global mc mh Cp Cpc Q1 Q2 Q3 Npoint Tf cf dm1 dm2 dm3 dHrx u conc p 

%mc=127*1000/3600;  % flow entering heat exchanger (kg/s)
Cp=3500;           % gas
Cpc=1100;          % catalyst
Npoint=30;         % No. of discretization points; 10 in each bed
rhoc=2200;
vol1=6.69;
vol2=9.63;
vol3=15.2;
dHrx=2.7e6; % [kJ/kg] Note: 111370 * 28 = 3.118 e6
dm1=vol1/Npoint*3*rhoc;  % mass of catalyst in each bed
dm2=vol2/Npoint*3*rhoc;
dm3=vol3/Npoint*3*rhoc;

p =200;          % Reactor pressure, bar

% Paadrag
Q1=58*1000/3600;   % quench flows (kg/s)
Q2=35*1000/3600;
Q3=32*1000/3600;
Tf=250;          % Fresh feed temperature, C
mh=252*1000/3600;  % total feed flow (kg/s)
cf=0.08;  % feed mass fraction of ammonia
mc=mh-(Q1+Q2+Q3);
