| 查看: 2292 | 回复: 2 | |||
wangyuxuan05银虫 (初入文坛)
|
[求助]
液膜表面蒸发fluent求助！
|
|
我的课题是用FLUENT做分子蒸馏器的液膜流体传质传热过程模拟，模拟物系是DHA、油酸（oa）、花生四烯酸（ara），所选的几何区域是高200mm，宽1mm的竖直液膜，操作压力为1pa，上端进口为mass-flow-inlet，左侧为蒸发壁面，下端为压力出口。目前遇到的问题是： 1、右侧液膜表面的边界条件不知道要如何选取 2、液膜表面涉及到多组分的蒸发，所以我想在这个边界上加入一个udf 1）我只做纵向上的一维研究，把组分的蒸发速率编成udf，但是在导入fluent时总是有错误，您能把我看一下程序吗？谢谢！ #include "udf.h" DEFINE_SOURCE(evapor, cell, thread,j) { real nc=80000; real zl=3; real p; real m_e; real M[3]={328.49,282.46,302.45}; real T; real T0=573; real fm; real p0[3]={3200,2800,3000}; real x0[3]={0.2158,0.6268,0.1574}; real interval; real x; if (interval==1) { for (j=0;j<3;j++) { x=x0[j]; } T[cell]=T0; } else { for (i=1;i<=zl;i++) { fm=0; fm=fm+C_YI(cell,thread,i)/M[i-1]; } for (j=1;j<=zl;j++) { x[cell,j]=C_YI(cell,thread,j)/M[j-1]/fm; } T[cell]=C_T(cell,thread); } p[cell,j]=p0[j-1]; m_e(cell,thread,j)=0.9*15.8*x[cell,j]*P[cell,j]*M[j]/T[cell]; return m_e(cell,thread,i,j); } 2）我也尝试着将论坛里水蒸发的udf修改成多组分的蒸发，但是成功导入UDF后，fluent不能运行，您能帮我把这个udf也看看吗？谢谢！ #include "udf.h" #include "sg_mphase.h" #define T_SAT_dha 593 #define T_SAT_ara 533 #define T_SAT_oa 523 #define LAT_HT_dha 237425.8 #define LAT_HT_ara 285632.3 #define LAT_HT_oa 280781.3 DEFINE_SOURCE(liq_src_dha, cell, pri_th, dS, eqn) { Thread *mix_th, *sec_th; real m_dot_l_dha; mix_th = THREAD_SUPER_THREAD(pri_th); sec_th = THREAD_SUB_THREAD(mix_th, 1); if(C_T(cell, mix_th)>=T_SAT_dha) { m_dot_l_dha = -0.1*C_VOF(cell, pri_th)*C_R(cell, pri_th)* fabs(C_T(cell, mix_th) - T_SAT_dha)/T_SAT_dha; dS[eqn] = -0.1*C_R(cell, pri_th)*fabs(C_T(cell, mix_th) - T_SAT_dha)/T_SAT_dha; } else {m_dot_l_dha= 0.1*C_VOF(cell, sec_th)*C_R(cell, sec_th)*fabs(T_SAT_dha-C_T(cell,mix_th))/T_SAT_dha; dS[eqn] = 0.; } return m_dot_l_dha; } DEFINE_SOURCE(vap_src_dha, cell, sec_th, dS, eqn) { Thread * mix_th, *pri_th; real m_dot_v_dha; mix_th = THREAD_SUPER_THREAD(sec_th); pri_th = THREAD_SUB_THREAD(mix_th, 0); if(C_T(cell, mix_th)>=T_SAT_dha) {m_dot_v_dha = 0.1*C_VOF(cell, pri_th)*C_R(cell, pri_th)*fabs(C_T(cell, mix_th) - T_SAT_dha)/T_SAT_dha; dS[eqn] = 0.; } else {m_dot_v_dha= -0.1*C_VOF(cell, sec_th)*C_R(cell, sec_th)* fabs(T_SAT_dha-C_T(cell,mix_th))/T_SAT_dha; dS[eqn] = -0.1*C_R(cell, sec_th)* fabs(C_T(cell, mix_th) - T_SAT_dha)/T_SAT_dha; } return m_dot_v_dha; } DEFINE_SOURCE(liq_src_ara, cell, pri_th, dS, eqn) { Thread *mix_th, *sec_th; real m_dot_l_ara; mix_th = THREAD_SUPER_THREAD(pri_th); sec_th = THREAD_SUB_THREAD(mix_th, 1); if(C_T(cell, mix_th)>=T_SAT_ara) { m_dot_l_ara = -0.1*C_VOF(cell, pri_th)*C_R(cell, pri_th)* fabs(C_T(cell, mix_th) - T_SAT_ara)/T_SAT_ara; dS[eqn] = -0.1*C_R(cell, pri_th)*fabs(C_T(cell, mix_th) - T_SAT_ara)/T_SAT_ara; } else {m_dot_l_ara = 0.1*C_VOF(cell, sec_th)*C_R(cell, sec_th)*fabs(T_SAT_ara-C_T(cell,mix_th))/T_SAT_ara; dS[eqn] = 0.; } return m_dot_l_ara; } DEFINE_SOURCE(vap_src_ara, cell, sec_th, dS, eqn) { Thread * mix_th, *pri_th; real m_dot_v_ara; mix_th = THREAD_SUPER_THREAD(sec_th); pri_th = THREAD_SUB_THREAD(mix_th, 0); if(C_T(cell, mix_th)>=T_SAT_ara) {m_dot_v_ara = 0.1*C_VOF(cell, pri_th)*C_R(cell, pri_th)*fabs(C_T(cell, mix_th) - T_SAT_ara)/T_SAT_ara; dS[eqn] = 0.; } else {m_dot_v_ara = -0.1*C_VOF(cell, sec_th)*C_R(cell, sec_th)* fabs(T_SAT_ara-C_T(cell,mix_th))/T_SAT_ara; dS[eqn] = -0.1*C_R(cell, sec_th)* fabs(C_T(cell, mix_th) - T_SAT_ara)/T_SAT_ara;} return m_dot_v_ara; } DEFINE_SOURCE(liq_src_oa, cell, pri_th, dS, eqn) { Thread *mix_th, *sec_th; real m_dot_l_oa; mix_th = THREAD_SUPER_THREAD(pri_th); sec_th = THREAD_SUB_THREAD(mix_th, 1); if(C_T(cell, mix_th)>=T_SAT_oa) { m_dot_l_oa= -0.1*C_VOF(cell, pri_th)*C_R(cell, pri_th)* fabs(C_T(cell, mix_th) - T_SAT_oa)/T_SAT_oa; dS[eqn] = -0.1*C_R(cell, pri_th)*fabs(C_T(cell, mix_th) - T_SAT_oa)/T_SAT_oa; } else {m_dot_l_oa = 0.1*C_VOF(cell, sec_th)*C_R(cell, sec_th)*fabs(T_SAT_oa-C_T(cell,mix_th))/T_SAT_oa; dS[eqn] = 0.; } return m_dot_l_oa ; } DEFINE_SOURCE(vap_src_oa, cell, sec_th, dS, eqn) { Thread * mix_th, *pri_th; real m_dot_v_oa; mix_th = THREAD_SUPER_THREAD(sec_th); pri_th = THREAD_SUB_THREAD(mix_th, 0); if(C_T(cell, mix_th)>=T_SAT_oa) {m_dot_v_oa = 0.1*C_VOF(cell, pri_th)*C_R(cell, pri_th)*fabs(C_T(cell, mix_th) - T_SAT_oa)/T_SAT_oa; dS[eqn] = 0.; } else {m_dot_v_oa = -0.1*C_VOF(cell, sec_th)*C_R(cell, sec_th)* fabs(T_SAT_oa-C_T(cell,mix_th))/T_SAT_oa; dS[eqn] = -0.1*C_R(cell, sec_th)* fabs(C_T(cell, mix_th) - T_SAT_oa)/T_SAT_oa; } return m_dot_v_oa; |
回复此楼» 收录本帖的淘帖专辑推荐
 博士科研新路历程 |
» 猜你喜欢
瑞典林雪平大学博士后招聘｜PEC Water Splitting 方向
已经有130人回复
-
PRB投稿，Acknowledgment sent to author状态十天了
已经有3人回复
-
物理学I论文润色/翻译怎么收费?
已经有286人回复
-
PVA溶解
已经有2人回复
-
基金申请
已经有44人回复
-
CSC与新西兰维多利亚大学PhD奖学金项目
已经有0人回复
-
新西兰Robinson研究所 招聘CSC公派访问人员
已经有0人回复
-
帮我的英语口语老师找学生
已经有0人回复
-
什么时候开奖？
已经有6人回复
-
散金币祈福
已经有94人回复
» 本主题相关商家推荐: (我也要在这里推广)
» 本主题相关价值贴推荐，对您同样有帮助:
- 新手求助聚砜铸膜液表面遇水生成白色薄膜的问题
已经有6人回复
- 【求助】气液分离两相流动模拟fluent gambit出入口的设置
已经有11人回复
- 【求助】用fluent模拟超重力气液流体动力模型和传质过程，中间有化学吸收反应，fluent
已经有23人回复
- 【求助】Fluent中的对称问题
已经有10人回复
- 【求助】Fluent 收敛问题
已经有10人回复
2楼2019-01-10 11:17:57
|
本帖内容被屏蔽 |
3楼2019-02-11 08:34:28
40