[pranab_jha]

Hello,

I am trying to model evaporation from a droplet. So I have to apply my evaporation model at the interface. I have a 2D axisymmetric case set up. But I am not able to get my UDF to work. Could someone take a look and let me know please. Comments are added for convenience.

SUmmary of the code:
-I have used the DEFINE_MASS_TRANSFER macro and defined all variables and initialized them.

-I calculated saturation pressure using a polynomial function of cell temperature.

-Then the mass fraction of each species is used to compute the molar fraction of required species.

-Then I compute the interfacial area density from the volume fraction gradient.

-Then using that, I compute the mass transferred by evaporation.

Thanks for any help!!!

Temporary solver memory has been turned on from the solve-set-expert menu in Fluent.

/************************************************** *********
UDF to apply mass transfer rate from liquid to gas phase at the interface
************************************************** **********/
#include "udf.h"
#include "sg_mphase.h"
#include "materials.h"

#define MW_W 18.0
#define MW_A 29.0
#define R 8.314
#define pi 3.14159
#define a_c 0.04 /*accommodation coefficient*/

DEFINE_MASS_TRANSFER(mass_transfer1, c, mixture_thread, from_phase_index, from_species_index, to_phase_index, to_species_index)
{
/************ Declare variables *********/
float m_lg, T_cell, P_cell, P_sat;
float NV_VEC(G);
float X_W, Y_W, Y_A;
float cur_ts;
Thread *w_liq, *gas_mix, *w_gas;
face_t f;
Domain *mix_domain, *pdomain;
int i, pdomain_index;
float area[ND_ND], A, ad, theta, cotan, len;

/******** Define variables *********/
mix_domain = Get_Domain(1);
/* pdomain = DOMAIN_SUB_DOMAIN(mixture_domain,1); */ /* For gas domain */
pdomain_index = 0;
pdomain = DOMAIN_SUB_DOMAIN(mix_domain,pdomain_index);

w_liq = THREAD_SUB_THREAD(mixture_thread, from_phase_index);
gas_mix = THREAD_SUB_THREAD(mixture_thread, to_phase_index);
w_gas = THREAD_SUB_THREAD(mixture_thread, to_species_index);

T_cell = C_T(c,mixture_thread); /*cell mixture temperature*/
P_cell = C_P(c,mixture_thread); /*cell mixture pressure*/
m_lg = 0.;
cur_ts = CURRENT_TIMESTEP; /* real time step size (in seconds)*/

/* compute saturation pressure for water vapor using polynomial fit */
P_sat = 0.000001*pow(T_cell,5) - 0.001*pow(T_cell,4) + 0.681*pow(T_cell,3) - 203.9*pow(T_cell,2) + 39482*T_cell + 4000000;

/* calculate molar fraction X_W from mass fraction Y_W */
Y_W = C_YI(c,gas_mix,0); /* index for water vap = 0, air = 1*/
Y_A = C_YI(c,gas_mix,1);
X_W = (Y_W*29)/((29*Y_W) + (18*Y_A));

/**** Compute the interfacial area density ****/
NV_V(G,=,C_VOF_G(c,w_liq)); /* vof gradient vector assignment*/

theta = atan(G[0]/G[1]); /* compute angle of VOF gradient vector, n1/n2 because of how geometry is set up in Fluent */
cotan = cos(theta) / sin(theta); /* compute cotangent of angle*/

A = C_VOLUME(c,mixture_thread)/(2*pi); /* in 2D- axis area computed from volume */

len = sqrt((2*C_VOF(c,w_liq)*A/cotan) + (2*C_VOF(c,w_liq)*A*cotan)); /* compute length of interface in a cell */

ad = len/A; /* calculate interfacial area density*/
/***** Computed the area density ad = length of interface / area of cell ***/

if (C_VOF(c, w_liq) != 0.0 && C_VOF(c, w_liq) != 1.0)
{
Message("AD = %f, theta = %f\n",ad, theta);

/* Compute m_lg only if P_sat > (Pcell*XW) */
if (P_sat - (P_cell*X_W) > 0.0)
{
m_lg = cur_ts * ad *(2*a_c/(2-a_c)) * sqrt(MW_W/(2*pi*R)) * ((P_sat - (P_cell*X_W)) / sqrt(T_cell));
}
else
{ m_lg = 0.0;}
}
else
{ m_lg = 0.0;}

return (m_lg); /* return value of mass transfer rate */

}