modelSMRSystem_noH2Loop
Steam methane reformer system with sufficient H2 in feed containing prereformer, SMR, WGS, dryer, PSA and heat exchangers
Information
1. Purpose of model
This model represents typical setup of a steam methane reformer system with enough hydrogen in the feed.
2. Level of detail, physical effects considered, and physical insight
The feed is preheated, mixed with preheated steam and the higher hydrocarbons are decomposed. Thereafter, the steam methane reformer produces hydrogen out of methane and steam. Afterwards, the hydrogen yield is increased in the water gas shift reactor. In the end, the stream is cooled, dried and purified in a
pressure swing adsorption reactor (PSA). In a real system there are many more heat exchangers but most of the models work simplified and thus independent of the temperature. Necessary for this process is heat for the preheaters and the steam methane reformer which is usually delivered by a burner in which the PSA off-
gas is burned.
3. Limits of validity
The model is valid if there is enough hydrogen in the stream. The applicability of the submodels should be checked as well before using this model.
4. Interfaces
gasPortIn: real gas inlet
gasPortOut_offGas: real gas outlet for the PSA off-gas
gasPortOut_hydrogen: real gas outlet for the produced hydrogen
heatFeedPreheater: heat port for the feed preheater
heatSteamPreheater: heat port for the steam preheater
heatSMR: heat port for the steam methane reformer
5. Nomenclature
(no elements)
6. Governing Equations
(no remarks)
7. Remarks for Usage
(no remarks)
8. Validation
Tested in check models "TransiEnt.Producer.Gas.SteamMethaneReformerSystem.Check.TestSMRSystem_noH2Loop" and "TransiEnt.Producer.Gas.SteamMethaneReformerSystem.Check.TestSMRSystem_noH2Loop"
9. References
(no remarks)
10. Version History
Model created by Carsten Bode (c.bode@tuhh.de) in March 2017
Model revised by Carsten Bode (c.bode@tuhh.de) in Apr 2018 (fixed for update to ClaRa 1.3.0)
Parameters
| Type | Name | Default | Description |
|---|---|---|---|
| TransiEnt.Basics.Types.TypeOfResource | typeOfResource | TransiEnt.Basics.Types.TypeOfResource.Consumer | Type of energy resource for global model statistics |
| TransiEnt.Basics.Media.Gases.VLE_VDIWA_NG7_SG_var | realGas_ng7_sg | ||
| TransiEnt.Basics.Media.Gases.VLE_VDIWA_SG6_var | realGas_sg6 | ||
| TransiEnt.Basics.Media.Gases.Gas_VDIWA_SG6_var | idealGas_sg6 | ||
| TILMedia.VLEFluidTypes.TILMedia_SplineWater | water | ||
| Boolean | integrateMassFlowSink | false | True if mass flow rate of the sink shall be integrated |
| Boolean | integrateMassFlowSource | false | True if mass flow rate of the source shall be integrated |
| Heat Exchangers | |||
| SI.Temperature | T_preheat | 864.18 | Temperature to which the gas mixture and the steam are preheated before the prereformer |
| SI.Temperature | T_SG_HEX_out | 293.15 | Temperature to which the syngas is cooled down in the water/sg heat exchanger |
| SI.PressureDifference | Delta_p_HEX_feed | 0 | Pressure loss in the feed preheater |
| SI.PressureDifference | Delta_p_HEX_water | 0 | Pressure loss in the water preheater |
| SI.PressureDifference | Delta_p_HEX_waterSG_water | 0 | Pressure loss in the water/sg heat exchanger on the water side |
| SI.PressureDifference | Delta_p_HEX_waterSG_SG | 0 | Pressure loss in the water/sg heat exchanger on the SG side |
| Steam Junction | |||
| SI.Volume | volume_junction | 0.01 | Volume of the junction of feed and water |
| Boolean | steamToCarbonRatioFromTable | false | true if table data is used for the steam to carbon ratio |
| TransiEnt.Basics.Tables.DataPrivacy | datasourceSteamToCarbonRatio | TransiEnt.Basics.Tables.DataPrivacy.isPublic | Source of table data |
| String | relativepathSteamToCarbonRatio | "gas/SteamToCarbonRatioExampleTimeseries.txt" | Path relative to source directory |
| Boolean | use_absolute_path_SteamToCarbonRatio | false | Should only be used for testing purposes |
| String | absolute_path_SteamToCarbonRatio | "" | |
| Prereformer | |||
| SI.PressureDifference | Delta_p_prereformer | 3e5 | Pressure loss in the prereformer |
| Steam methane reformer › Fundamental Definitions | |||
| Integer | N_cv_SMR | 1 | Number of control volumes in the SMR |
| SI.Efficiency[N_cv_SMR,3] | eff_SMR | fill({0.019, 0.015, 0.021}, N_cv_SMR) | Effectiveness factors for the reactions |
| SI.PressureDifference | Delta_p_SMR | 2.3e5 | Total pressure loss over the reactor |
| Integer | pressureCalculation_SMR | 2 | Method of pressure calculation |
| Steam methane reformer › Geometry | |||
| Real | N_tube_SMR | 176 | Number of tubes |
| SI.Diameter | dia_tube_i_SMR | 0.0795 | Inner tube diameter |
| SI.Diameter | dia_tube_o_SMR | 0.1020 | Outer tube diameter |
| SI.Diameter | dia_part_SMR | 0.0174131 | Equivalent pellet diameter |
| SI.Length | l_SMR | 11.95 | Length of reactor |
| Steam methane reformer › Catalyst | |||
| SI.VolumeFraction | eps_bed_SMR | 0.605 | Bed porosity |
| SI.VolumeFraction | eps_cat_SMR | 0.51963 | Catalyst porosity |
| SI.Density | d_cat_SMR | 2396.965 | Density of catalyst particle |
| SI.Density | d_bed_SMR | d_cat_SMR*(1 - eps_bed_SMR) | Density of fixed-bed |
| SI.SpecificHeatCapacity | cp_cat_SMR | 949.72 | Specific heat capacity of catalyst |
| Steam methane reformer › Heat Transfer | |||
| SI.Area | A_refractor_SMR | 1164*N_tube_SMR/176 | Surface area of refractor |
| SI.Area | A_flame_SMR | 0.01 | Surface area of a flame of one burner |
| SI.Emissivity | em_gas_SMR | 0.1 | Emissivity of furnace gas |
| SI.Emissivity | em_flame_SMR | 0.1 | Emissivity of flames |
| SI.Emissivity | em_tube_SMR | 0.95 | Emissivity of reformer tubes |
| SI.Temperature | T_adi_SMR | 2200 | Adiabatic flame temperature |
| Real | N_burner_SMR | 112*N_tube_SMR/176 | Number of burners |
| Steam methane reformer › Nominal Values | |||
| SI.Temperature[N_cv_SMR] | T_nom_SMR | (820.574 + 273.15)*ones(N_cv_SMR) | Nominal gas and catalyst temperature in the control volumes of the SMR |
| SI.Pressure[N_cv_SMR] | p_nom_SMR | 24.338e5*ones(N_cv_SMR) | Nominal pressure in the control volumes of the SMR |
| SI.MassFraction[N_cv_SMR,5] | xi_nom_SMR | fill({0.0319, 0.1893, 0.6089, 0.0575, 0.1073}, N_cv_SMR) | Nominal values for mass fractions in the control volumes of the SMR |
| Initialization › Junction | |||
| Integer | initOption_junction | 201 | InitOption of the junction of feed and water |
| SI.SpecificEnthalpy | h_start_junction | 2.13667e6 | Initial specific enthalpy in the junction of feed and water |
| SI.Pressure | p_start_junction | 29e5 | Initial pressure in the junction of feed and water |
| SI.MassFraction[8] | xi_start_junction | {0.0961314, 0.0185838, 0.00918786, 0.034747, 0.00354792, 0.00311627, 0.821655, 0} | Initial mass fractions in the junction of feed and water |
| Initialization › Steam Methane Reformer | |||
| SI.Temperature[N_cv_SMR] | T_start_SMR | (820.574 + 273.15)*ones(N_cv_SMR) | Initial gas and catalyst temperature in the control volumes of the SMR |
| SI.Pressure[N_cv_SMR] | p_start_SMR | 24.338e5*ones(N_cv_SMR) | Initial pressure in the control volumes of the SMR |
| SI.MassFraction[N_cv_SMR,5] | xi_start_SMR | fill({0.0319, 0.1893, 0.6089, 0.0575, 0.1073}, N_cv_SMR) | Initial values for mass fractions in the SMR |
| Water Gas Shift Reactor | |||
| SI.PressureDifference | Delta_p_WGS | 3.5e5 | Pressure loss in the water gas shift reactor |
| Real | conversionRate_WGS | 0.97 | CO conversion rate in the water gas shift reactor |
| Gas Cleaning | |||
| SI.PressureDifference | Delta_p_dryer | 0 | Pressure loss in the dryer |
| SI.PressureDifference | Delta_p_PSA | 0.2e5 | Pressure loss in the pressure swing adsorption (on the H2 side) |
| SI.Efficiency | eta_H2_PSA | 0.8 | Efficiency of the hydrogen separation in the pressure swing adsorption |
| Water Supply | |||
| SI.Efficiency | eta_mech_pump_H2O | 0.97 | Mechanical efficiency of the water pump |
| SI.Efficiency | eta_el_pump_H2O | 0.98 | Electrical efficiency of the water pump |
| SI.Pressure | p_H2O_in | 1e5 | Inlet pressure of the water supply |
| SI.Temperature | T_H2O_in | 293.15 | Inlet temperature of the water supply |
| Statistics | |||
| SI.EnthalpyFlowRate | H_flow_H2_n | 1e6 | Nominal hydrogen enthalpy flow rate leaving the system |
| Demand-related Cost | |||
| TransiEnt.Basics.Units.MonetaryUnitPerEnergy | Cspec_demAndRev_el | simCenter.Cspec_demAndRev_free | Specific demand-related cost per electric energy |
| Real | Cspec_demAndRev_other_water | simCenter.Cspec_demAndRev_other_free | Specific cost per cubic meter water |
| Summary | |||
| Boolean | useFluidModelsForSummary | false | True, if fluid models shall be used for the summary |
Connectors
| Type | Name | Default | Description |
|---|---|---|---|
| TransiEnt.Basics.Interfaces.Gas.RealGasPortIn | gasPortIn | ||
| TransiEnt.Basics.Interfaces.Gas.RealGasPortOut | gasPortOut_offGas | ||
| TransiEnt.Basics.Interfaces.Gas.RealGasPortOut | gasPortOut_hydrogen | ||
| TransiEnt.Basics.Interfaces.General.MassFlowRateOut | massflow_H2_out | ||
| Modelica.Thermal.HeatTransfer.Interfaces.HeatPort_b | heatFeedPreheater | ||
| Modelica.Thermal.HeatTransfer.Interfaces.HeatPort_b | heatSteamPreheater | ||
| Modelica.Thermal.HeatTransfer.Interfaces.HeatPort_b | heatSMR |
Components
| Type | Name | Default | Description |
|---|---|---|---|
| TransiEnt.SimCenter | simCenter | ||
| TransiEnt.ModelStatistics | modelStatistics | ||
| Summary | summary | ||
| Real | expressionSteamToCarbonRatio | 4.8 | Desired molar ratio of H2O to C for the steam controller |
| SI.Mass | source_H2O_m | Mass from the water source | |
| SI.Mass | sink_H2O_m | Mass into the water sink | |
| Modelica.Blocks.Sources.RealExpression | realExpression | ||
| Modelica.Blocks.Logical.Switch | switch1 | ||
| Modelica.Blocks.Sources.BooleanExpression | booleanExpression | ||
| Basics.Tables.GenericDataTable | tableSteamToCarbonRatio |
Contents
| Name | Description |
|---|---|
 CostSpecsGeneral | |
 ControllerH2OForReformer | |
 Outlineprotected | |
 MolarDryCompositionsprotected | |
 HeatSMRprotected | |
 Summaryprotected |