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Add process block example notebooks: CSTR, heat exchanger, flash drum and distillation
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‎docs/source/examples/cstr_reaction.ipynb‎

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{
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"cells": [
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"# Continuous Stirred-Tank Reactor\n",
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"\n",
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"Simulating the startup transient of an exothermic first-order reaction in a cooled CSTR, showing the dynamic interaction between concentration decay and temperature rise."
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"The CSTR model couples a material balance with an energy balance. For a first-order irreversible reaction $A \\to \\text{products}$ with Arrhenius kinetics:\n",
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"\n",
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"$$\\frac{dC_A}{dt} = \\frac{C_{A,\\text{in}} - C_A}{\\tau} - k(T)\\, C_A$$\n",
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"\n",
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"$$\\frac{dT}{dt} = \\frac{T_\\text{in} - T}{\\tau} + \\frac{(-\\Delta H_\\text{rxn})}{\\rho\\, C_p}\\, k(T)\\, C_A + \\frac{UA}{\\rho\\, C_p\\, V}\\,(T_c - T)$$\n",
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"\n",
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"where $k(T) = k_0 \\exp(-E_a / RT)$ and $\\tau = V/F$ is the residence time."
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]
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": [
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"import matplotlib.pyplot as plt\n",
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"\n",
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"from pathsim import Simulation, Connection\n",
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"from pathsim.blocks import Source, Scope\n",
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"\n",
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"from pathsim_chem.process import CSTR"
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"Configure the reactor with parameters typical of an exothermic liquid-phase reaction. The reactor starts empty ($C_A = 0$) at ambient temperature and is fed with a concentrated stream."
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]
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": "cstr = CSTR(\n V=1.0, # reactor volume [m³]\n F=0.05, # volumetric flow rate [m³/s] -> tau = 20 s\n k0=1e6, # pre-exponential factor [1/s]\n Ea=40000.0, # activation energy [J/mol]\n n=1.0, # first-order reaction\n dH_rxn=-40000.0, # exothermic [J/mol]\n rho=1000.0, # density [kg/m³]\n Cp=4184.0, # heat capacity [J/(kg·K)]\n UA=800.0, # cooling jacket [W/K]\n C_A0=0.0, # start empty\n T0=300.0, # initial temperature [K]\n)"
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": "Feed a constant concentration of 1000 mol/m³ at 320 K, with the coolant held at 290 K. A `Scope` records both the outlet concentration and temperature."
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": "# Constant feed and coolant conditions\nC_feed = Source(func=lambda t: 1000.0) # feed concentration [mol/m³]\nT_feed = Source(func=lambda t: 320.0) # feed temperature [K]\nT_cool = Source(func=lambda t: 290.0) # coolant temperature [K]\n\nscp = Scope(labels=[\"C_A [mol/m³]\", \"T [K]\"])\n\nsim = Simulation(\n blocks=[C_feed, T_feed, T_cool, cstr, scp],\n connections=[\n Connection(C_feed, cstr), # C_in -> port 0\n Connection(T_feed, cstr[1]), # T_in -> port 1\n Connection(T_cool, cstr[2]), # T_c -> port 2\n Connection(cstr, scp), # C_out -> scope port 0\n Connection(cstr[1], scp[1]), # T_out -> scope port 1\n ],\n dt=0.1,\n)\n\nsim.run(200)"
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": [
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"time, signals = scp.read()\n",
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"\n",
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"fig, (ax1, ax2) = plt.subplots(1, 2, figsize=(12, 5))\n",
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"\n",
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"ax1.plot(time, signals[0])\n",
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"ax1.set_xlabel(\"Time [s]\")\n",
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"ax1.set_ylabel(\"Concentration [mol/m³]\")\n",
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"ax1.set_title(\"Outlet Concentration\")\n",
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"ax1.grid(True, alpha=0.3)\n",
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"\n",
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"ax2.plot(time, signals[1])\n",
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"ax2.set_xlabel(\"Time [s]\")\n",
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"ax2.set_ylabel(\"Temperature [K]\")\n",
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"ax2.set_title(\"Reactor Temperature\")\n",
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"ax2.grid(True, alpha=0.3)\n",
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"\n",
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"plt.tight_layout()\n",
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"plt.show()"
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"The reactor starts cold and empty. As fresh feed enters, concentration rises initially but then the Arrhenius kinetics kick in — the exothermic reaction heats the fluid, which accelerates the rate, consuming more reactant. The cooling jacket prevents thermal runaway and the system settles to a steady state where reaction rate balances the feed."
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]
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}
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],
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"metadata": {
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"kernelspec": {
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"display_name": "Python 3",
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"language": "python",
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"name": "python3"
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},
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"language_info": {
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"name": "python",
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"version": "3.11.0"
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}
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},
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"nbformat": 4,
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"nbformat_minor": 4
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}

‎docs/source/examples/flash_distillation.ipynb‎

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{
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"cells": [
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"# Flash Drum and Distillation Column\n",
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"\n",
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"Simulating two fundamental separation processes: an isothermal binary flash drum and a multi-tray distillation column built from individual `DistillationTray` blocks wired in series."
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"## Part 1: Isothermal Flash Drum\n",
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"\n",
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"A flash drum separates a liquid feed into vapor and liquid streams using vapor-liquid equilibrium (VLE). The drum uses Raoult's law with Antoine correlations to compute K-values:\n",
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"\n",
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"$$K_i = \\frac{P^\\text{sat}_i(T)}{P}$$\n",
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"\n",
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"The Rachford-Rice equation determines the vapor fraction $\\beta$, from which the vapor ($y_i$) and liquid ($x_i$) compositions follow."
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]
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": [
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"import matplotlib.pyplot as plt\n",
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"\n",
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"from pathsim import Simulation, Connection\n",
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"from pathsim.blocks import Source, Scope\n",
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"\n",
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"from pathsim_chem.process import FlashDrum, DistillationTray"
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": "Configure a flash drum for a benzene-toluene mixture (default Antoine coefficients). Feed an equimolar mixture at 1 atm and sweep temperature from 340 K to 400 K. This range covers the bubble point (~365 K) and dew point (~380 K) of the mixture, so we can observe the transition from all-liquid to two-phase to all-vapor."
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": "flash = FlashDrum(holdup=100.0) # default benzene/toluene Antoine params\n\n# Feed: 10 mol/s, equimolar (z1 = 0.5), 1 atm\nF_src = Source(func=lambda t: 10.0)\nz_src = Source(func=lambda t: 0.5)\nT_src = Source(func=lambda t: 340.0 + t * 0.5) # ramp 340 -> 400 K\nP_src = Source(func=lambda t: 101325.0)\n\nscp = Scope(labels=[\"V_rate\", \"L_rate\", \"y_1 (benzene)\", \"x_1 (benzene)\"])\n\nsim = Simulation(\n blocks=[F_src, z_src, T_src, P_src, flash, scp],\n connections=[\n Connection(F_src, flash), # F -> port 0\n Connection(z_src, flash[1]), # z_1 -> port 1\n Connection(T_src, flash[2]), # T -> port 2\n Connection(P_src, flash[3]), # P -> port 3\n Connection(flash, scp), # V_rate -> scope 0\n Connection(flash[1], scp[1]), # L_rate -> scope 1\n Connection(flash[2], scp[2]), # y_1 -> scope 2\n Connection(flash[3], scp[3]), # x_1 -> scope 3\n ],\n dt=0.5,\n)\n\nsim.run(120)"
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": "time, signals = scp.read()\nT_sweep = 340.0 + time * 0.5\n\nfig, (ax1, ax2) = plt.subplots(1, 2, figsize=(12, 5))\n\nax1.plot(T_sweep, signals[0], label=\"Vapor rate\")\nax1.plot(T_sweep, signals[1], label=\"Liquid rate\")\nax1.set_xlabel(\"Temperature [K]\")\nax1.set_ylabel(\"Flow rate [mol/s]\")\nax1.set_title(\"Flash Drum Flow Rates\")\nax1.legend()\nax1.grid(True, alpha=0.3)\n\nax2.plot(T_sweep, signals[2], label=r\"$y_1$ (vapor)\")\nax2.plot(T_sweep, signals[3], label=r\"$x_1$ (liquid)\")\nax2.axhline(0.5, color=\"gray\", ls=\"--\", alpha=0.4, label=\"Feed\")\nax2.set_xlabel(\"Temperature [K]\")\nax2.set_ylabel(\"Mole fraction (benzene)\")\nax2.set_title(\"VLE Compositions\")\nax2.legend()\nax2.grid(True, alpha=0.3)\n\nplt.tight_layout()\nplt.show()"
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"As temperature increases, more liquid vaporizes (higher vapor rate). The vapor is enriched in the lighter component (benzene), while the liquid becomes richer in toluene — the classic VLE separation."
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"## Part 2: Distillation Column (5 Trays)\n",
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"\n",
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"A distillation column is built by wiring multiple `DistillationTray` blocks in series. Each tray enforces vapor-liquid equilibrium with a constant relative volatility $\\alpha$:\n",
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"\n",
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"$$y = \\frac{\\alpha\\, x}{1 + (\\alpha - 1)\\, x}$$\n",
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"\n",
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"Under constant molar overflow (CMO), liquid flows down and vapor flows up with constant rates $L$ and $V$. We feed the column at the middle tray."
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]
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": [
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"# Column parameters\n",
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"N_trays = 5\n",
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"alpha = 2.5 # relative volatility\n",
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"L = 5.0 # liquid flow rate [mol/s]\n",
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"V = 5.0 # vapor flow rate [mol/s]\n",
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"x_feed = 0.5 # feed composition (light component)\n",
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"\n",
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"# Create tray blocks (all start at x = 0.5)\n",
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"trays = [DistillationTray(M=1.0, alpha=alpha, x0=0.5) for _ in range(N_trays)]\n",
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"\n",
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"# Liquid feed from condenser (enters tray 0 from above)\n",
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"L_src = Source(func=lambda t: L)\n",
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"x_top = Source(func=lambda t: 0.95) # reflux composition (nearly pure light)\n",
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"\n",
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"# Vapor feed from reboiler (enters tray N-1 from below)\n",
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"V_src = Source(func=lambda t: V)\n",
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"y_bot = Source(func=lambda t: 0.05) # reboiler vapor (nearly pure heavy)\n",
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"\n",
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"# Record composition on each tray\n",
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"scp = Scope(labels=[f\"Tray {i+1}\" for i in range(N_trays)])"
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"Wire the trays: liquid cascades downward (tray $i$ liquid output $\\to$ tray $i+1$ liquid input), vapor rises upward (tray $i$ vapor output $\\to$ tray $i-1$ vapor input). External feeds enter the top and bottom."
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]
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": [
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"connections = []\n",
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"\n",
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"# Top tray (0): liquid from reflux\n",
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"connections.append(Connection(L_src, trays[0])) # L_in -> port 0\n",
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"connections.append(Connection(x_top, trays[0][1])) # x_in -> port 1\n",
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"\n",
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"# Bottom tray (N-1): vapor from reboiler\n",
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"connections.append(Connection(V_src, trays[-1][2])) # V_in -> port 2\n",
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"connections.append(Connection(y_bot, trays[-1][3])) # y_in -> port 3\n",
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"\n",
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"# Inter-tray connections\n",
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"for i in range(N_trays - 1):\n",
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" # Liquid flows down: tray i -> tray i+1\n",
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" connections.append(Connection(trays[i], trays[i+1])) # L_out -> L_in\n",
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" connections.append(Connection(trays[i][1], trays[i+1][1])) # x_out -> x_in\n",
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"\n",
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" # Vapor flows up: tray i+1 -> tray i\n",
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" connections.append(Connection(trays[i+1][2], trays[i][2])) # V_out -> V_in\n",
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" connections.append(Connection(trays[i+1][3], trays[i][3])) # y_out -> y_in\n",
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"\n",
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"# Connect each tray's liquid composition to scope\n",
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"for i, tray in enumerate(trays):\n",
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" connections.append(Connection(tray[1], scp[i])) # x_out -> scope\n",
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"\n",
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"sim = Simulation(\n",
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" blocks=[L_src, x_top, V_src, y_bot, *trays, scp],\n",
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" connections=connections,\n",
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" dt=0.05,\n",
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")\n",
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"\n",
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"sim.run(30)"
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]
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},
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{
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"cell_type": "code",
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"execution_count": null,
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"metadata": {},
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"outputs": [],
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"source": [
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"time, signals = scp.read()\n",
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"\n",
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"fig, (ax1, ax2) = plt.subplots(1, 2, figsize=(12, 5))\n",
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"\n",
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"# Dynamic tray composition evolution\n",
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"for i in range(N_trays):\n",
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" ax1.plot(time, signals[i], label=f\"Tray {i+1}\")\n",
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"ax1.set_xlabel(\"Time [s]\")\n",
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"ax1.set_ylabel(r\"$x$ (light component)\")\n",
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"ax1.set_title(\"Tray Compositions Over Time\")\n",
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"ax1.legend()\n",
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"ax1.grid(True, alpha=0.3)\n",
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"\n",
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"# Steady-state composition profile\n",
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"x_profile = [tray.engine.state[0] for tray in trays]\n",
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"tray_nums = list(range(1, N_trays + 1))\n",
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"\n",
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"ax2.plot(tray_nums, x_profile, \"o-\", markersize=8)\n",
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"ax2.set_xlabel(\"Tray number (top to bottom)\")\n",
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"ax2.set_ylabel(r\"$x$ (light component)\")\n",
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"ax2.set_title(\"Composition Profile (Steady State)\")\n",
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"ax2.grid(True, alpha=0.3)\n",
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"\n",
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"plt.tight_layout()\n",
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"plt.show()"
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]
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},
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{
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"cell_type": "markdown",
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"metadata": {},
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"source": [
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"The column separates the light and heavy components across its trays. The top tray is enriched in the light component (high $x$) while the bottom tray is depleted. The steady-state composition profile shows the characteristic staircase that a McCabe-Thiele diagram would predict for this relative volatility."
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]
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}
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],
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"metadata": {
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"kernelspec": {
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"display_name": "Python 3",
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"language": "python",
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"name": "python3"
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},
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"language_info": {
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"name": "python",
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"version": "3.11.0"
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}
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},
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"nbformat": 4,
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"nbformat_minor": 4
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}

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