fuel cell stack model based on multipliply shared space method steven b. beale* and sergei v....

FUEL CELL STACK MODEL BASED ON MULTIPLIPLY SHARED SPACE METHOD

Steven B. Beale* and Sergei V. Zhubrin**

* National Research Council, Ottawa, Canada** Flowsolve Ltd, London, United Kingdom

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Contents

Introduction to distributed resistance analogy

Introduction to solid oxide fuel cells

Governing equations

Cell and stack geometries considered

Comparison of present model with detailed calculations

Discussion of results

Conclusions and future work

3

DISTRIBUTED RESISTANCE ANALOGY

Problem: Not possible to make grid fine enough to capture flow around all tubes.

Solution: Prescribe distributed resistance, F, and heat transfer coefficients, , and solve for superficial flow around baffles. Values of f, and Nu, obtained from experiments, analysis, or detailed numerical simulations.

4

DISTRIBUTED RESISTANCE ANALOGY

Original scheme developed by Patankar and Spalding (1972) only shell-side flow solved for. Key concept: replace diffusion terms with prescribed rate terms

Problem: In general CFD codes only admit to a single value for pressure, p. How to solve for two ‘phases’ at a given point?

Multiply-shared Space method (MUSES) developed in 1990’s to solve this problem.

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5

SOLID OXIDE FUEL CELL

Converts chemical energy to electricity and heat.

Basic components anode, cathode, electrolyte.

O2- ions produced at cathode combine with electrons and H2, at anode to form H2O.

Operate at 800-1 000 °C,

Thermally induced stresses, and performance of cell important.

Cells ‘stacked’ together to increase voltage; Fuel/air introduced through manifolds. Stainless steel interconnects make electrical connection. Uniform flow/pressure important.

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SOLID OXIDE FUEL CELL

Many CFD companies now developing PEM and SOFC models – None of these codes can be scaled to model stack.

Numerous flow channels. Same meshing problem as for heat exchangers.

Authors have developed original stack model.

System treated as ‘sandwich’ of four materials; air, fuel, electrolyte (including electrodes) and interconnect.

Idealised geometry: All fluid and solid regions simple rectangular-shaped zones; planar ducts - Allowed for comparison with detailed model for SOFC stack.

Single-cell and 10 cell stack considered: Fuel/air in cross flow.

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SOLID OXIDE FUEL CELL

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THERMODYNAMICS

Nernst potential, E, given by

When current flows, actual potential, V, is lower,

i’’ current density (A/m2), are ‘overpotentials’, re is electrolyte resistance All lumped together as a internal resistance, r.

Goal to develop DRA model for SOFC stack design. Detailed numerical model (DNM) used to validate model

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THEORY

General form:

(i) Transient, (ii) convection, (iii) inter-phase transfer, (iv) diffusion or within phase transfer, and (v) source.

1. Continuity:

Mass sources computed from Faraday’s law. Coded as volumetric sources.

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THEORY

2. Momentum:

F is ‘distributed resistance’. If then .

Viscous terms in zero fluids, F is zero in manifolds.

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THEORY

3. Heat transfer

Heat sources due to Joule and Peltier effects. Two terms combined as single volumetric term .

Heat transfer coefficient

Mass transfer effects accounted for by using

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THEORY

4. Mass transfer

Mass sources/sinks ‘T-state’ value.

Wall (not bulk) values are needed for Nernst equation

Mass transfer driving force for 1-D convection/diffusion

Blowing parameter

g* is conductance zero mass transfer

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13

MUSES method

Multiply-shared Space method. Separate spaces for each material. Porosities used (except manifolds). Inter-phase values fetched across structured rectilinear mesh.

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Implementation

FORTRAN code inPLANTed in PHOENICS code:

PATCH (fu2el,VOLUME,NI1,NI2,NJ1,NJ2,NK1,NK2,1,LSTEP)

<SORC01> VAL=TEM1[,,+:FTOE:]

COVAL(fu2el,TEM1,GRND,GRND)

IF(INDVAR.EQ.INAME('TEM1 ').AND.NPATCH.EQ.'FU2EL ') THEN

LFVAL =L0F(VAL)

LFTEM1=L0F(INAME('TEM1 '))

DO 13801 IX=IXF ,IXL

IADD=NY*(IX-1)

DO 13801 IY=IYF ,IYL

I=IY+IADD

L0TEM1=LFTEM1+I

13801 F(LFVAL+I)=F(L0TEM1+NFM*42)

ENDIF

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COMPUTE ALGORTHM

1. Solve transport equations.

2. Solve Nernst potential,

3. Compute values for cell resistance, r, and heat and mass sources/sinks.

4. Repeat steps 1-3 until convergence is obtained.

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VOLTAGE ‘CORRECTION’

Both galvanostatic and potentiostatic situations occur. For former adjust voltage iteratively until the desired current reached.

V* is V-value of at previous iteration and is a voltage correction is desired current density. This step arguably redundant (can compute cell voltage from mean current density direct)

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DETAILED NUMERICAL MODEL (DNM)

Used for comparison. Rate eqns. not assumed in DNM. Fine mesh. No volume averaging.

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SINGLE CELL RESULTS :Current density

Both cell temperature and Nernst potential affect the current density since

r is inversely proportional to temperature

DRA DNM

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Nernst Potential

Nernst potential more influenced by H2 and H2O mass factions than by O2, due to the stoichiometry. E decreases as concentrations of O2 and H2 decrease and H2O increase from inlet to outlet.

DRA DNM

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Temperature

Temperature variations are inevitable: If heat production uniform, maximum would be at top-right corner.

Since both E and i’’ are maximum at top-left; peak shifts

Metallic interconnect serves as a thermal fin

DRA DNM

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Anode wall H2 mass fraction

H2 contours nominally perpendicular to, and decreasing along fuel streamlines

NB: DRA values wall values

DRA DNM

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Anode wall H2O mass fraction

Good agreement between methodologies.

DRA DNM

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Cathode wall O2 mass fraction

Current density identical at anode/cathode (thin electrolyte), so source terms of H2, H2O and O2 coupled, and mass fraction contours skewed, more pronounced at high current densities.

DRA DNM

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10-CELL STACK RESULTS: Air side velocity vectors

Fine detail of motion lost,

Characteristic parabolic-shaped (DNM) velocity profile associated with fluid flow in planar ducts absent from DRA

Manifold-stack assembly ‘well designed’ pressure/velocity fields uniform: Manifolds losses small compared to cell.

2A/m0004'' i

DRA DNM

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Air side pressure

Pressure fields in close agreement.

Problems can arise in large stacks, where mass transfer into results in stack pressure gradient decreasing upwards. results in variations in flow field. Minimised by ensuring cell passages small in comparison manifolds.

DRA DNM

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Air side bulk O2 mass fraction

O2 mass fractions constant from cell-to-cell. Good agreement between methodologies. NB: DRA values bulk values,

Significant variation across micro-channels; maximum for high current density (short circuit, V  0) ‘diffusion limit’; mass transfer rate-limiting factor. Important that wall values obtained to avoid over-prediction of Nernst potential from bulk values

DRA DNM

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Temperature

‘Zig-zag’ temperature field in DNM

Secondary thermal distribution due to ‘ordering of fluids’

Occurs even if heating perfectly uniform and flow constant

DRA DNM

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DISCUSSION

Problem: In original DRA secondary thermal effects lost, due to volume-averaging.

Solution:

Computational cells in z direction coincided with actual fuel cells. Inter-phase heat transfer terms computed as pairs eg.

air-electrolyte pair, Similarly treatment for air-interconnect, fuel-interconnect but for fuel-to-electrolyte pair sources computed as.

Recovered ‘ordering of streams’

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DISCUSSION

Complex interaction between physical chemistry and transport phenomena; subject known as ‘physical-chemical hydrodynamics’

Voltage correction algorithm converged provided a reasonable initial guess is made.

If V-i’’ curve is linear, and r is actual resistance, correct cell value predicted after 1 iteration: In practice V-i’’ curve non-linear and r only an estimate

Advantage voltage-correction approach, is r need not be exact,

Alternative can compute the average resistance and current density by integration, and hence obtain voltage. Same result is obtained.

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DISCUSSION

PLANT/IMMERSOL good for ‘in-line’ programming, but need way to nest multi-line commands e.g. using curly braces {} or the like.

In some aspects (eg voltage correction) PLANT is a little clumsy. (Compromise)

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CONCLUSIONS

Most CFD vendors developing single cell models which cannot be scaled to stack level

We developed first CFD stack-level model

Excellent agreement between DRA and DNM results

Substitution of appropriate values for and F leads to reasonable results at fraction of cost

1-D mass transfer analysis yields wall mass fractions in agreement with detailed calculations even when significant variations in mw and mb

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steven.beale@nrc.ca

svz@flowsolve.com