7 tipsandtraps upd
TRANSCRIPT
OLGA Tips and Traps
Pipeline discretisation
• For each pipeline GEOMETRY we must specify the number of calculation segments (sections) per pipe
• The number of sections is a compromise: accuracy vs computation time
• The number of sections is important when temperatures, pressuresand velocities change rapidly
Pipeline discretisation cont.
• Some terrain effects are lost if grid is too coarse– due to the staggered grid solution scheme
• Example case:– 3000 SCF/BBL GOR multiphase production– very hilly terrain
Hilly Terrain Multiphase Pipeline Profile
2500270029003100
0 6000 13500 19000Distance (m)
Elev
atio
n (m
)
Effect of pipeline discretisation
Pressure drop varying for varying number of segments
320
360
400
0 2 4 6 8 10 12 14 16 18Multiplication factor for # of segments
Tota
l pre
ssur
e dr
op(p
si)
Pipeline discretisationsummary
• Check sensitivity to discretisation– Finer discretisation reduces errors and increase computing
time• Try to use at least 2 segments for any pipe• Try not to violate the following rule:
Li Li+1
0.5 ≤ Li / Li+1 ≤ 2 for all i
Pipeline discretisation and time step
• The time step HT is limited by the CFL criterion for implicit solutions (default = ON)
CFL: HT < min ( Lsection/Ufluid)
• You may also limit HT by the 2nd derivative of pressure (default = OFF)
• Use DTCONTROL to change defaults
• Moreover, HT is always limited byController action and Slugtracking
SHUT-IN simulations
• In some cases OLGA gives un-physical pressure rises in a pipeline that has been shut-in for a while, where the temperature is falling.
• Ways of getting around it:– Reduce the time step and/or reduce the ratio of
MAXDT/ MINDT to limit the changes in time-step.– Re-section the pipeline with somewhat shorter
sections where there are liquid interfaces.• The problem is mainly due to limitations in the
Fluid Table approach and the best solution is to use either Compositional Tracking or the Black Oil model.– Black oil parameters may have to be tuned with PVTsim
to work properly
Shut-in continued
• The main source of the problem is flashing of liquid to gas when the gas-liquid interface crosses section boundaries due to movements caused by the numerics. There is usually no equivalent condensation, and the result is a slight increase in pressure over time.
• Most frequent problem cases:– several gas/liquid interfaces and relatively little
gas (pressure increases quite rapidly when extra gas is created),
– the liquid density decreases with pressure – there are sections filled with liquid
Steady state - an example
FLOWLINE
Elev
atio
n [m
]
0
-1
-2-2.5
Horizontal length [m]
150010005000
Elevation profile 2
PIPE ID = 0.5 m
total # of sections: 20
Steady state example cont.
Total liquid inventory in % of pipe volume
0
5
10
15
20
25
30
35
0 5 10 15 20 25Flowrate (kg/s)
(%)
Steady state preprocessorDynamic steady state
Steady state example cont.
Total liquid inventory in % of pipe volume
0
4
8
12
16
12 14 16Flowrate (kg/s)
(%)
Steady state preprocessorDynamic steady state
General observation
• At lower flowrates and a pipe with dips and humps (gravity dominated flow) an obtained steady state solution may be meaningless since the flow in reality may exhibit continuous fluctuations.
Steady state stratified flow • All steady state stratified flow models solve the same type of
equation by iterating on liquid holdup (OLGA uses time stepping to “iterate” to a dynamic steady state solution)
• The equation has normally only one root, but it may havemultiple roots for:– upward inclination angles– low liquid velocities– low/medium gas velocities
• Stability analysis show that only one root is stable• The existence of multiple roots is now demonstrated by
experiments• OLGA does not always converge to the minimum liquid holdup
solution (maximum gas volume fraction)
Stratified flow - possible steady state solutions
α = gas volume fraction ≤ 1
1.0
0.5
0.0
-0.5
0.6 0.7 0.8 0.9
F(α)
the solution to F (α) =0 is found by iteration, starting at α =1
liquid holdup = 1- α
UsL = 0.001 m/s
ϕ = 0.2 °
Usg = 0.8 m/s
0.75
0.70.65
Stratified flow - conclusion
• Be concerned whether OLGA finds the right liquid inventory for high GOR flow in hilly terrain
• OLGA should find the right liquid inventory after pigging or after a rate change from a high to a lower rate
Initial conditions
WELL
Pressure boundary
reservoir pressure
The steady state pre-processor may have problems finding a solution at t = 0
Use INITIALCONDITIONS and specify
- a high gas volume fraction (void fraction) everywhere
- pressure gradient with correct direction
Network
• OLGA was designed to handle converging networks
Split nodes and closed loops are also possible
Loop line design case Schematic
Gas Plant
Cluster 1
Cluster 2
Cluster 3
Node Node
Pressure boundary
Pressure boundary
Source1 Source 2 Source 3
Loop line design case- single branch OLGA model
P plant
Loop line design case closed loop OLGA model
Source1
Source2 Source3
Terminal Node Pressure boundary
Merging Node
splitting Node
Terminal Node Closed boundary
A typical network
to e.g. flare
SD Valve
Blow Down Valve
Possible OLGA model
Source
BDV back pressureBDV
SDV
Separator pressureNode:
INTERNAL
ClosedNODE
Pressure NODE
Pressure NODE
BDV
SDVQ
Pb
PsFlow direction
Blow down simulation
Normal operation
Source flow = Q
BDV opening = 0
SDV opening = 1
Blow down
Source flow = 0
BDV opening = 1
SDV opening = 0
Bubble / Dew points
• OLGA does NOT check against dew points– In the gas region - outside the 2-phase region, the
predicted gas mass fraction can be different from 1 due to linear interpolation across the dew point line
• Above bubble point – no mass transfer– i.e. gas is not condensed/dissolved
• When actual P,T is close to critical then fluid properties could be dubious
Phase envelope
0
1000
2000
3000
4000
5000
6000
-100 0 100 200 300 400 500 600 700 800 900
Temperature/°F
Crit P
TEST 4 BHS OIL C10+
Table Points Gas mass fraction could be < than 1 due to linear interpolation
Water vapour and free water
• No separate mass equation for water vapour in basic OLGA
• Assumption:– The gas phase is always saturated with water vapour
Water
Liquid water
Water vapour
FlashingOK
No check on available
wat.vapour
Mass transfer of water
• Water vapour mass fraction from fluid table:
• Change in water vapour mass fraction due to change in pressure and temperature:
TT
Rswpp
RswRsw Δ∂∂
+Δ∂
∂=Δ
gas
OvapourHsw m
mR 2=
Saturated and undersaturated gas
If there is a change in Rsw due to changes of P,Twater may condense even if no water vapour is left in the gas
• Be careful simulating undersaturated gases with standard OLGA
• Possible to turn off water flashing
Standard volume flow in sources and wells
• You may specify e.g. PHASE = OIL in SOURCEQoil , GOR (or GLR) and Water Cut. (Equivalent for gas)
• All the variables are assumed to be at standard conditions• Standard conditions (1 atm. and 60 F) must be a point
within the fluid table P&T boundaries • If you do not specify GOR the fluid table value is used• On terminal nodes you specify GOR (or GLR) and WC
Equivalent mass rate is calculated :
– calculates volume flow of gas using GOR – calculates volume flow of water using WC– converts to mass flows using std. densities– adds up mass flow for each phase
wc: watercut fraction [0, 1]
)1
( STDw
STDg
STDo
STDotot wc
wcGORQm ρρρ−
+⋅+=&
Standard conditions – tips
• Your specified GOR should be ≈ to the GOR of the fluid table
• Use a dense grid in the PVT table around std. cond.– fluid densities are taken from interpolation in PVT table
• OLGA expects that GOR is from a 0. stage flash