本人用ctex編輯一篇文檔，用的{cctart}模板編輯，編譯用的pdftex。在文檔中插入幾張圖片均能用pdf正常輸出，但在我用同樣的方法再插入一張圖片后，編譯沒有問題，可以打開pdf卻打不開，顯示錯(cuò)誤：文檔打開時(shí)出錯(cuò)，文件已損壞并無法修復(fù)。但我試著將插入圖片的位置調(diào)整一下后，又有可能正常輸出并打開，我想問下大神，這算怎么回事啊？？（應(yīng)該不是我插入圖片的命令什么有問題，因?yàn)槲抑�前插入的能正常輸出，我用同樣的方法在此基礎(chǔ)上在插入時(shí)出的錯(cuò)�。┓浅８兄x，希望大家能幫幫我！
以下是我的源代碼
\documentclass[11pt]{cctart}
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\usepackage{graphicx}
\usepackage{epstopdf}
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\usepackage{psfig}
\setlength{\parindent}{0cm} %段落中第一行縮進(jìn)設(shè)為12pt
\setlength{\parskip}{3pt plus1pt minus2pt} %plus伸展值minus收縮值
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\title{\bfseries Two energy conservation principles in convcctive heat optiminization}
\author{Fang Yuan, Qun Chen*\\匯報(bào)人：李貴}

\begin{document}
\maketitle
\zihao{4}\ziti{B} \quad Abstract  \\
\hspace*{2\ccwd}\zihao{-4} In this contribution, in order to
effectively optimize convective heat transfer, such two principles
as the field synergy principle and the entransy dissipation extremum
principle are investigated to reveal the physical nature of the
entransy dissipation and its intrinsic relationship with the field
synergy degree.We first established the variational relations of the
entransy dissipation and the field synergy degree with the heat
transfer performance, and then derived the optimization equation of
the field synergy principle and made comparison with that of the
entransy dissipation extremum principle. Finally the theoretical
analysis is then validated by the optimization results in both a
fin-and-flat tube heat exchanger and a foursquare cavity. The
results show that, for prescribed temperature boundary conditions,
the above two optimization principles both aim at maximizing the
total heat flow rate and their optimization equations can
effectively obtain the best flow pattern. However, for given heat
flux boundary conditions, only the optimization equation based on
the entransy dissipation extremum principle intends to minimize the
heat transfer temperature difference and could get the optimal
velocity and temperature fields.\\


\zihao{4}\ziti{B} 2.\quad 對(duì)流換熱的最優(yōu)化原則\\
\zihao{-4}\ziti{B} 2.1\quad 傳熱性能和場協(xié)同程度的關(guān)系\\
對(duì)于無內(nèi)熱源的不可壓流對(duì)流換熱過程，忽略粘性耗散，能量方程可以表示為：
\[{\rho}c_pU\cdot{\nabla}T={\nabla}{\cdot}(\lambda{\nabla}T)~~(3)\]
對(duì)（3）式進(jìn)行積分，忽略進(jìn)口和出口的縱向熱傳導(dǎo)，并運(yùn)用高斯定理有：
\[\iiint_V{\rho}c_pU{\cdot}{\triangledown}TdV=\iiint_V{\rho}c_p\lvert{U}\rvert{\lvert{\nabla}T\rvert}cos{\beta}dV=\iint_S{\vec{n}}{\cdot}({\lambda{\nabla}T})dS~~(4)\]
引入以下無量綱參數(shù)：
\[\bar{U}=\frac{U}{U_m},~~{\nabla}{\bar{T}}=\frac{{\nabla}T}{(T_m-T_b)/D}~~(5)\]
則（4）式可以化為：
\[\iiint_{v_0}(\bar{U}{\cdot}{\nabla}{\bar{T}})d\vec{V}=\frac{Nu}{Repr}=Fc~~(6)\]
$Fc$為場協(xié)同數(shù)，表示流體速度和溫度梯度在整個(gè)流場中的協(xié)同程度。從（6）式可以看出，對(duì)于給定入口流速，由于$Re$和$Pr$為常數(shù)
，所以$Nu$隨$Fc$的增大而增大。即換熱性能越好。

\zihao{-4}\ziti{B} 2.2\quad 火積耗散與傳熱性能的關(guān)系\\
在（3）式左右兩邊乘以溫度$T$，我們得到，
\[U\cdot{\nabla}(\frac{1}{2}\rho{c_p}T^2)={\nabla}\cdot(\lambda{T}{\nabla}T)-\lambda\lvert{\nabla}T\rvert^2~~(8)\]
即，
\[U\cdot{\nabla}G={\nabla}\cdot(\lambda{T}{\nabla}T)-\lambda\lvert{\nabla}T\rvert^2~~(9)\]
令$\phi_h=\iiint_v\lambda\lvert{\nabla}T\rvert^2dV$,可以作為不可逆的量度。

對(duì)（8）式在整個(gè)流場積分，并運(yùn)用高斯定理，有：
\[\phi_h=\iint_S{-q^{''}}T\cdot\vec{n}dS+\frac{\rho{c_p}U_{in}{T_{in}}^2}{2}-\frac{\rho{c_p}U_{out}{T_{out}}^2}{2}~~(10)\]
當(dāng)邊界熱通量$q^{''}$給定時(shí)，（10）式可以表示為;
\[\phi_h={-q^{''}}\cdot\vec{n}S\iint_S{\frac{T}{S}}dS+\frac{\rho{c_p}U_{in}{T_{in}}^2}{2}-\frac{\rho{c_p}U_{out}{T_{out}}^2}{2}~~(11)\]
因?yàn)榱黧w吸收或釋放的熱量等于通過邊界轉(zhuǎn)移的熱量，所以（11）式可以進(jìn)一步簡化為：
\[\phi_h=Q（T_b-\frac{T_{in}+T_{out}}{2}）~~(12)\]
其中，$\frac{T_{in}+t_{out}}{2}$表示流體的平均溫度，$T_b$表示平均邊界溫度。
\[Q\delta({\Delta}T)=\delta(\phi_h)~~(13)\]
其中，${\Delta}T=T_b-\frac{T_{in}+T_{out}}{2}$表示溫差。 \\
由（13）式可知，對(duì)于總邊界熱流量不變的情況，在熱傳遞區(qū)域，最小火積耗散率可以導(dǎo)出流體和邊界的最小
溫差。（the minimum entransy dissipation rate in the heat transfer
domain leads to the least temperature difference between the fluid
and the wall） 對(duì)于給定邊界溫度$T_b(T_b>T_{in})$,由（10）式可得，
\[(T_b-T_{in}-\frac{Q}{US\rho{c_p}})\delta{Q}=\delta(\phi_h)~~(15)\]

由于${\delta}^2Q<0$,(15)式是最大值原理。也就是說，當(dāng)邊界溫度固定時(shí)，火積耗散最大導(dǎo)致熱流量最大
（when the boundary temperature is fixed, the maximum
entransydissipation rate in the heat transfer domain leads to the
largest heat flow rate, i.e. the optimal heat transfer
performance.） \\
另外，如果對(duì)流傳熱發(fā)生在一個(gè)有內(nèi)熱源的封閉系統(tǒng)，則，能量守恒方程可以表示為：
\[{\rho}c_pU\cdot{\nabla}T={\nabla}{\cdot}(\lambda{\nabla}T)+q_v~~(16)\]
其中$q_v$表示熱源。假設(shè)只有一個(gè)邊界溫度是恒溫，其它邊界都是絕熱的，（16）式兩邊乘以T,有，
\[\nabla\cdot{(\rho{c_p}UT^2/D)}-\frac{c_pT^2}{2}\nabla\cdot(\rho{U})=-\nabla\cdot{({\lambda}T{\nabla}T)}-{\lambda}\lvert{\nabla}T\rvert^2+q_vT~~(17)\]
對(duì)（17）式積分，并利用高斯公式和變分方法的，有，
\[\phi_h=Q(T_f-T_b)~~(18)\]
其中$Q=q_vV$式總熱流量，$T_f$是平均溫度。這種情況，當(dāng)
\[Q\delta(T_f)=\delta(\phi_h)~~(19)\]
從（19）式可知，在這種條件下，在腔中，最小火積耗散可以導(dǎo)致最小平均溫度。（it
is clear that the minimum entransy dissipation in this condition
leads to the minimum average temperature in the cavity.）

總的來說，在不同邊界條件下，最小火積耗散原則和最大火積耗散可以簡單的稱為EDEP，即火積耗散極值原理可以優(yōu)化傳熱性能。
（the extremumof entransy dissipation leads to the optimal heat
transfer performance.）

\zihao{-4}\ziti{B} 2.3\quad 基于歐拉方程的FSP\\
\[\Pi=\iiint_V\{{\rho}{c_p}U{\cdot}{\nabla}T+C_{\phi_m}
+A[{\rho}{c_p}U\cdot{\nabla}T-{\nabla}T\cdot({\lambda}{\nabla}T)~~(21)]
+B{\nabla}T\cdot(\rho{U})\}dV\]
由火積散極值原理得到的歐拉方程：
\[\rho{U}\cdot{\nabla}U=-{\nabla}P+\mu{\nabla}^2U+(C_{\phi}A{\nabla}T+\rho{U}\cdot{\nabla}U)~~(29)\]

\zihao{-4}\ziti{B} 2.4\quad 基于歐拉方程的EDEP（The EDEP-based
Euler’s equation）\\
\[\Pi=\iiint_V\{{\lambda}{\nabla}T{\cdot}{\nabla}T+C^{'}_{\phi_m}
+A^{'}[{\rho}{c_p}U\cdot{\nabla}T-{\nabla}T\cdot({\lambda}{\nabla}T)]+
B^{'}{\nabla}T\cdot(\rho{U})\}dV~~(30)\]
\[C^{'}_{\phi}=\frac{\rho{c_p}}{2C^{'}}~~(33)\]
\[F=C^{'}_{\phi}A^{'}{\nabla}T+\rho{U}\cdot{\nabla}U~~(34)\]
總的來說，場協(xié)同程度和火積耗散率兩個(gè)物理量不僅都可以作為評(píng)價(jià)傳熱性能的指標(biāo)，而且都能指導(dǎo)我們通過變分法獲得
在約束條件下獲得最佳流場。\\

\zihao{4}\ziti{B} 3.\quad a fin-and-flat tube換熱器的優(yōu)化\\
\zihao{-4}\ziti{B} 3.1\quad 數(shù)值模型\\
\hspace*{2\ccwd}\zihao{-4}Fig 1 is the sketch of the elementary
pattern of air-side geometry of an actual condenser with the
detailed parameters listed in Table 1, where a laminar heat transfer
process takes place. In this paper, only half of the tube and two
half of the fins are presented due to the symmetry, and the air is
taken as the working fluid with constant physical properties,
including:$\rho=1.128kg m^{-3}$,$\mu=1.91\times10^{-5}kg
m^{-1}s^{-1}$,$\lambda=0.0276 Wm^{-1}K^{-1},c_p=1005Jkg^{-1}K^{-1}$
\begin{figure}[!htbp]
\centering
\includegraphics[height=6cm,width=8cm]{fig1.eps}
\caption{The sketch of the computational domain and boundary
conditions}
\end{figure}
\hspace*{2\ccwd}\zihao{-4}The meshes at the sections of $z=8.25mm$,
$x=2mm$ and $y=0.65mm$ are showed in Fig. 2(a)-(c), respectively,
which are more condensed in the near wall and entrance regions,
where the steeper velocity gradients are expected. In order to set
boundary condition of variable A at outlet conveniently, the
computational domain is extended downstream ten times the fin
length, and then the gradient of variable A at outlet is assumed to
be zero.
\begin{figure}[!htbp]
\centering
\includegraphics[height=8cm,width=5cm]{fig2.eps}
\caption{Computation meshes of the calculating domain}
\end{figure}

\zihao{-4}\ziti{B} 3.3\quad Mesh independence of the solution\\
\hspace*{2\ccwd}\zihao{-4}For the sake of adopting an appropriate
grid system, a grid refinement is conducted to investigate the
influence of the grid density on the numerical results. The
simulation results of five different grid systems at a constant
boundary temperature are shown in Fig. 3. Compared to the finest
grid 133$\times$42$\times$696, the grid 133$\times$42$\times$520
yields 0.2\% lower Nu. Thus, the grid 133$\times$42$\times$696 has
the sufficient precision for numerical
simulation.\\
To further validate the computational model, the predicted heat
transfer characteristics (j-factor) under different Reynolds numbers
is also compared with that calculated from the empirical relation
proposed by Sieder and Tate [38], which are provided in Fig. 4.

\zihao{-4}\ziti{B} 3.3\quad Optimization at a constant boundary
temperature\\
When the airflow with the inlet velocity and temperature of 2m/s and
308K, respectively, and the wall temperature of the rectangular
domain keeps at 327K, Fig. 5(a)-(c) show the optimal distributions
of velocity vector, velocity magnitude and temperature at the cross
section of z=8.25mm based on the EDEP with
$C^{'}_{\phi}=-1\times10^(-2)$in Eq.(31).

\begin{figure}[!htbp]
\centering
\includegraphics[height=5cm,width=6cm]{fig3.eps}
\caption{The Nusselt number, Nu, versus the grid number}
\end{figure}

\hspace*{2\ccwd}\zihao{-4}There exist five vortexes in the
computational domain, which play the role of strengthening the
mixture of the flow near the wall with the mainstream so as to
transfer more heat from the boundary into the mainstream. In
addition, from Fig. 5(b), it is clear that the velocity magnitude of
vortex which reflects the strength of vortex becomes larger from the
near tube region to the center between every two tubes.

\begin{figure}[!htbp]
\centering
\includegraphics[height=5cm,width=6cm]{fig4.eps}
\caption{The heat transfer characteristics, j-factor, versus the
Reynolds number, Re.}
\end{figure}
\hspace*{2\ccwd}\zihao{-4}Increasing
$C^{'}_{\phi}=-3.5\times10^(-2)$, we may get the optimized results
at the same cross section shown in Fig. 6(a)-(c).The comparison of
Figs. 5 and 6 indicates that the vortexes formed at the cross
section increase to nine with the average velocity magnitude and
temperature becoming larger and higher, respectively. Therefore, it
can be concluded that as the absolute value of$C^{'}_{\phi}$ which
represents the viscous dissipation rate is increasing, the flow with
much more turbulence will be obtained so as to increase the heat
flux from the boundary, and consequently optimize heat transfer.
\begin{figure}[!htbp]
\centering
\includegraphics[height=8cm,width=10cm]{fig5.eps}
\caption{Optimal distributions of velocity vector, velocity
magnitude and temperature based on the EDEP at z=8.25mm
($C^{'}_{\phi}=-1\times10^{-2}.$)}
\end{figure}
\hspace*{2\ccwd}\zihao{-4}Based on Eqs. (24) and (32), Fig. 7 gives
the Nu variation with different viscous dissipation rates. The
results show that the Nu increases along with the viscous
dissipation rate and the optimized trend curves based on two
optimization principles are nearly the same

\begin{figure}
\centering
\includegraphics[height=5cm,width=6cm]{fig7.eps}
\caption{The Nusselt number, Nu, versus viscous dissipation rate,
$\Phi_m$}
\end{figure}

\hspace*{2\ccwd}\zihao{-4}Moreover, Fig. 8(a)-(c) show the optimal
distributions of velocity vector, velocity magnitude and temperature
at the cross section of z=8.25mm based on the FSP, respectively. In
a word, the optimized results are in reasonable agreement with our
theoretical analysis, i.e. the FSP and EDEP optimizations for a
prescribed boundary temperature are the same, they both can
effectively maximize the total heat flow rate.
\zihao{4}\ziti{B} 3.4\quad Optimization at a constant heat flux\\
\hspace*{2\ccwd}\zihao{-4}For the prescribed heat flux $q^{''}$ in
the simulation model, based on the EDEP where
$C^{'}_{\phi}=1.25\times10^(-2).$, the optimal distributions of
velocity vector, velocity magnitude and temperature are shown in
Fig. 9(a)-(c), respectively. Eleven vortexes exist in the
computational domain, which reduce the heat transfer temperature
difference by 24.2\%, and increase the Nu by 31.9\%.


\hspace*{2\ccwd}\zihao{-4}Fig. 10 gives
the Nu at different viscous dissipation rates based on the EDEP.
Increasing the overall viscous dissipation rate effectively enlarges
the Nu based on the EDEP. It exactly corresponds with the
theoretical analysis.


\hspace*{2\ccwd}\zihao{-4}According to the physical meaning of
variational method, the Euler’s equation derived based on the FSP
will not make any contribution to decrease the temperature
difference. Fig. 11 indicates that the optimized results are the
same but with the viscous
dissipation decreasing 5.24\% and the Nu reducing 3.94%.
Therefore, the numerical results further prove that, for prescribed
heat flow rate boundary conditions, only the EDEP does work.


\zihao{4}\ziti{B}4\quad Optimization in a foursquare cavity
\zihao{4}\ziti{B} Conclusion\quad\\
\hspace*{2\ccwd}\zihao{-4}By establishing the relationships of the
field synergy degree and the entransy dissipation over the entire
domain with the total heat flow rate (temperature difference) in
convective heat transfer processes for both open and closed systems,
we find that both the field synergy degree and the entransy
dissipation rate are suitable for evaluating heat transfer
performance. With the criterion of maximum field synergy degree, the
FSPbased Euler’s equation is derived by the variational method, and
thereafter compared to the one deduced from the EDEP. It indicates
that both the FSP and the EDEP will obtain the best flow pattern for
a given boundary temperature, regardless of the different forms of
the governing equations of variables A and A’. However, for a
prescribed heat flux boundary condition, since the field synergy
degree over the entire domain keeps constant, the Euler’s equation
based on the FSP, in this case, makes no contribution to heat
transfer optimization. Next, we investigate the laminar heat
transfer process in the air side of a fin-and-flat tube heat
exchanger. For a prescribed temperature boundary, with the viscous
dissipation rate increasing, both two optimization principles will
make the Nu increase. Moreover, for the same dissipation rate, the
optimization results based on the EDEP and the FSP are the same.
However, for a prescribed heat flux boundary condition, only the
optimized flow based on the EDEP enlarges the Nu, whereas the
optimization based on the FSP makes no sense. Furthermore, a similar
process in a foursquare cavity is also optimized and the same
conclusion is obtained, which is well agreed with the theoretical
analysis. In conclusion, the EDEP and the FSP are both suitable for
the optimization of heat transfer to improve energy utilization
performance, where the EDEP is superior due to its effectiveness in
heat tranfer optimization with prescribed boundary heat fluxes.
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