Design og modellering af metanolanlæg til VEnzin-visionen Bilag

VEnzin.for
c:/dna/source/
IF (MDOT(2).LT.−1D−10) GOTO 550
IF (MDOT(3).GT.1D−10) GOTO 550
IF (MDOT(4).GT.1D−10) GOTO 550
IF (T1.GT.T3) GOTO 550
IF (T2.LT.T4) GOTO 550
IF (Q.GT.1D−10) GOTO 550
IF (X_J(MEDIE(1),37)−X_J(MEDIE(3),37).LT.−1D−6) GOTO 550
IF (X_J(MEDIE(1),7).GT.1D−10) GOTO 550
GOTO 9999
550 FBETI = .FALSE.
GOTO 9999
C−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−
C Write component information
C−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−−
600 CONTINUE
KOMDSC = ’Steam dryer for solid fuels (Steam is a real fluid).’
K_PAR(1) = ’Moisture content of dried fuel’
K_PAR(2) = ’Pressure loss: $\\Delta p$ [bar]’
K_BET = ’$\\dot{m}_1 \\gt 0 \\\\ \\dot{m}_2 \\gt 0 \\\\
$\\dot{m}_3 \\lt 0 \\\\ \\dot{m}_4 \\lt 0 \\\\
$T_1 \\lt T_3 \\\\ T_2 \\gt T_4 \\\\ Q \\lt 0 \\\\
$x_{1,H_2O} \\gt x_{3,H_2O}$’
KMEDDS(1) = ’Solid in’
KMEDDS(2) = ’Steam in’
KMEDDS(3) = ’Dry solid out’
KMEDDS(4) = ’Steam out’
KMEDDS(5) = ’Heat loss’
K_INP=’struc dryer DRYER_04 1 2 3 4 300 0.05 0\\\\
$media 1 Wood 3 dry−wood\\\\
$SOLID Wood H .0305 O .1886 H2O−L .5 C .2503 S .00005 ASH .0255\\\\
$+ N 0.003 36 0.00205\\\\
$+ LHV 21750 CP 1.35\\\\
$addco m dryer 1 2.05 t dryer 1 15 p 1 1\\\\
$addco t dryer 2 322 t dryer 3 150 t dryer 4 150\\\\
$addco p 2 1 p 3 1\\\\
$addco q dryer 300 0\\\\
$START M dryer 2 8.3 M dryer 3 −1\\\\
$START X_J dry−wood H2 0.057 X_J dry−wood O2 0.35\\\\
$START X_J dry−wood C 0.47 X_J dry−wood H2O−L 0.05’
C
9999 CONTINUE
RETURN
END
C=======================================================================
C***********************************************************************
SUBROUTINE GASIFI_3_VENZIN(KOMTY,ANTLK,ANTEX,ANTKN,ANTPK,ANTM1,
: MMVAR,PARNAM,ZANAM,MEDIE,
: ANTME,VARME,ANTEL,VAREL,MDOT,P,H,Q,PAR,ZA,ZC,
: RES,X_J,CP,HV,HF,KOMDSC,KMEDDS,K_LIG,k_par,K_BET,k_inp)
C***********************************************************************
C
C GASIFI_3 is a model of a gasifier. The fuel is added
C with water based on the steam table and is gasified using an
C oxydant. The
C gasifier works at given pressure and temperature. Through the plant
C is a constant pressure drop. A heat loss representing real losses
C due to radiation and convection, and also the removed high tempe−
C ture ashes is modelled. Using equilibrium assumption and minimizing
C Gibbs energy the composition of the raw gas is found. Pressure and
C temperature are identical on all outlets.
C
c be 20041117 A new parameter for bypassing methane from the
c equilibrium calculation has been added
C***********************************************************************
C
CA FKOMP − INPUT − Flag with the value:
CA 1: Initialize the component.
CA 2: Initialize with actual system.
CA 3: Fluid composition calculation (constant).
CA 4: Find residuals.
CA 5: Find residuals and check variables.
CA 6: Output information about component.
CA MDOT − INPUT − Massflows from nodes.
CA P − INPUT − Pressure in nodes.
CA Q − INPUT − Exchanged heat.
CA PAR − INPUT − Parameters of the component.
CA X_J − INPUT − Fluid composition.
CA KOMTY − OUTPUT − Component name.
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