https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&feed=atom&action=historyPressure changer - Revision history2024-03-28T17:27:04ZRevision history for this page on the wikiMediaWiki 1.39.2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4583&oldid=prevKedricdaly2: Updated "date presented" to final due date2016-02-21T21:33:11Z<p>Updated "date presented" to final due date</p>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4581&oldid=prevKedricdaly2: Other pressure changers and slight summary modification and internal link modifications2016-02-21T21:29:22Z<p>Other pressure changers and slight summary modification and internal link modifications</p>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>Pumps do work on fluids, causing them to increase in pressure at a constant volume, due to the assumption that liquids that enter pumps are mostly incompressible. For more information on different types of pumps<del style="font-weight: bold; text-decoration: none;"> and other pressure changers</del>, see [[Process hydraulics]].</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>=Compressors=</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>For background on different types of compressors, see [[Process hydraulics]]. Typically centrifugal compressors are used for compressing higher volumes of gas to moderate pressures, whereas positive-displacement compressors are use for compressing low volumes to high pressures.<ref name="Turton"/></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>For background on different types of compressors, see [[Process hydraulics<ins style="font-weight: bold; text-decoration: none;">|Compressors</ins>]]. Typically centrifugal compressors are used for compressing higher volumes of gas to moderate pressures, whereas positive-displacement compressors are use for compressing low volumes to high pressures.<ref name="Turton"/></div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Centrifugal compressors are similar to centrifugal pumps, with the major difference being the fluid going into the compressors are compressible. <ref name="Turton"/> This fact makes the math behind modeling compressors more complex than for pumps where an incompressible fluid assumption is made. There are still similarities however, in that a performance curve is often provided by the manufacturer so that outlet pressure can be related to inlet pressure and flow rates. One major difference between pump and compressor performance curves is that compressor performance curves deal with a pressure ratio, rather than a pressure difference, and a surge line is often included as well. <ref name="Turton"/> The surge line is important because it marks the point where a lower flowrate would result in backflow, which could lead to a reversal of flow direction and would damage the compressor.<ref name="Turton"/>.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Centrifugal compressors are similar to centrifugal pumps, with the major difference being the fluid going into the compressors are compressible. <ref name="Turton"/> This fact makes the math behind modeling compressors more complex than for pumps where an incompressible fluid assumption is made. There are still similarities however, in that a performance curve is often provided by the manufacturer so that outlet pressure can be related to inlet pressure and flow rates. One major difference between pump and compressor performance curves is that compressor performance curves deal with a pressure ratio, rather than a pressure difference, and a surge line is often included as well. <ref name="Turton"/> The surge line is important because it marks the point where a lower flowrate would result in backflow, which could lead to a reversal of flow direction and would damage the compressor.<ref name="Turton"/>.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>We can see the operating point is to the right of the surge curve, so blowback should not be a problem for these specifications. The resulting outlet stream conditions for these specifications should be 154.7 C, and 145.7 kPa.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>We can see the operating point is to the right of the surge curve, so blowback should not be a problem for these specifications. The resulting outlet stream conditions for these specifications should be 154.7 C, and 145.7 kPa.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>[[File:PC_valve_converged.PNG|thumb|A converged valve in HYSYS]]</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>When modeling valves in HYSYS, they also require an inlet and outlet stream, the same as pumps and compressors, but do not require a duty stream. For steady state simulation, as long as a pressure drop is specified along in some form, the valve should converge. This can be done by specifying inlet and outlet pressures (and other conditions required for stream convergence), or by specifying the pressure drop across the valve and the inlet or outlet pressure, although inlet pressure is preferred in most cases because then HYSYS does not need to try and backward solve for the inlet pressure in complicated systems.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div><br/></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Even piping itself can change the pressure of a stream due to viscous losses. When modeling a process, it is often best to initially estimate this based on pipe length and any fittings the piping will need, by using relations that can be found in the table below in equations found in [[Process hydraulics|Pressure Drop in Pipes]], taken from Towler. <ref name="Towler"/> When final instrumentation drawings are completed for the process, ore rigorous hydraulic calculations should be completed to ensure there is enough pressure head throughout the process.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>When modeling pressure changers with computer software, it is important to not over-specify them, as for any other piece of equipment. Failing to include them in the final process simulation may lead to odd results, such as a negative pressure drop through a heater or cooler in order to meet pressure or temperature specifications on a material stream. Should this situation occur, a pump or compressor should be added to ensure that a physically possible pressure drop takes place in the processing equipment. Pumps and compressors will use electricity to perform their pressure changes, and if many pumps or a large compressor is used in the process, this can have impacts on the process economics, so it is important to model pressure changers when designing a chemical process.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>When modeling pressure changers with computer software, it is important to not over-specify them, as for any other piece of equipment. Failing to include them in the final process simulation may lead to odd results, such as a negative pressure drop through a heater or cooler in order to meet pressure or temperature specifications on a material stream. Should this situation occur, a pump or compressor should be added to ensure that a physically possible pressure drop takes place in the processing equipment. Pumps and compressors will use electricity to perform their pressure changes, and if many pumps or a large compressor is used in the process, this can have impacts on the process economics, so it is important to model pressure changers when designing a chemical process<ins style="font-weight: bold; text-decoration: none;">. Estimates for piping and valves also need to be included in the simulation so that proper pressure heads are maintained throughout the process simulation</ins>.</div></td>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4572&oldid=prevKedricdaly2: /* Modeling Compressors with HYSYS */2016-02-21T20:26:52Z<p><span dir="auto"><span class="autocomment">Modeling Compressors with HYSYS</span></span></p>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>{|</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>{|</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>|[[File:PC_compressor_add_surge_curve.PNG]]||[[File:PC_compressor_surge_curve_data.PNG]]</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>|[[File:PC_compressor_add_surge_curve.PNG<ins style="font-weight: bold; text-decoration: none;">|500px</ins>]]||[[File:PC_compressor_surge_curve_data.PNG]]</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>|}</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div></center></div></td>
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<td class="diff-marker" data-marker="+"></td>
<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td class="diff-marker" data-marker="+"></td>
<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>The resulting plot makes it easy to see whether or not an operating point is above the surge line in order to ensure blowback does not occur.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>[[File:PC_compressor_perf_curve_with_surge.PNG|center|500px]]</div></td>
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<td class="diff-marker" data-marker="+"></td>
<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>We can see the operating point is to the right of the surge curve, so blowback should not be a problem for these specifications. The resulting outlet stream conditions for these specifications should be 154.7 C, and 145.7 kPa.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>=Summary=</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>=Summary=</div></td>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4566&oldid=prevKedricdaly2: /* Modeling Compressors with HYSYS */ added surge curve data2016-02-21T20:14:28Z<p><span dir="auto"><span class="autocomment">Modeling Compressors with HYSYS: </span> added surge curve data</span></p>
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<td colspan="2" style="background-color: #fff; color: #202122; text-align: center;">Revision as of 15:14, 21 February 2016</td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>After setting the compressor speed to 4900 rpm (as seen in the top right of the figure to the left, above), the inlet stream can be specified. In this example, set the temperature to 110 C, the pressure to 100 kPa, the std. ideal liq flow to 9 m<sup>3</sup>/h, and the composition of the stream to 100 water. After specifying the stream, the compressor will have enough information to converge without specifying any outlet stream conditions. This is because the performance curve relates the flow rate to the possible pressure change, and combined with information such as adiabatic pump efficiency, HYSYS can calculate any changes the pump has on the inlet stream. This type of specification is useful when you know what compressor will be used in the process design, as more accurate utility costs can be calculated.</div></td>
<td class="diff-marker"></td>
<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>After setting the compressor speed to 4900 rpm (as seen in the top right of the figure to the left, above), the inlet stream can be specified. In this example, set the temperature to 110 C, the pressure to 100 kPa, the std. ideal liq flow to 9 m<sup>3</sup>/h, and the composition of the stream to 100 water. After specifying the stream, the compressor will have enough information to converge without specifying any outlet stream conditions. This is because the performance curve relates the flow rate to the possible pressure change, and combined with information such as adiabatic pump efficiency, HYSYS can calculate any changes the pump has on the inlet stream. This type of specification is useful when you know what compressor will be used in the process design, as more accurate utility costs can be calculated.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Once data for the performance curves are input, they can also be viewed by clicking "plot curves". This can be convenient to ensure the operating point of the pump falls where the modeler wants it because the operating point of the pump is also placed on the same plot. The figure below shows the compressor curve with an additional performance curve added. The large red dot is the operating point, and it falls on the red 4900 rpm performance curve because this rpm was specified for the pump.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div><center></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>[[File:PC_compressor_curve_4900rpm.PNG|500px]]</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div></center></div></td>
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<td class="diff-marker" data-marker="+"></td>
<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td class="diff-marker" data-marker="+"></td>
<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>It is also possible to plot a surge curve on the same plot to easily ensure operation above the surge line. To do so, click on the flow limits page under the rating tab within the compressor and click the surge curve button, then input whatever data fits the surge curve for the pump.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>{|</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>=Summary=</div></td>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4556&oldid=prevKedricdaly2: /* Modeling Compressors with HYSYS */ minor capitalization2016-02-21T19:54:21Z<p><span dir="auto"><span class="autocomment">Modeling Compressors with HYSYS: </span> minor capitalization</span></p>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>After setting the compressor speed to 4900 rpm (as seen in the top right of the figure to the left, above), the inlet stream can be specified. In this example, set the temperature to 110 C, the pressure to 100 kPa, the <del style="font-weight: bold; text-decoration: none;">Std</del>. ideal liq flow to 9 m<sup>3</sup>/h, and the composition of the stream to 100 water. After specifying the stream, the compressor will have enough information to converge without specifying any outlet stream conditions. This is because the performance curve relates the flow rate to the possible pressure change, and combined with information such as adiabatic pump efficiency, HYSYS can calculate any changes the pump has on the inlet stream. This type of specification is useful when you know what compressor will be used in the process design, as more accurate utility costs can be calculated.</div></td>
<td class="diff-marker" data-marker="+"></td>
<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>After setting the compressor speed to 4900 rpm (as seen in the top right of the figure to the left, above), the inlet stream can be specified. In this example, set the temperature to 110 C, the pressure to 100 kPa, the <ins style="font-weight: bold; text-decoration: none;">std</ins>. ideal liq flow to 9 m<sup>3</sup>/h, and the composition of the stream to 100 water. After specifying the stream, the compressor will have enough information to converge without specifying any outlet stream conditions. This is because the performance curve relates the flow rate to the possible pressure change, and combined with information such as adiabatic pump efficiency, HYSYS can calculate any changes the pump has on the inlet stream. This type of specification is useful when you know what compressor will be used in the process design, as more accurate utility costs can be calculated.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>=Summary=</div></td>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4555&oldid=prevKedricdaly2: /* Modeling Compressors with HYSYS */2016-02-21T19:53:49Z<p><span dir="auto"><span class="autocomment">Modeling Compressors with HYSYS</span></span></p>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4547&oldid=prevKedricdaly2: /* Modeling Compressors with HYSYS */2016-02-21T19:28:06Z<p><span dir="auto"><span class="autocomment">Modeling Compressors with HYSYS</span></span></p>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>Likewise, specifying an inlet and outlet stream conditions will cause the compressor to converge. Another option for more specific information to be included in the simulation is by adding performance curves to the equipment. To add a performance curve, double click the compressor and go to the rating tab, then the curve page, check the "Enable Curves" check box, and then hit the add curve button.<ref name="Compressor Tutorial">N. Brownrigg. Jump start: Compressor modeling in Aspen HYSYS® Dynamics. Aspen Tech, 2015. Available at http://www.aspentech.com/compressor_modeling_jump_start.pdf Accessed 2/21/2016</ref></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Likewise, specifying an inlet and outlet stream conditions will cause the compressor to converge. Another option for more specific information to be included in the simulation is by adding performance curves to the equipment. To add a performance curve, double click the compressor and go to the rating tab, then the curve page, check the "Enable Curves" check box, and then hit the add curve button<ins style="font-weight: bold; text-decoration: none;"> and fill out the data from the table below</ins>.<ref name="Compressor Tutorial">N. Brownrigg. Jump start: Compressor modeling in Aspen HYSYS® Dynamics. Aspen Tech, 2015. Available at http://www.aspentech.com/compressor_modeling_jump_start.pdf Accessed 2/21/2016</ref></div></td>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4541&oldid=prevKedricdaly2: Changed reference punctuation2016-02-21T19:23:33Z<p>Changed reference punctuation</p>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>=Introduction=</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>Pressure changers are any piece of equipment where the main goal is to increase or decrease the pressure of a stream. Typically, pressure changers are used mostly for increasing pressure, due to the fact that pressure losses occur within a system due to friction with pipes, pipe bends, valves, and other pieces of equipment <ref name="Towler">G.P. Towler, R. Sinnott<del style="font-weight: bold; text-decoration: none;">,</del> Chemical Engineering Design: Principles, Practice and Economics of Plant and Process Design<del style="font-weight: bold; text-decoration: none;">,</del> Elsevier, 2012.</ref>. Lowering the pressure of a system can also be useful however, such as to favor the products of a chemical reaction through Le Chatelier's principle. It is important however to ensure proper pressure is maintained throughout a chemical process so that blowback does not occur, and any fluids actually reach their destination as expected, at the proper conditions.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Pressure changers are any piece of equipment where the main goal is to increase or decrease the pressure of a stream. Typically, pressure changers are used mostly for increasing pressure, due to the fact that pressure losses occur within a system due to friction with pipes, pipe bends, valves, and other pieces of equipment <ref name="Towler">G.P. Towler, R. Sinnott<ins style="font-weight: bold; text-decoration: none;">.</ins> Chemical Engineering Design: Principles, Practice and Economics of Plant and Process Design<ins style="font-weight: bold; text-decoration: none;">.</ins> Elsevier, 2012.</ref>. Lowering the pressure of a system can also be useful however, such as to favor the products of a chemical reaction through Le Chatelier's principle. It is important however to ensure proper pressure is maintained throughout a chemical process so that blowback does not occur, and any fluids actually reach their destination as expected, at the proper conditions.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div><br><br></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>There are many different types of modeling software for chemical processing, Aspen HYSYS, and Aspen Plus being well known. Like any piece of process equipment, it is necessary to specify a number of independent variables in order for the simulation to converge and produce unknown values. There are different combinations of independent variables that will suffice and cause the model to converge. Typically, the inlet and outlet pressures are specified (pressure drop, or ΔP), rather than pump duty, because these variables are important to ensure process design specifications are met.<ref name="Biegler">L.T. Biegler, I.E. Grossmann, A.W. Westerberg<del style="font-weight: bold; text-decoration: none;">,</del> Systematic Methods of Chemical Process Design<del style="font-weight: bold; text-decoration: none;">,</del> Prentice-Hall: Upper Saddle River, 1997.</ref> Different parameters of the pump or compressor can also be specified, such as efficiency, which will impact the results of the simulation. It is therefore important to ensure the equipment is correctly specified to ensure accurate results.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>There are many different types of modeling software for chemical processing, Aspen HYSYS, and Aspen Plus being well known. Like any piece of process equipment, it is necessary to specify a number of independent variables in order for the simulation to converge and produce unknown values. There are different combinations of independent variables that will suffice and cause the model to converge. Typically, the inlet and outlet pressures are specified (pressure drop, or ΔP), rather than pump duty, because these variables are important to ensure process design specifications are met.<ref name="Biegler">L.T. Biegler, I.E. Grossmann, A.W. Westerberg<ins style="font-weight: bold; text-decoration: none;">.</ins> Systematic Methods of Chemical Process Design<ins style="font-weight: bold; text-decoration: none;">.</ins> Prentice-Hall: Upper Saddle River, 1997.</ref> Different parameters of the pump or compressor can also be specified, such as efficiency, which will impact the results of the simulation. It is therefore important to ensure the equipment is correctly specified to ensure accurate results.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>Another important consideration for pumps is that a Net Positive Suction Head (<math>NPSH</math>) must be maintained within the pump, in order to avoid cavitation.<ref name="Turton">R.T. Turton, R.C. Bailie, W.B. Whiting, J.A. Shaeiwitz<del style="font-weight: bold; text-decoration: none;">,</del> Analysis, Synthesis, and Design of Chemical Processes<del style="font-weight: bold; text-decoration: none;">,</del> Prentice Hall: Upper Saddle River, 2003.</ref> Cavitation occurs because as fluid enters a pump, frictional losses near the pump entrance cause a pressure drop, leading to a minimum pressure somewhere in the pump, and if the fluid is close to saturation, bubbles can form within the pump<ref name ="Turton" />. Specifically, to avoid cavitation, the available NPSH (<math> NPSH_{avail} </math>) must exceed the required NPSH (<math> NPSH_{reqd} </math>), which is specified by the manufacturer of the pump because <math> NPSH_{reqd} </math> depends on the pump design. The <math> NPSH_{avail} </math> can be found by using equation (20.21) in Towler, below: <ref name ="Towler" /></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Another important consideration for pumps is that a Net Positive Suction Head (<math>NPSH</math>) must be maintained within the pump, in order to avoid cavitation.<ref name="Turton">R.T. Turton, R.C. Bailie, W.B. Whiting, J.A. Shaeiwitz<ins style="font-weight: bold; text-decoration: none;">.</ins> Analysis, Synthesis, and Design of Chemical Processes<ins style="font-weight: bold; text-decoration: none;">.</ins> Prentice Hall: Upper Saddle River, 2003.</ref> Cavitation occurs because as fluid enters a pump, frictional losses near the pump entrance cause a pressure drop, leading to a minimum pressure somewhere in the pump, and if the fluid is close to saturation, bubbles can form within the pump<ref name ="Turton" />. Specifically, to avoid cavitation, the available NPSH (<math> NPSH_{avail} </math>) must exceed the required NPSH (<math> NPSH_{reqd} </math>), which is specified by the manufacturer of the pump because <math> NPSH_{reqd} </math> depends on the pump design. The <math> NPSH_{avail} </math> can be found by using equation (20.21) in Towler, below: <ref name ="Towler" /></div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>==Modeling Pumps with HYSYS==</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>==Modeling Pumps with HYSYS==</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>Pumps can be modeled in Aspen HYSYS using the pump unit operation. Modeling can be done because while the specific thermodynamics, physical properties, and kinetics may differ from process to process, the conservation equations remain the same for similar process units, pumps included.<ref name="Seider"> W.D. Seider, J.D. Seader, D.R. Lewin<del style="font-weight: bold; text-decoration: none;">,</del> Process Design Principles: Synthesis, Analysis, and Evaluation<del style="font-weight: bold; text-decoration: none;">,</del> Wiley: New York, 2004.</ref>. In order to model a pump, it pump requires an inlet stream, an outlet stream, and an energy stream, as can be seen in the figure below.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Pumps can be modeled in Aspen HYSYS using the pump unit operation. Modeling can be done because while the specific thermodynamics, physical properties, and kinetics may differ from process to process, the conservation equations remain the same for similar process units, pumps included.<ref name="Seider"> W.D. Seider, J.D. Seader, D.R. Lewin<ins style="font-weight: bold; text-decoration: none;">.</ins> Process Design Principles: Synthesis, Analysis, and Evaluation<ins style="font-weight: bold; text-decoration: none;">.</ins> Wiley: New York, 2004.</ref>. In order to model a pump, it pump requires an inlet stream, an outlet stream, and an energy stream, as can be seen in the figure below.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>Likewise, specifying an inlet and outlet stream conditions will cause the compressor to converge. Another option for more specific information to be included in the simulation is by adding performance curves to the equipment. To add a performance curve, double click the compressor and go to the rating tab, then the curve page, check the "Enable Curves" check box, and then hit the add curve button.<ref name="Compressor Tutorial">N. Brownrigg. Jump start: Compressor modeling in Aspen HYSYS® Dynamics. Aspen Tech<del style="font-weight: bold; text-decoration: none;">.</del> 2015. Available at http://www.aspentech.com/compressor_modeling_jump_start.pdf Accessed 2/21/2016</ref></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Likewise, specifying an inlet and outlet stream conditions will cause the compressor to converge. Another option for more specific information to be included in the simulation is by adding performance curves to the equipment. To add a performance curve, double click the compressor and go to the rating tab, then the curve page, check the "Enable Curves" check box, and then hit the add curve button.<ref name="Compressor Tutorial">N. Brownrigg. Jump start: Compressor modeling in Aspen HYSYS® Dynamics. Aspen Tech<ins style="font-weight: bold; text-decoration: none;">,</ins> 2015. Available at http://www.aspentech.com/compressor_modeling_jump_start.pdf Accessed 2/21/2016</ref></div></td>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4540&oldid=prevKedricdaly2: /* Modeling Compressors with HYSYS */2016-02-21T19:21:46Z<p><span dir="auto"><span class="autocomment">Modeling Compressors with HYSYS</span></span></p>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>Likewise, specifying an inlet and outlet stream conditions will cause the compressor to converge. Another option for more specific information to be included in the simulation is by adding performance curves to the equipment.</div></td>
<td class="diff-marker" data-marker="+"></td>
<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Likewise, specifying an inlet and outlet stream conditions will cause the compressor to converge. Another option for more specific information to be included in the simulation is by adding performance curves to the equipment.<ins style="font-weight: bold; text-decoration: none;"> To add a performance curve, double click the compressor and go to the rating tab, then the curve page, check the "Enable Curves" check box, and then hit the add curve button.<ref name="Compressor Tutorial">N. Brownrigg. Jump start: Compressor modeling in Aspen HYSYS® Dynamics. Aspen Tech. 2015. Available at http://www.aspentech.com/compressor_modeling_jump_start.pdf Accessed 2/21/2016</ref></ins></div></td>
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</table>Kedricdaly2https://processdesign.mccormick.northwestern.edu/index.php?title=Pressure_changer&diff=4535&oldid=prevKedricdaly2 at 19:12, 21 February 20162016-02-21T19:12:28Z<p></p>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Where <math> P </math> is the pressure above the liquid in the feed vessel, <math> H </math> is the height of the liquid above the pump section, <math>P_f</math> is the pressure loss in the suction piping, <math> P_v </math> is the vapor pressure of the liquid at the pump suction, <math> \rho </math> is the density of the liquid, and <math> g </math> is the acceleration due to gravity. Regardless of what <math> NPSH_{reqd} </math> is, the <math> NPSH_{avail} </math> from the above equation must exceed it to avoid cavitation.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Where <math> P </math> is the pressure above the liquid in the feed vessel, <math> H </math> is the height of the liquid above the pump section, <math>P_f</math> is the pressure loss in the suction piping, <math> P_v </math> is the vapor pressure of the liquid at the pump suction, <math> \rho </math> is the density of the liquid, and <math> g </math> is the acceleration due to gravity. Regardless of what <math> NPSH_{reqd} </math> is, the <math> NPSH_{avail} </math> from the above equation must exceed it to avoid cavitation.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #ffe49c; vertical-align: top; white-space: pre-wrap;"><div>==Modeling with HYSYS==</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>==Modeling<ins style="font-weight: bold; text-decoration: none;"> Pumps</ins> with HYSYS==</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Pumps can be modeled in Aspen HYSYS using the pump unit operation. Modeling can be done because while the specific thermodynamics, physical properties, and kinetics may differ from process to process, the conservation equations remain the same for similar process units, pumps included.<ref name="Seider"> W.D. Seider, J.D. Seader, D.R. Lewin, Process Design Principles: Synthesis, Analysis, and Evaluation, Wiley: New York, 2004.</ref>. In order to model a pump, it pump requires an inlet stream, an outlet stream, and an energy stream, as can be seen in the figure below.</div></td>
<td class="diff-marker"></td>
<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Pumps can be modeled in Aspen HYSYS using the pump unit operation. Modeling can be done because while the specific thermodynamics, physical properties, and kinetics may differ from process to process, the conservation equations remain the same for similar process units, pumps included.<ref name="Seider"> W.D. Seider, J.D. Seader, D.R. Lewin, Process Design Principles: Synthesis, Analysis, and Evaluation, Wiley: New York, 2004.</ref>. In order to model a pump, it pump requires an inlet stream, an outlet stream, and an energy stream, as can be seen in the figure below.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Centrifugal compressors are similar to centrifugal pumps, with the major difference being the fluid going into the compressors are compressible. <ref name="Turton"/> This fact makes the math behind modeling compressors more complex than for pumps where an incompressible fluid assumption is made. There are still similarities however, in that a performance curve is often provided by the manufacturer so that outlet pressure can be related to inlet pressure and flow rates. One major difference between pump and compressor performance curves is that compressor performance curves deal with a pressure ratio, rather than a pressure difference, and a surge line is often included as well. <ref name="Turton"/> The surge line is important because it marks the point where a lower flowrate would result in backflow, which could lead to a reversal of flow direction and would damage the compressor.<ref name="Turton"/>.</div></td>
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<td style="background-color: #f8f9fa; color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #eaecf0; vertical-align: top; white-space: pre-wrap;"><div>Centrifugal compressors are similar to centrifugal pumps, with the major difference being the fluid going into the compressors are compressible. <ref name="Turton"/> This fact makes the math behind modeling compressors more complex than for pumps where an incompressible fluid assumption is made. There are still similarities however, in that a performance curve is often provided by the manufacturer so that outlet pressure can be related to inlet pressure and flow rates. One major difference between pump and compressor performance curves is that compressor performance curves deal with a pressure ratio, rather than a pressure difference, and a surge line is often included as well. <ref name="Turton"/> The surge line is important because it marks the point where a lower flowrate would result in backflow, which could lead to a reversal of flow direction and would damage the compressor.<ref name="Turton"/>.</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>==Modeling Compressors with HYSYS==</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>[[File:PC_compressor_initial.PNG|center|500px]]</div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div></center></div></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><br /></td>
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<td style="color: #202122; font-size: 88%; border-style: solid; border-width: 1px 1px 1px 4px; border-radius: 0.33em; border-color: #a3d3ff; vertical-align: top; white-space: pre-wrap;"><div>Likewise, specifying an inlet and outlet stream conditions will cause the compressor to converge. Another option for more specific information to be included in the simulation is by adding performance curves to the equipment.</div></td>
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</table>Kedricdaly2