y
eq
-
Y
)
(
1
+
X
)
ρ
p
d
p
v
p
.The mass transfer coefficientK
y, the Schmidt number Sc, and the Prandtl number Pr in (6) were associated and calculated according to the correlation proposed by literature [12]:
(7)
h
K
y
=
C
g
(
1
+
Y
)
(
Sc
Pr
)
0.56
Pr
=
(
C
g
ν
g
ρ
g
)
λ
g
,
Sc
=
ν
g
D
v
a
.Combining (3) and (6), the differential equation of airflow and humidity could be obtained as
(8)
d
Y
d
z
=
-
6
G
p
K
y
(
Y
eq
-
Y
)
(
1
+
X
)
G
g
ρ
p
d
p
v
p
.The heat balance equation of cut tobacco particles was(9)
d
t
p
d
z
=
-
C
w
t
p
C
s
+
C
w
X
d
X
d
z
+
6
(
1
+
X
)
[
h
(
t
g
-
t
p
)
-
K
y
(
Y
eq
-
Y
)
(
r
0
+
C
w
t
p
)
]
ρ
p
v
p
d
p
(
C
s
+
C
w
X
)
.The convective heat transfer coefficienth between the air stream and cut tobacco particles in (9) was associated with Russell number Nu and also calculated by literature [12].The equation of gas heat balance was as follows:(10)
d
t
g
d
z
=
-
r
0
C
g
d
Y
d
z
-
6
G
p
(
1
+
X
)
[
h
(
t
g
-
t
p
)
-
K
y
(
Y
eq
-
Y
)
(
r
0
+
C
w
t
p
)
]
G
g
v
p
d
p
C
g
.The differential equation of pipe diameter was as follows:(11)
d
D
d
z
=
2
cot
θ
.There,θ was the expansion angle of the adjustable pipe.According to the equations from (1) to (2) and (6) to (11), the tapered tubular air drying cut tobacco mathematical model was formed. Then this mathematical model was calculated using fourth-order Runge-Kutta method and Matlab software program.


## 3.1. Assumption

In this work, a relatively simple one-dimensional model [9, 10] was adopted assuming no radial or axial dispersion of flow. The shape of cut tobacco particles was considered as equal volume sphere and had a uniform size. Diameter and density variations of cut tobacco particles were ignored in the drying process. The wall of drying pipe has good insulation and there was no heat exchange with the atmospheric environment.


## 3.2. Mathematical Model of the Drying Process

The momentum equation of cut tobacco particle was as follows:(1)
d
v
p
d
z
=
3
4
ξ
ρ
g
(
v
g
-
v
p
)
2
v
p
d
p
ρ
p
-
(
1
-
ρ
g
ρ
p
)
g
v
p
-
0.1
D
.The relationship betweenξ and Re in (1) was shown in Table 2 [11].Table 2
The relationship betweenξ and Re.
Parameter
Numerical value
Re
0-1
1–500
500–15000
ξ
24/Re
24/Re0.5
0.44The movement equation of air stream was as follows:(2)
d
v
g
d
z
=
-
d
P
ρ
g
v
g
d
z
-
g
v
g
-
3
N
ξ
(
v
g
-
v
p
)
2
4
v
g
d
p
-
λ
v
g
2
D
.The parameterN of (2) was the number of particles per unit volume in the drying pipe and identified according to the experimental conditions.The differential equations of cut tobacco particles and airflow humidity distribution were as follows:(3)
G
p
d
X
+
G
g
d
Y
=
0
(4)
G
P
d
X
+
W
d
d
A
=
0
.
The equation of dry mass transfer rate was as follows:
(5)
W
d
=
K
y
(
Y
eq
-
Y
)
.
The differential equation of cut tobacco particles humidity was as follows:
(6)
d
X
d
z
=
-
6
K
y
(
Y
eq
-
Y
)
(
1
+
X
)
ρ
p
d
p
v
p
.The mass transfer coefficientK
y, the Schmidt number Sc, and the Prandtl number Pr in (6) were associated and calculated according to the correlation proposed by literature [12]:
(7)
h
K
y
=
C
g
(
1
+
Y
)
(
Sc
Pr
)
0.56
Pr
=
(
C
g
ν
g
ρ
g
)
λ
g
,
Sc
=
ν
g
D
v
a
.Combining (3) and (6), the differential equation of airflow and humidity could be obtained as
(8)
d
Y
d
z
=
-
6
G
p
K
y
(
Y
eq
-
Y
)
(
1
+
X
)
G
g
ρ
p
d
p
v
p
.The heat balance equation of cut tobacco particles was(9)
d
t
p
d
z
=
-
C
w
t
p
C
s
+
C
w
X
d
X
d
z
+
6
(
1
+
X
)
[
h
(
t
g
-
t
p
)
-
K
y
(
Y
eq
-
Y
)
(
r
0
+
C
w
t
p
)
]
ρ
p
v
p
d
p
(
C
s
+
C
w
X
)
.The convective heat transfer coefficienth between the air stream and cut tobacco particles in (9) was associated with Russell number Nu and also calculated by literature [12].The equation of gas heat balance was as follows:(10)
d
t
g
d
z
=
-
r
0
C
g
d
Y
d
z
-
6
G
p
(
1
+
X
)
[
h
(
t
g
-
t
p
)
-
K
y
(
Y
eq
-
Y
)
(
r
0
+
C
w
t
p
)
]
G
g
v
p
d
p
C
g
.The differential equation of pipe diameter was as follows:(11)
d
D
d
z
=
2
cot
θ
.There,θ was the expansion angle of the adjustable pipe.According to the equations from (1) to (2) and (6) to (11), the tapered tubular air drying cut tobacco mathematical model was formed. Then this mathematical model was calculated using fourth-order Runge-Kutta method and Matlab software program.


## 4. Results and Discussion

### 4.1. The heating Experiments of Parabolic Trough Concentrating System

Experiments were studied to analyze the effect of cavity opening width on collector temperatures as shown in Figure3.Effect of cavity opening width on collector temperature (experimental conditions: mass of heat conduction oil = 42.65 kg and flow rate = 0.15 kg/s).
(a)
7 cm
(b)
4 cmAs can be seen from Figure3, when the solar irradiation intensity is low, the cavity with opening width of 7 cm has faster heating rate because the cavity with opening width of 4 cm has relatively larger heat loss. When the run time increases to about 1 month, the cavity opening width of 4 cm has larger deformation. As for the cavity with opening width of 7 cm, it was almost not deformed except in enclosure seams of insulated enclosure. These changes before and after heating about the cavity shape are shown in Figure 4.The changes about the cavity shape before and after heating.
(a)
4 cm
(b)
7 cmIn order to analyze the effect of cavity opening width on energy flux density distribution, the test results were shown in Figure5. During test process, the direct solar radiation during measurement was 568 W/m2. As can be seen from Figure 5, the 95% of energy is concentrated in the focal line of concentration at the 0–7.5 cm. When the cavity absorber with opening width of 4 cm is used, there is part of the energy outside the cavity focused on the insulation enclosure. This may be because the insulation housing material and the absorber material were different. The cavity absorber with opening width of 4 cm has severe deformation when it is stressed. The cavity absorber with opening width of 7 cm can absorb most of the energy. The insulation enclosure absorbs less energy and only causes deformation of shell commissure.Figure 5
The test results of focal line energy flux density distribution.When the impact of tracking accuracy is ignored, the optical efficiency of this collector system is equal to the product of mirror reflectivity, acquisition factor, and the cavity absorptivity. The acquisition factors of the cavity absorber with the opening width of 4 cm and 7 cm are 0.81 and 0.96, respectively. The collector system efficiency is calculated using the following formula:(12)
η
sys
=
m
C
oil
(
t
out
-
t
in
)
A
a
H
b
.When the heat conduction oil temperature is 230°C, the collector system efficiency of the cavity absorber with the opening width of 4 cm and 7 cm is 10.9% and 25.2%, respectively. The result shows that the heating rate, acquisition factor, and collector system efficiency increase with increasing the opening width of the absorber and can also prevent the cavity from deformation. It naturally follows that stability of heat conduction oil output temperature can be improved.


### 4.2. Design and Construction of the Variable Diameter Drying Pipe

#### 4.2.1. Approximation of Variable Diameter Drying Pipe

This paper uses the Fedorov method on the drying tube diameter and height of approximate calculation.The numberK
i is calculated by the following equation:
(13)
K
i
=
d
p
×
4
g
(
ρ
p
-
ρ
g
)
3
μ
g
2
ρ
g
.
3Through the Figure6 found the relationship between R
e
p and K
i and through the Figure 7 found the relationship between R
e
p and Nu, the heat transfer coefficient of K between air and material particles is as follows:
(14)
K
=
Nu
·
λ
g
d
p
.
Suspension velocity of particles is as follows:
(15)
υ
a
=
R
e
p
μ
g
d
p
.
The total surface area of the particle is as follows:
(16)
A
s
=
6
G
p
d
p
ρ
p
.
The mean temperature difference between the material and the air is
(17)
Δ
t
=
t
1
+
t
2
2
-
t
s
.
The time of the drying process is
(18)
τ
=
Q
K
A
s
Δ
t
.
The length z of the drying pipe is as follows:
(19)
z
=
(
v
g
-
v
a
)
τ
.
The diameter D of the drying pipe is
(20)
D
=
4
G
g
ρ
s
3600
π
υ
g
.Figure 6
The relationship betweenR
e
p and K
i.Figure 7
The relationship betweenR
e
p and Nu.The design parameters are substituted into the above formula of cut tobacco drying. The parameters are shown in Table3.Table 3
The design parameters of cut tobacco drying.
Parameters
Density(kg/m3)
Specific heat(kJ/kg·°C)
Initial velocity(m/s)
Initial moisturecontent (kg/kg)
Initial temperature(°C)
The water contentafter drying (kg/kg)
Diameter(m)
Cut tobacco
800
1.467
0
0.25
20
0.115~0.14
1.2
×
10
-
3
Air
0.75
1.025
15
0.025
190
—
—


#### 4.2.2. The Simulation Speed Flow of Variable Diameter Drying Pipe

Reducing type dry pipe consists of two different diameters of straight pipe and an expansion pipe connection. In the actual environment, the improper value ofθ will lead to sediment in the drying pipe on drying process. According to the actual model using ANSYS Fluent for the fluid flow model the sediment will make the flow channel blockage and have a great influence on the drying effect even an accident.Figure8 shows the entrance of hot air temperature is 200°C, velocity of 15 m/s; the variable angle θ is 50
° and 5
2
°, respectively. We get the velocity of flow field in variable diameter drying pipe through ANSYS Fluent.The velocity of flow field in variable diameter drying pipe.
(a)
θ
=
5
0
°
(b)
θ
=
5
2
°Figure8 shows that, when the θ is 5
0
°, there is reflux area in variable diameter of variable diameter drying pipe. The reflux area will make sediment in the drying pipe on drying process. When the θ is 5
2
°, there is no reflux area in variable diameter drying pipe. In practical design, the height and heat loss of variable diameter drying pipe are considered; the variable angle θ of 60° can well meet the requirements of cut tobacco drying process.


#### 4.2.3. Production of the Variable Diameter Drying Pipe

According to the above calculation and analysis, the variable diameter drying pipe is designed and is made of stainless steel 304 with the thickness of 2 mm. It is fixed through the bracket to ensure the drying tube vertically. The parameters of the drying pipe and the photo are shown in Figure9.The diagram of variable diameter drying pipe.
(a)
The parameters of the drying pipe
(b)
The photo of variable diameter drying pipe


### 4.3. Cut Tobacco Drying Process

#### 4.3.1. Simulation of Cut Tobacco Drying Process

The distribution simulation of airflow and cut tobacco parameters is shown in Table4. The velocities shown in Figure 10 vary with the height of drying process. In the accelerating section (range from 0 m to 1.2 m), the airflow velocity decreases slightly and that of cut tobacco increases quickly with increasing the height of drying pipe. In the transition section (from 1.2 m to 1.25 m), the airflow velocity decreases sharply and that of cut tobacco increases slowly with increasing the height of drying pipe. But in the constant section (from 1.25 m to 3.25 m), the velocities of the airflow and the cut tobacco decrease gradually with the height increasing.Table 4
Parameters of cut tobacco drying (cut tobacco).
Intensity/kg·m−3
Specific heat/J·(kg·°C)−1
Initial moisture content/%
Diameter/m
Solids-gas ratio
Airflow temperature/°C
Airflow speed/ms−1
Initial  temperature /°C
255
1467
25.05
1.2×10-3
0.1
200
15
20Distribution simulation of airflow and cut tobacco parameters (simulation experimental conditions: inlet air temperature = 200°C, flow rate = 15 m/s, and initial moisture content of cut tobacco = 25%).
(a)
(b)As shown in Figure10(b), the temperature of air flow decreases with the increases of drying pipe height. The temperature of cut tobacco increases rapidly in the accelerating section and then increases slowly with the increases of drying pipe height. This is the cut tobacco is put into the drying pipe and separated quickly by high-speed airflow. Then the contact area between the airflow and the cut tobacco is increased, indicating that both heat and mass transfer rates are improved. In the accelerating section, because the relative speed of cut tobacco particles is large, both heat transfer areas for gas phase together with solid phase and the volumetric heat transfer coefficient are improved. It naturally follows that cut tobacco temperature increases rapidly in the accelerating section. But in the constant section, the relative speed of airflow and cut tobacco particles basically keeps unchanged, so the speed of cut tobacco particles no longer increases and the time of cut tobacco in drying pipe is prolonged.


#### 4.3.2. Validation of Mathematical Model

The mathematical model of the cut tobacco particles drying process was calculated using fourth-order Runge-Kutta numerical solution method. Experimental conditions [12] and the results of both simulation and experiment are shown in Table 5 and Figures 11, 12, and 13, respectively.Table 5
Summaries of experimental conditions.
Run number
t
g
in
v
g
in
v
g
out
t
p
out
X
in
X
out
A1
199.5
15
163.4
53.2
24.03
12.37
B1
199.8
15
156.9
58.7
26.02
14.15
C1
200.4
15
157.7
59.3
25.05
13.39
C1′
200.4
20
152.6
61.2
25.05
11.23
C2
190.3
15
148.5
52.8
25.05
14.33Figure 11
Final cut tobacco moisture contents of simulation and experiment results.Figure 12
Final cut tobacco temperatures of simulation and experiment results.Figure 13
Final airflow temperatures of simulation and experiment results.Figures11, 12, and 13 show the final cut tobacco moisture contents, temperatures, and the final airflow temperatures along with the simulation results for the same. It can be seen from it that the simulation results are in good agreement with experimental data for cut tobacco drying process. The relative errors between simulated and experimental values are less than 8%, indicating that this mathematical model is accurate for the cut tobacco airflow drying process.


### 4.4. Optimization Parameters of Cut Tobacco Drying Process

The effects of initial cut tobacco moisture content, inlet airflow velocity, and temperature on cut tobacco drying process are studied by the orthogonal experiment in three factors and three levels. Criteria for determining the optimum parameter conditions are the final cut tobacco moisture content and thermal efficiency of the dryer. The optimization results are shown in Table6.Table 6
Result of orthogonal experiment.
Run number
v
g
in (m/s)
X
in (%)
t
g
in (°C)
η (%)
1
15
24
180
62.46
2
15
25
190
63.54
3
15
26
200
66.32
4
18
24
190
59.46
5
18
25
200
61.34
6
18
26
180
60.64
7
20
24
200
54.56
8
20
25
180
52.35
9
20
26
190
57.49
K1
64.107
58.827
58.483
—
K2
60.480
59.077
60.163
—
K3
54.800
61.483
60.740
—
Range
9.307
2.656
2.257
—According to the orthogonal test result, it can be seen that the thermal efficiency increases with increasing the airflow temperature and the inlet cut tobacco moisture content but decreases with the decrease of airflow velocity. The result shows the optimum preparation conditions are an inlet airflow velocity of 15 m/s, an initial cut tobacco moisture content of 26%, and an inlet airflow temperature of 200°C. The thermal efficiency of the dryer and the final cut tobacco moisture content are 66.32% and 14.15%, respectively. The final cut tobacco moisture content meets the requirements of cut tobacco drying process. The result shows that this parabolic trough concentrating solar heating will be a potential heat recourse for cut tobacco drying system.


## 4.1. The heating Experiments of Parabolic Trough Concentrating System

Experiments were studied to analyze the effect of cavity opening width on collector temperatures as shown in Figure3.Effect of cavity opening width on collector temperature (experimental conditions: mass of heat conduction oil = 42.65 kg and flow rate = 0.15 kg/s).
(a)
7 cm
(b)
4 cmAs can be seen from Figure3, when the solar irradiation intensity is low, the cavity with opening width of 7 cm has faster heating rate because the cavity with opening width of 4 cm has relatively larger heat loss. When the run time increases to about 1 month, the cavity opening width of 4 cm has larger deformation. As for the cavity with opening width of 7 cm, it was almost not deformed except in enclosure seams of insulated enclosure. These changes before and after heating about the cavity shape are shown in Figure 4.The changes about the cavity shape before and after heating.
(a)
4 cm
(b)
7 cmIn order to analyze the effect of cavity opening width on energy flux density distribution, the test results were shown in Figure5. During test process, the direct solar radiation during measurement was 568 W/m2. As can be seen from Figure 5, the 95% of energy is concentrated in the focal line of concentration at the 0–7.5 cm. When the cavity absorber with opening width of 4 cm is used, there is part of the energy outside the cavity focused on the insulation enclosure. This may be because the insulation housing material and the absorber material were different. The cavity absorber with opening width of 4 cm has severe deformation when it is stressed. The cavity absorber with opening width of 7 cm can absorb most of the energy. The insulation enclosure absorbs less energy and only causes deformation of shell commissure.Figure 5
The test results of focal line energy flux density distribution.When the impact of tracking accuracy is ignored, the optical efficiency of this collector system is equal to the product of mirror reflectivity, acquisition factor, and the cavity absorptivity. The acquisition factors of the cavity absorber with the opening width of 4 cm and 7 cm are 0.81 and 0.96, respectively. The collector system efficiency is calculated using the following formula:(12)
η
sys
=
m
C
oil
(
t
out
-
t
in
)
A
a
H
b
.When the heat conduction oil temperature is 230°C, the collector system efficiency of the cavity absorber with the opening width of 4 cm and 7 cm is 10.9% and 25.2%, respectively. The result shows that the heating rate, acquisition factor, and collector system efficiency increase with increasing the opening width of the absorber and can also prevent the cavity from deformation. It naturally follows that stability of heat conduction oil output temperature can be improved.


## 4.2. Design and Construction of the Variable Diameter Drying Pipe

### 4.2.1. Approximation of Variable Diameter Drying Pipe

This paper uses the Fedorov method on the drying tube diameter and height of approximate calculation.The numberK
i is calculated by the following equation:
(13)
K
i
=
d
p
×
4
g
(
ρ
p
-
ρ
g
)
3
μ
g
2
ρ
g
.
3Through the Figure6 found the relationship between R
e
p and K
i and through the Figure 7 found the relationship between R
e
p and Nu, the heat transfer coefficient of K between air and material particles is as follows:
(14)
K
=
Nu
·
λ
g
d
p
.
Suspension velocity of particles is as follows:
(15)
υ
a
=
R
e
p
μ
g
d
p
.
The total surface area of the particle is as follows:
(16)
A
s
=
6
G
p
d
p
ρ
p
.
The mean temperature difference between the material and the air is
(17)
Δ
t
=
t
1
+
t
2
2
-
t
s
.
The time of the drying process is
(18)
τ
=
Q
K
A
s
Δ
t
.
The length z of the drying pipe is as follows:
(19)
z
=
(
v
g
-
v
a
)
τ
.
The diameter D of the drying pipe is
(20)
D
=
4
G
g
ρ
s
3600
π
υ
g
.Figure 6
The relationship betweenR
e
p and K
i.Figure 7
The relationship betweenR
e
p and Nu.The design parameters are substituted into the above formula of cut tobacco drying. The parameters are shown in Table3.Table 3
The design parameters of cut tobacco drying.
Parameters
Density(kg/m3)
Specific heat(kJ/kg·°C)
Initial velocity(m/s)
Initial moisturecontent (kg/kg)
Initial temperature(°C)
The water contentafter drying (kg/kg)
Diameter(m)
Cut tobacco
800
1.467
0
0.25
20
0.115~0.14
1.2
×
10
-
3
Air
0.75
1.025
15
0.025
190
—
—


### 4.2.2. The Simulation Speed Flow of Variable Diameter Drying Pipe

Reducing type dry pipe consists of two different diameters of straight pipe and an expansion pipe connection. In the actual environment, the improper value ofθ will lead to sediment in the drying pipe on drying process. According to the actual model using ANSYS Fluent for the fluid flow model the sediment will make the flow channel blockage and have a great influence on the drying effect even an accident.Figure8 shows the entrance of hot air temperature is 200°C, velocity of 15 m/s; the variable angle θ is 50
° and 5
2
°, respectively. We get the velocity of flow field in variable diameter drying pipe through ANSYS Fluent.The velocity of flow field in variable diameter drying pipe.
(a)
θ
=
5
0
°
(b)
θ
=
5
2
°Figure8 shows that, when the θ is 5
0
°, there is reflux area in variable diameter of variable diameter drying pipe. The reflux area will make sediment in the drying pipe on drying process. When the θ is 5
2
°, there is no reflux area in variable diameter drying pipe. In practical design, the height and heat loss of variable diameter drying pipe are considered; the variable angle θ of 60° can well meet the requirements of cut tobacco drying process.


### 4.2.3. Production of the Variable Diameter Drying Pipe

According to the above calculation and analysis, the variable diameter drying pipe is designed and is made of stainless steel 304 with the thickness of 2 mm. It is fixed through the bracket to ensure the drying tube vertically. The parameters of the drying pipe and the photo are shown in Figure9.The diagram of variable diameter drying pipe.
(a)
The parameters of the drying pipe
(b)
The photo of variable diameter drying pipe


## 4.2.1. Approximation of Variable Diameter Drying Pipe

This paper uses the Fedorov method on the drying tube diameter and height of approximate calculation.The numberK
i is calculated by the following equation:
(13)
K
i
=
d
p
×
4
g
(
ρ
p
-
ρ
g
)
3
μ
g
2
ρ
g
.
3Through the Figure6 found the relationship between R
e
p and K
i and through the Figure 7 found the relationship between R
e
p and Nu, the heat transfer coefficient of K between air and material particles is as follows:
(14)
K
=
Nu
·
λ
g
d
p
.
Suspension velocity of particles is as follows:
(15)
υ
a
=
R
e
p
μ
g
d
p
.
The total surface area of the particle is as follows:
(16)
A
s
=
6
G
p
d
p
ρ
p
.
The mean temperature difference between the material and the air is
(17)
Δ
t
=
t
1
+
t
2
2
-
t
s
.
The time of the drying process is
(18)
τ
=
Q
K
A
s
Δ
t
.
The length z of the drying pipe is as follows:
(19)
z
=
(
v
g
-
v
a
)
τ
.
The diameter D of the drying pipe is
(20)
D
=
4
G
g
ρ
s
3600
π
υ
g
.Figure 6
The relationship betweenR
e
p and K
i.Figure 7
The relationship betweenR
e
p and Nu.The design parameters are substituted into the above formula of cut tobacco drying. The parameters are shown in Table3.Table 3
The design parameters of cut tobacco drying.
Parameters
Density(kg/m3)
Specific heat(kJ/kg·°C)
Initial velocity(m/s)
Initial moisturecontent (kg/kg)
Initial temperature(°C)
The water contentafter drying (kg/kg)
Diameter(m)
Cut tobacco
800
1.467
0
0.25
20
0.115~0.14
1.2
×
10
-
3
Air
0.75
1.025
15
0.025
190
—
—


## 4.2.2. The Simulation Speed Flow of Variable Diameter Drying Pipe

Reducing type dry pipe consists of two different diameters of straight pipe and an expansion pipe connection. In the actual environment, the improper value ofθ will lead to sediment in the drying pipe on drying process. According to the actual model using ANSYS Fluent for the fluid flow model the sediment will make the flow channel blockage and have a great influence on the drying effect even an accident.Figure8 shows the entrance of hot air temperature is 200°C, velocity of 15 m/s; the variable angle θ is 50
° and 5
2
°, respectively. We get the velocity of flow field in variable diameter drying pipe through ANSYS Fluent.The velocity of flow field in variable diameter drying pipe.
(a)
θ
=
5
0
°
(b)
θ
=
5
2
°Figure8 shows that, when the θ is 5
0
°, there is reflux area in variable diameter of variable diameter drying pipe. The reflux area will make sediment in the drying pipe on drying process. When the θ is 5
2
°, there is no reflux area in variable diameter drying pipe. In practical design, the height and heat loss of variable diameter drying pipe are considered; the variable angle θ of 60° can well meet the requirements of cut tobacco drying process.


## 4.2.3. Production of the Variable Diameter Drying Pipe

According to the above calculation and analysis, the variable diameter drying pipe is designed and is made of stainless steel 304 with the thickness of 2 mm. It is fixed through the bracket to ensure the drying tube vertically. The parameters of the drying pipe and the photo are shown in Figure9.The diagram of variable diameter drying pipe.
(a)
The parameters of the drying pipe
(b)
The photo of variable diameter drying pipe


## 4.3. Cut Tobacco Drying Process

### 4.3.1. Simulation of Cut Tobacco Drying Process

The distribution simulation of airflow and cut tobacco parameters is shown in Table4. The velocities shown in Figure 10 vary with the height of drying process. In the accelerating section (range from 0 m to 1.2 m), the airflow velocity decreases slightly and that of cut tobacco increases quickly with increasing the height of drying pipe. In the transition section (from 1.2 m to 1.25 m), the airflow velocity decreases sharply and that of cut tobacco increases slowly with increasing the height of drying pipe. But in the constant section (from 1.25 m to 3.25 m), the velocities of the airflow and the cut tobacco decrease gradually with the height increasing.Table 4
Parameters of cut tobacco drying (cut tobacco).
Intensity/kg·m−3
Specific heat/J·(kg·°C)−1
Initial moisture content/%
Diameter/m
Solids-gas ratio
Airflow temperature/°C
Airflow speed/ms−1
Initial  temperature /°C
255
1467
25.05
1.2×10-3
0.1
200
15
20Distribution simulation of airflow and cut tobacco parameters (simulation experimental conditions: inlet air temperature = 200°C, flow rate = 15 m/s, and initial moisture content of cut tobacco = 25%).
(a)
(b)As shown in Figure10(b), the temperature of air flow decreases with the increases of drying pipe height. The temperature of cut tobacco increases rapidly in the accelerating section and then increases slowly with the increases of drying pipe height. This is the cut tobacco is put into the drying pipe and separated quickly by high-speed airflow. Then the contact area between the airflow and the cut tobacco is increased, indicating that both heat and mass transfer rates are improved. In the accelerating section, because the relative speed of cut tobacco particles is large, both heat transfer areas for gas phase together with solid phase and the volumetric heat transfer coefficient are improved. It naturally follows that cut tobacco temperature increases rapidly in the accelerating section. But in the constant section, the relative speed of airflow and cut tobacco particles basically keeps unchanged, so the speed of cut tobacco particles no longer increases and the time of cut tobacco in drying pipe is prolonged.


### 4.3.2. Validation of Mathematical Model

The mathematical model of the cut tobacco particles drying process was calculated using fourth-order Runge-Kutta numerical solution method. Experimental conditions [12] and the results of both simulation and experiment are shown in Table 5 and Figures 11, 12, and 13, respectively.Table 5
Summaries of experimental conditions.
Run number
t
g
in
v
g
in
v
g
out
t
p
out
X
in
X
out
A1
199.5
15
163.4
53.2
24.03
12.37
B1
199.8
15
156.9
58.7
26.02
14.15
C1
200.4
15
157.7
59.3
25.05
13.39
C1′
200.4
20
152.6
61.2
25.05
11.23
C2
190.3
15
148.5
52.8
25.05
14.33Figure 11
Final cut tobacco moisture contents of simulation and experiment results.Figure 12
Final cut tobacco temperatures of simulation and experiment results.Figure 13
Final airflow temperatures of simulation and experiment results.Figures11, 12, and 13 show the final cut tobacco moisture contents, temperatures, and the final airflow temperatures along with the simulation results for the same. It can be seen from it that the simulation results are in good agreement with experimental data for cut tobacco drying process. The relative errors between simulated and experimental values are less than 8%, indicating that this mathematical model is accurate for the cut tobacco airflow drying process.


## 4.3.1. Simulation of Cut Tobacco Drying Process

The distribution simulation of airflow and cut tobacco parameters is shown in Table4. The velocities shown in Figure 10 vary with the height of drying process. In the accelerating section (range from 0 m to 1.2 m), the airflow velocity decreases slightly and that of cut tobacco increases quickly with increasing the height of drying pipe. In the transition section (from 1.2 m to 1.25 m), the airflow velocity decreases sharply and that of cut tobacco increases slowly with increasing the height of drying pipe. But in the constant section (from 1.25 m to 3.25 m), the velocities of the airflow and the cut tobacco decrease gradually with the height increasing.Table 4
Parameters of cut tobacco drying (cut tobacco).
Intensity/kg·m−3
Specific heat/J·(kg·°C)−1
Initial moisture content/%
Diameter/m
Solids-gas ratio
Airflow temperature/°C
Airflow speed/ms−1
Initial  temperature /°C
255
1467
25.05
1.2×10-3
0.1
200
15
20Distribution simulation of airflow and cut tobacco parameters (simulation experimental conditions: inlet air temperature = 200°C, flow rate = 15 m/s, and initial moisture content of cut tobacco = 25%).
(a)
(b)As shown in Figure10(b), the temperature of air flow decreases with the increases of drying pipe height. The temperature of cut tobacco increases rapidly in the accelerating section and then increases slowly with the increases of drying pipe height. This is the cut tobacco is put into the drying pipe and separated quickly by high-speed airflow. Then the contact area between the airflow and the cut tobacco is increased, indicating that both heat and mass transfer rates are improved. In the accelerating section, because the relative speed of cut tobacco particles is large, both heat transfer areas for gas phase together with solid phase and the volumetric heat transfer coefficient are improved. It naturally follows that cut tobacco temperature increases rapidly in the accelerating section. But in the constant section, the relative speed of airflow and cut tobacco particles basically keeps unchanged, so the speed of cut tobacco particles no longer increases and the time of cut tobacco in drying pipe is prolonged.


## 4.3.2. Validation of Mathematical Model

The mathematical model of the cut tobacco particles drying process was calculated using fourth-order Runge-Kutta numerical solution method. Experimental conditions [12] and the results of both simulation and experiment are shown in Table 5 and Figures 11, 12, and 13, respectively.Table 5
Summaries of experimental conditions.
Run number
t
g
in
v
g
in
v
g
out
t
p
out
X
in
X
out
A1
199.5
15
163.4
53.2
24.03
12.37
B1
199.8
15
156.9
58.7
26.02
14.15
C1
200.4
15
157.7
59.3
25.05
13.39
C1′
200.4
20
152.6
61.2
25.05
11.23
C2
190.3
15
148.5
52.8
25.05
14.33Figure 11
Final cut tobacco moisture contents of simulation and experiment results.Figure 12
Final cut tobacco temperatures of simulation and experiment results.Figure 13
Final airflow temperatures of simulation and experiment results.Figures11, 12, and 13 show the final cut tobacco moisture contents, temperatures, and the final airflow temperatures along with the simulation results for the same. It can be seen from it that the simulation results are in good agreement with experimental data for cut tobacco drying process. The relative errors between simulated and experimental values are less than 8%, indicating that this mathematical model is accurate for the cut tobacco airflow drying process.


## 4.4. Optimization Parameters of Cut Tobacco Drying Process

The effects of initial cut tobacco moisture content, inlet airflow velocity, and temperature on cut tobacco drying process are studied by the orthogonal experiment in three factors and three levels. Criteria for determining the optimum parameter conditions are the final cut tobacco moisture content and thermal efficiency of the dryer. The optimization results are shown in Table6.Table 6
Result of orthogonal experiment.
Run number
v
g
in (m/s)
X
in (%)
t
g
in (°C)
η (%)
1
15
24
180
62.46
2
15
25
190
63.54
3
15
26
200
66.32
4
18
24
190
59.46
5
18
25
200
61.34
6
18
26
180
60.64
7
20
24
200
54.56
8
20
25
180
52.35
9
20
26
190
57.49
K1
64.107
58.827
58.483
—
K2
60.480
59.077
60.163
—
K3
54.800
61.483
60.740
—
Range
9.307
2.656
2.257
—According to the orthogonal test result, it can be seen that the thermal efficiency increases with increasing the airflow temperature and the inlet cut tobacco moisture content but decreases with the decrease of airflow velocity. The result shows the optimum preparation conditions are an inlet airflow velocity of 15 m/s, an initial cut tobacco moisture content of 26%, and an inlet airflow temperature of 200°C. The thermal efficiency of the dryer and the final cut tobacco moisture content are 66.32% and 14.15%, respectively. The final cut tobacco moisture content meets the requirements of cut tobacco drying process. The result shows that this parabolic trough concentrating solar heating will be a potential heat recourse for cut tobacco drying system.


## 5. Conclusion

A novel parabolic trough concentrating solar heating for cut tobacco drying system was established. The result shows that the heating rate, acquisition factor, and collector system efficiency increase with increasing the opening width of the absorber and can also prevent the cavity from deformation. The simulation results using the cut tobacco drying mathematical model were in good agreement with experimental data for cut tobacco drying process. The optimum preparation conditions were an inlet airflow velocity of 15 m/s, an initial cut tobacco moisture content of 26%, and an inlet airflow temperature of 200°C. The thermal efficiency of the dryer and the final cut tobacco moisture content were 66.32% and 14.15%, respectively. The result showed that this parabolic trough concentrating solar heating would be one of the heat recourse candidates for cut tobacco drying system.



---

*Source: 209028-2014-03-26.xml*