Can anyone help me with next code?
clear all clc
Param=[4.3276103255301335 0.10215543561231799 12.346130949956718 0.04565511507929096 0.0074744247798137625 0.0022142903501092513 1.6957452439712215 0.008166212885461337 0.028435528710812962 6.156650857937292 2.0566837008694536 0.9088238699999999 0.8669780915448081 8.072715437027492 0.010453310496367572 5.260491048 5.325728554979126 6.837140753063702 0.03947867100809781]; Optim=[1.4989542634814161 1.4335418277418217 1.5744495703184183 0.2559519340674219 0.7975221812123433 1.3319125502728477 1.1153538963112686]; Sens=[0.5 0.973342635 2 8.827704916 0.87519757 1.2];
% Parameters for Fed-Batch Models um=0.54*Param(1)*0.6*0.6*0.5*Optim(1);%h^-1 tomada de Development of a structure dynamic model Ksr=0.15*Param(2); %adimensional saturation constant for the inhibition due to N/C, tomada de Simulation and optimization of PHB Sm=0.3*Param(3)*Optim(2);%adimensional, relación N/C a la cual miu es cero tomada de Simulation and optimization of PHB Csx=1.7640*Param(4)*0.59*25*Optim(3);%gS/gX taken from model baed fed batch cultivation as the a value Rcsx=0.022*Param(5)*Optim(4);%*50Sucrose specific consumption rate for respiration/maintenance for the residual biomass (g/gh) Csp=1.7460*Param(6);%gS/gP taken from model based fed batch cultivation as the b value k1=0.14*Param(7)*1.5*Optim(5);%gP/gX taken from model based fed batch cultivation as the e value k2=0.74*Param(8);%gP/gX h taken from development of a structured Cnx=0.336*Param(9);%gN/gX h taken from updated mathematical model and fedbatch as the parameter d KL=0.1*Param(10);%1/h taken as constant from development of a structured dynamic model k3=93*Param(11);%gO2/gX taken from development of a structured dynamic model k4=85*Param(12);%gO2/gP taken from development of a structured dynamic model the parameter was k5 O2Leq=7.6*10^-3*Param(13);%taken from development of a structured dynamic model as O2loeq nk=1.22*Param(14)*Optim(6);%adimensional exponent on the kinetic expression taken from simulation and optimisation Rcnx=0.16*Param(15)*Optim(7);%taken from mode based dynamic optimization alfa1=0.143*Param(16); %mmolCO2/g biomass alfa2=0.0000004*Param(17); %mmolCO2/ g biomass h alfa3=0.0001*Param(18); %mmolCO2/lh Kox=0.02*Param(19); %gO2/gX Taken from A modular simulation package for fed-batch fermentation: penicillin production
%Parameters for polymerization model ki=0.62*10^4; kp=0.46*10^5; kt=0.14*10^1; km1=0.11*10^-3; km2=0.86*10^7; kd=0.83*10^2;
%Initial Conditions validation data X(1)=1.16;%0.433743333333333;%active biomass g/L S(1)=20.05;%43.4579133333333*Sens(1); %fructose g/L N(1)=2;%0.577887666666667*Sens(2);%Nitrogen g/L P(1)=1.01;%0.136603333333333;%PHA g/L O2L(1)=0.002432; CO2(1)=0.01; V(1)=4; V1(1)=0; V2(1)=0;
%Initial Conditions for polymerization M(1)=0; ESHM(1)=0; dp1dt(1)=0; dp2dt(1)=0; dDdt(1)=0;
F3=0.1; Sin=300*Sens(3);%g/L Fructose Cocentration in the feeding Nin=7*Sens(4); %g/L Nitrogen concentration in the feeding O2in=0.002432; %g/L
Yms=3.48*10^-3;%calculado con los datos iniciales del papaer Jf=0.2818; %initial iteration for substrate Jm=Yms*Jf;
%Specific growth rate u(1)=um*((N(1)/S(1))/((N(1)/S(1))+Ksr))*(1-((N(1)/S(1))/Sm)^nk)*((O2L(1)/(Kox*X(1)+O2L(1))));
tsim=50; t(1)=0; dt=0.001; i=1;
Nt=50;%for fixed pivot method
% Euler Method for ODE´s solution while t(i)<tsim
if t(i)<6 F1=0; F2=0; elseif t(i)>6 && t(i)<10 F1=0; F2=70*(1/1000)*Sens(5); Fobj31=1.3*F2*4; elseif t(i)>10 && t(i)<16 F1=80*(1/1000)*Sens(6); F2=70*(1/1000)*Sens(5); Fobj32=3.2*F1*6+1.3*F2*6; elseif t(i)>16 && t(i)<20 F1=80*(1/1000)*Sens(6); F2=0; Fobj33=3.2*F1*4; Fobj3=Fobj31+Fobj32+Fobj33; else F1=0; F2=0; end V(i+1)=V(i)+(F1+F2)*dt; V1(i+1)=F1; V2(i+1)=F2; % Fed-Batch States
X(i+1)=X(i)+(u(i)*X(i)*dt-((F1+F2)/V(i))*X(i)*dt);%Biomass
S(i+1)=S(i)-((Csx*u(i)*X(i))+(Rcsx*X(i))+Csp*((k1*u(i)*X(i))+(k2*X(i))))*dt+(F1/V(i))*Sin*dt-((F1+F2)/V(i))*S(i)*dt;%Carbon Source
P(i+1)=P(i)+((k1*u(i)*X(i))+(k2*X(i)))*dt-((F1+F2)/V(i))*P(i)*dt;%Polymer
N(i+1)=N(i)-((Cnx*u(i)*X(i))+(Rcnx*X(i)))*dt+(F2/V(i))*Nin*dt-((F1+F2)/V(i))*N(i)*dt;%Nitrogen Source
if N(i+1)<0.15 N(i+1)=0.15; end O2L(i+1)=O2L(i)+((KL*(O2Leq-O2L(i)))-(k3*u(i)*X(i))-((k4*k1*u(i)*X(i))+(k4*k2*X(i))))*dt+(F3/V(i))*O2in*dt-((F1+F2)/V(i))*O2L(i)*dt;%Dissolved Oxygen
if O2L (i+1)<0.002432 O2L(i+1)=0.002432; end CO2(i+1)=CO2(i)+((alfa1*u(i)+alfa2)*X(i)*dt)+(alfa3*dt)-((F1+F2)/V(i))*CO2(i)*dt;%Dissolved CO2
u(i+1)=um*((N(i+1)/S(i+1))/((N(i+1)/S(i+1))+Ksr))*(1-((N(i+1)/S(i+1))/Sm)^nk)*((O2L(i)/(Kox*X(i)+O2L(i)))); if u(i+1)<0 u(i+1)=0; end %se quita acá
% t(i+1)=t(i)+dt;
% i=i+1;
%
% end %hasta acá
%Monomer and Complex definition
ESHM(i+1)=ESHM(i)+(-((F1+F2)/V(i))*ESHM(i)*dt+(km1*M(i)*dt)-(ki*(ESHM(i)*dt))); %Synthase-Monomer Complex
dp1dt(1)=1;%
for n=1:Nt M(i+1)=M(i)+ (-((F1+F2)/V(i))*M(i)*dt+(-((Csx*u(i)*X(i))+(Rcsx*X(i))+Csp*((k1*u(i)*X(i))+(k2*X(i))))*Yms)-(km1*M(i)*dt)-(km2*M(i)*dp1dt(n))*dt); %Monomer (revisar acá dp1dt(n))
% t(i+1)=t(i)+dt; % i=i+1; % end % end % % % %Polymerization Equations % % % Revisar acá for i=1:Nt % for k=1:j dp1dt(i)=(-((F1+F2)/V(i))*dp1dt(i)+(ki(ESHM))-(km2*(dp1dt(i)*M(i)))+kp*(dp2dt(k)*A-kt*dp1dt(i)));%Lumped Molar balances equations for the active polymer chain dp2dt(i)=(-((F1+F2)/V(i))*dp2dt(i)+(km2*(dp1dt(i)*M(i)))-(kp(dp2dt(i)))); %Lumped Molar balance equation for the intermediate polymer chain dDdt(i)=(-((F1+F2)/V(i))*dDdt(i)+(kt*dp1dt(i))-(kd*dDdt(i))+(kd*(dDdt(k)*B))); %Lumped molar balance equation for the inactive polymer chain end end t(i+1)=t(i)+dt; i=i+1; end
% end
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