Design og modellering af metanolanlæg til VEnzin-visionen Bilag

VEnzin.for
c:/dna/source/
tau_1_2=b_1_2/(R_u*T_K)
c
x_ME_3=ZA(6)
x_ST_3=1D0−x_ME_3
gamma_2=exp((x_ST_3**2*(tau_1_2*((exp(−(alpha
$ *tau_1_2))/(x_ME_3+x_ST_3*exp(−(alpha*tau_1_2))))
$ )**2+(tau_2_1*(exp(−(alpha*tau_2_1))/(x_ST_3+x_ME_3
$ *exp(−(alpha*tau_2_1)))**2)))))
gamma_1=exp((x_ME_3**2*(tau_2_1*((exp(−(alpha
$ *tau_2_1))/(x_ST_3+x_ME_3*exp(−(alpha*tau_2_1))))
$ )**2+(tau_1_2*(exp(−(alpha*tau_1_2))/(x_ME_3+x_ST_3
$ *exp(−(alpha*tau_1_2)))**2)))))
c
P_ST_IN=X_J(MEDIE(2),H2O_G$)*P(2)
P_ME_IN=X_J(MEDIE(2),CH3OH$)*P(2)
c
P_ME=P_ME_IN*0.999d0
x_ME=P_ME/(gamma_2*P_SAT_ME)
x_ST=1D0−x_ME
P_ST_2=gamma_1*P_SAT_ST*x_ST
P_ST=(P_ME_IN−P_ME+P_ST_IN)−(P_ME_IN−P_ME)/x_ME
if (T.gt.239.1) then
RES(RES_NR)=T−238
else
RES(RES_NR)=P_ST−P_ST_2
endif
c
RES(RES_NR+1)=x_ME−x_ME_3
C
IF (FKOMP.EQ.5) GOTO 500
GOTO 9999
C−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−
C Solution check
C−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−
500 CONTINUE
CALL STATES(P(2),H(2),T2,V,S,X,U,1,2,MEDIE(2))
IF (MDOT(1).LT.−1D−10) GOTO 550
IF (MDOT(2).GT.1D−10) GOTO 550
IF (Q(1).GT.1D−10) GOTO 550
IF (T2.LT.T) GOTO 550
GOTO 9999
550 FBETI = .FALSE.
GOTO 9999
C−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−
C Write component information
C−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−
600 CONTINUE
KOMDSC = ’Methanol converter. Outlet gas is at equilibrium
$ between $ H_2$, CO, $CO_2$, $H_2O$ and $CH_3OH$. One of the
$ conditions for the component is that condensation of methanol
$ and water does not occur.’
K_PAR(1) = ’Pressure loss: $\\Delta p$ [bar]’
K_BET =
$ ’$\\dot{m}_1 \\gt 0 \\\\ \\dot{m}_2 \\lt 0 \\\\ \\dot{Q} \\lt
$0 \\\\ T_2 \\gt T_{condensation} $’
KMEDDS(1) =’Inlet gas’
KMEDDS(2) =’Oulet gas’
KMEDDS(3) =’Heat loss’
k_inp=’struc Meoh−convert MEOH_CONVERTER 601 602 311 0.01\\\\
$media 601 Syngas 602 Syngas−meoh\\\\
$fluid Syngas H2 0.5 CO 0.3 CO2 0.2\\\\
$addco p 601 144\\\\
$addco t Meoh−convert 602 235 t Meoh−convert 601 230 m Meoh−convert
$ 601 100\\\\
$START Y_J Syngas−meoh H2 0.15 Y_J Syngas−meoh CO 0.16\\\\
$START Y_J Syngas−meoh CO2 0.33 Y_J Syngas−meoh CH3OH 0.34\\\\
$START ZA Meoh−convert 5 230’
GOTO 9999
C
9999 CONTINUE
RETURN
END
C=======================================================================
C***********************************************************************
SUBROUTINE SET_M(KOMTY,ANTLK,ANTKN,ANTPK,ANTM1,MEDIE,ANTME
$ ,VARME,MDOT,P,H,ZC,PAR,RES,X_J,KOMDSC,K_PAR,K_lig,K_bet
$ ,KMEDDS,K_inp)
C***********************************************************************
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19−03−2007