Natural-gas processing

<h2 id="types-of-raw-natural-gas-wells">Types of raw-natural-gas wells</h2>
<ul><li>Crude <a href="/facts/Oil_well/mNNRJmuE">oil wells</a>: Natural gas that comes from crude oil wells is typically called associated gas. This gas could exist as a separate gas cap above the crude oil in the underground reservoir or could be dissolved in the crude oil, ultimately coming out of solution as the pressure is reduced during production. Condensate produced from oil wells is often referred to as lease condensate.<a class="footnote-ref" id="fnref:7" href="#fn:7">7</a></li>
<li>Dry gas wells: These wells typically produce only raw natural gas that contains no condensate with little to no crude oil and are called non-associated gas. Condensate from dry gas is extracted at gas processing plants and is often called plant condensate.<a class="footnote-ref" id="fnref:8" href="#fn:8">8</a></li>
<li>Condensate wells: These wells typically produce raw natural gas along with natural gas liquid with little to no crude oil and are called non-associated gas. Such raw natural gas is often referred to as <a href="/facts/Wet_gas/rErrFqJF">wet gas</a>.</li>
<li>Coal seam wells: These wells typically produce raw natural gas from methane deposits in the pores of coal seams, often existing underground in a more concentrated state of <a href="/facts/Adsorption/ARH9peYM">adsorption</a> onto the surface of the coal itself. Such gas is referred to as coalbed gas or <a href="/facts/Coalbed_methane/2uRWPWpE">coalbed methane</a> (<a href="/facts/Coal_seam_gas/2uRWPWpE">coal seam gas</a> in Australia). Coalbed gas has become an important source of energy in recent decades.</li></ul>
<h2 id="contaminants-in-raw-natural-gas">Contaminants in raw natural gas</h2>
See also: <a href="/facts/Natural-gas_condensate/yFKqn8SS">Natural-gas condensate</a>
Raw natural gas typically consists primarily of <a href="/facts/Methane/kBHneYnh">methane</a> (CH4) and <a href="/facts/Ethane/BGCzc6yh">ethane</a> (C2H6), the shortest and lightest <a href="/facts/Hydrocarbon/Dcg95Ju5">hydrocarbon</a> molecules. It often also contains varying amounts of:

<ul><li>Heavier gaseous hydrocarbons: <a href="/facts/Propane/E0b23KGh">propane</a> (C3H8), <a href="/facts/Butane/InIHpYlY">normal butane</a> (n-C4H10), <a href="/facts/Isobutane/Bd8H7rsH">isobutane</a> (i-C4H10) and <a href="/facts/Pentane/B5LzJ2zD">pentanes</a>. All of these are collectively referred to as <a href="/facts/Natural-gas_condensate/yFKqn8SS">Natural Gas Liquids</a> or NGL and can be processed into finished by-products.</li>
<li>Liquid hydrocarbons (also referred to as casinghead gasoline or natural gasoline) and/or <a href="/facts/Crude_oil/IQV0bHVd">crude oil</a>.</li>
<li><a href="/facts/Acid_gas/IN9jzyMg">Acid gases</a>: <a href="/facts/Carbon_dioxide/xGzpppEp">carbon dioxide</a> (CO2), <a href="/facts/Hydrogen_sulfide/UbCqjMMk">hydrogen sulfide</a> (H2S) and <a href="/facts/Mercaptan/VemKEDP9">mercaptans</a> such as <a href="/facts/Methanethiol/hKk384K1">methanethiol</a> (CH3SH) and <a href="/facts/Ethanethiol/3zjKzHH4">ethanethiol</a> (C2H5SH).</li>
<li>Other gases: <a href="/facts/Nitrogen/Nf1QpGDz">nitrogen</a> (N2) and <a href="/facts/Helium/yRul93TG">helium</a> (He).</li>
<li>Water: <a href="/facts/Water_vapor/DX5IUFG0">water vapor</a> and liquid water. Also dissolved salts and dissolved gases (acids).</li>
<li><a href="/facts/Mercury_(element)/WlxfoHva">Mercury</a>: minute amounts of mercury primarily in elemental form, but chlorides and other species are possibly present.<a class="footnote-ref" id="fnref:9" href="#fn:9">9</a></li>
<li><a href="/facts/Naturally_occurring_radioactive_material/oUbIxWlg">Naturally occurring radioactive material</a> (NORM): natural gas may contain <a href="/facts/Radon/0V9arWKl">radon</a>, and the <a href="/facts/Produced_water/0MwkTub2">produced water</a> may contain dissolved traces of <a href="/facts/Radium/VWo5gkzn">radium</a>, which can accumulate within piping and processing equipment; rendering piping and equipment radioactive over time.<a class="footnote-ref" id="fnref:10" href="#fn:10">10</a></li></ul>
<h2 id="natural-gas-quality-standards">Natural gas quality standards</h2>
Raw natural gas must be purified to meet the quality standards specified by the major <a href="/facts/Pipeline_transport/gEmKcFhD">pipeline</a> transmission and distribution companies. Those quality standards vary from pipeline to pipeline and are usually a function of a pipeline system's design and the markets that it serves. In general, the standards specify that the natural gas:

<ul><li>Be within a specific range of heating value (caloric value). For example, in the United States, it should be about 1035 ± 5% <a href="/facts/British_thermal_unit/GwIjRAPz">BTU</a> per cubic foot of gas at 1 atmosphere and 60 °F (41 <a href="/facts/Megajoule/9ndq9jD2">MJ</a> ± 5% per cubic metre of gas at 1 atmosphere and 15.6 °C). In the United Kingdom the gross <a href="/facts/Calorific_value/HdQX0mPP">calorific value</a> must be in the range 37.0 – 44.5 MJ/m3 for entry into the <a href="/facts/National_Transmission_System/o7lMlnsf">National Transmission System</a> (NTS).<a class="footnote-ref" id="fnref:11" href="#fn:11">11</a></li>
<li>Be delivered at or above a specified <a href="/facts/Hydrocarbon_dew_point/utwIU2NP">hydrocarbon dew point</a> temperature (below which some of the hydrocarbons in the gas might condense at pipeline pressure forming liquid slugs that could damage the pipeline.) Hydrocarbon dew-point adjustment reduces the concentration of heavy hydrocarbons so no condensation occurs during the ensuing transport in the pipelines. In the UK the hydrocarbon dew point is defined as <-2 °C for entry into the NTS.<a class="footnote-ref" id="fnref:12" href="#fn:12">12</a> The hydrocarbon dewpoint changes with the prevailing ambient temperature, the seasonal variation is:<a class="footnote-ref" id="fnref:13" href="#fn:13">13</a></li></ul>
Seasonal variation of hydrocarbon dewpoint<table><tbody><tr><th>Hydrocarbon dewpoint</th><td>30 °F (–1.1 °C)</td><td>35 °F (1.7 °C)</td><td>40 °F (4.4 °C)</td><td>45 °F (7.2 °C)</td><td>50 °F (10 °C)</td></tr><tr><th>Months</th><td>DecemberJanuaryFebruaryMarch</td><td>AprilNovember</td><td>MayOctober</td><td>JuneSeptember</td><td>JulyAugust</td></tr></tbody></table>
The natural gas should: 

<ul><li>Be free of particulate solids and liquid water to prevent erosion, corrosion or other damage to the pipeline.</li>
<li>Be dehydrated of water vapor sufficiently to prevent the formation of methane hydrates within the gas processing plant or subsequently within the sales gas transmission pipeline. A typical water content specification in the U.S. is that gas must contain no more than seven pounds of water per million <a href="/facts/Standard_cubic_foot/vK9AzNT3">standard cubic feet</a> of gas.<a class="footnote-ref" id="fnref:14" href="#fn:14">14</a><a class="footnote-ref" id="fnref:15" href="#fn:15">15</a> In the UK this is defined as <-10 °C @ 85barg for entry into the NTS.<a class="footnote-ref" id="fnref:16" href="#fn:16">16</a></li>
<li>Contain no more than trace amounts of components such as hydrogen sulfide, carbon dioxide, mercaptans, and nitrogen. The most common specification for hydrogen sulfide content is 0.25 <a href="/facts/Grain_(unit)/kkDKk6na">grain</a> H2S per 100 cubic feet of gas, or approximately 4 ppm. Specifications for CO2 typically limit the content to no more than two or three percent. In the UK hydrogen sulfide is specified ≤5 mg/m3 and total sulfur as ≤50 mg/m3, carbon dioxide as ≤2.0% (molar), and nitrogen as ≤5.0% (molar) for entry into the NTS.<a class="footnote-ref" id="fnref:17" href="#fn:17">17</a></li>
<li>Maintain mercury at less than detectable limits (approximately 0.001 <a href="/facts/Parts_per_billion/PozRuoLM">ppb</a> by volume) primarily to avoid damaging equipment in the gas processing plant or the pipeline transmission system from mercury amalgamation and embrittlement of aluminum and other metals.<a class="footnote-ref" id="fnref:18" href="#fn:18">18</a><a class="footnote-ref" id="fnref:19" href="#fn:19">19</a><a class="footnote-ref" id="fnref:20" href="#fn:20">20</a></li></ul>
<h2 id="description-of-a-natural-gas-processing-plant">Description of a natural-gas processing plant</h2>
There are a variety of ways in which to configure the various <a href="/facts/Unit_process/H9YTSunn">unit processes</a> used in the treatment of raw natural gas. The <a href="/facts/Process_flow_diagram/Gs8MKv9M">block flow diagram</a> below is a generalized, typical configuration for the processing of raw natural gas from non-associated gas wells showing how raw natural gas is processed into sales gas piped to the end user markets.<a class="footnote-ref" id="fnref:21" href="#fn:21">21</a><a class="footnote-ref" id="fnref:22" href="#fn:22">22</a><a class="footnote-ref" id="fnref:23" href="#fn:23">23</a><a class="footnote-ref" id="fnref:24" href="#fn:24">24</a><a class="footnote-ref" id="fnref:25" href="#fn:25">25</a> and various byproducts:

<ul><li><a href="/facts/Natural-gas_condensate/yFKqn8SS">Natural-gas condensate</a></li>
<li><a href="/facts/Sulfur/IK0amTfM">Sulfur</a></li>
<li>Ethane</li>
<li><a href="/facts/Natural_gas_liquids/yFKqn8SS">Natural gas liquids</a> (NGL): propane, butanes and C5+ (which is the commonly used term for pentanes plus higher molecular weight hydrocarbons)<a class="footnote-ref" id="fnref:26" href="#fn:26">26</a><a class="footnote-ref" id="fnref:27" href="#fn:27">27</a><a class="footnote-ref" id="fnref:28" href="#fn:28">28</a></li></ul>
Raw natural gas is commonly collected from a group of adjacent wells and is first processed in a separator vessels at that collection point for removal of free liquid water and <a href="/facts/Natural_gas_condensate/yFKqn8SS">natural gas condensate</a>.<a class="footnote-ref" id="fnref:29" href="#fn:29">29</a> The condensate is usually then transported to an oil refinery and the water is treated and disposed of as wastewater.
The raw gas is then piped to a gas processing plant where the initial purification is usually the removal of acid gases (hydrogen sulfide and carbon dioxide). There are several processes available for that purpose as shown in the flow diagram, but <a href="/facts/Amine_gas_treating/oJ0HHFQV">amine treating</a> is the process that was historically used. However, due to a range of performance and environmental constraints of the amine process, a newer technology based on the use of <a href="/facts/Synthetic_membrane/ImpnK6eH">polymeric membranes</a> to separate the carbon dioxide and hydrogen sulfide from the natural gas stream has gained increasing acceptance. Membranes are attractive since no reagents are consumed.<a class="footnote-ref" id="fnref:30" href="#fn:30">30</a>
The acid gases, if present, are removed by membrane or amine treating and can then be routed into a sulfur recovery unit which converts the hydrogen sulfide in the acid gas into either elemental sulfur or sulfuric acid. Of the processes available for these conversions, the <a href="/facts/Claus_process/FbhagLPm">Claus process</a> is by far the most well known for recovering elemental sulfur, whereas the conventional <a href="/facts/Contact_process/vNmmUQ3s">Contact process</a> and the WSA (<a href="/facts/Wet_sulfuric_acid_process/sS0AKY1p">Wet sulfuric acid process</a>) are the most used technologies for recovering <a href="/facts/Sulfuric_acid/Wom6fymJ">sulfuric acid</a>. Smaller quantities of acid gas may be disposed of by flaring.
The residual gas from the Claus process is commonly called tail gas and that gas is then processed in a tail gas treating unit (TGTU) to recover and recycle residual sulfur-containing compounds back into the Claus unit. Again, as shown in the flow diagram, there are a number of processes available for treating the Claus unit tail gas and for that purpose a WSA process is also very suitable since it can work autothermally on tail gases.
The next step in the gas processing plant is to remove water vapor from the gas using either the regenerable <a href="/facts/Absorption_(chemistry)/XGeB64bC">absorption</a> in liquid <a href="/facts/Triethylene_glycol/cyejXbCc">triethylene glycol</a> (TEG),<a class="footnote-ref" id="fnref:31" href="#fn:31">31</a> commonly referred to as <a href="/facts/Glycol_dehydration/paA6g9YI">glycol dehydration</a>, deliquescent chloride desiccants, and or a <a href="/facts/Pressure_Swing_Adsorption/lwajr7zV">Pressure Swing Adsorption</a> (PSA) unit which is regenerable <a href="/facts/Adsorption/ARH9peYM">adsorption</a> using a solid adsorbent.<a class="footnote-ref" id="fnref:32" href="#fn:32">32</a> Other newer processes like <a href="/facts/Membrane_technology/H82dQc58">membranes</a> may also be considered.
Mercury is then removed by using adsorption processes (as shown in the flow diagram) such as <a href="/facts/Activated_carbon/YAbaXCcb">activated carbon</a> or regenerable <a href="/facts/Molecular_sieve/Lzle8J7k">molecular sieves</a>.<a class="footnote-ref" id="fnref:33" href="#fn:33">33</a>
Although not common, nitrogen is sometimes removed and rejected using one of the three processes indicated on the flow diagram:

<ul><li><a href="/facts/Cryogenic/cw7dHAkp">Cryogenic</a> process (<a href="/facts/Nitrogen_Rejection_Unit/WaduqUnI">Nitrogen Rejection Unit</a>),<a class="footnote-ref" id="fnref:34" href="#fn:34">34</a> using low temperature <a href="/facts/Continuous_distillation/0w5QbD8c">distillation</a>. This process can be modified to also recover helium, if desired (see also <a href="/facts/Industrial_gas/LcMR7LkG">industrial gas</a>).</li>
<li>Absorption process,<a class="footnote-ref" id="fnref:35" href="#fn:35">35</a> using lean oil or a special solvent<a class="footnote-ref" id="fnref:36" href="#fn:36">36</a> as the absorbent.</li>
<li>Adsorption process, using activated carbon or molecular sieves as the adsorbent. This process may have limited applicability because it is said to incur the loss of butanes and heavier hydrocarbons.</li></ul>
<h3>NGL fractionation train</h3>
The NGL fractionation process treats offgas from the separators at an <a href="/facts/Oil_terminal/8xqIeRjU">oil terminal</a> or the overhead fraction from a crude distillation column in a <a href="/facts/Refinery/ErU4apog">refinery</a>. Fractionation aims to produce useful products including natural gas suitable for piping to industrial and domestic consumers; <a href="/facts/Liquefied_petroleum_gas/bw6trakm">liquefied petroleum gases</a> (Propane and Butane) for sale; and <a href="/facts/Gasoline/lcnxq5BS">gasoline</a> feedstock for liquid fuel blending.<a class="footnote-ref" id="fnref:37" href="#fn:37">37</a> The recovered NGL stream is processed through a fractionation train consisting of up to five distillation towers in series: a demethanizer, a deethanizer, a depropanizer, a debutanizer and a butane splitter. The fractionation train typically uses a cryogenic low temperature distillation process involving expansion of the recovered NGL through a <a href="/facts/Turbo-expander/QqUeVKQu">turbo-expander</a> followed by distillation in a demethanizing <a href="/facts/Fractionating_column/snYmDSRI">fractionating column</a>.<a class="footnote-ref" id="fnref:38" href="#fn:38">38</a><a class="footnote-ref" id="fnref:39" href="#fn:39">39</a> Some gas processing plants use lean oil absorption process<a class="footnote-ref" id="fnref:40" href="#fn:40">40</a> rather than the cryogenic turbo-expander process.
The gaseous feed to the NGL fractionation plant is typically compressed to about 60 <a href="/facts/Bar_(unit)/wwFWTTkT">bar</a> and 37 °C.<a class="footnote-ref" id="fnref:41" href="#fn:41">41</a> The feed is cooled to -22 °C, by exchange with the demethanizer overhead product and by a refrigeration system and is split into three streams:

<ul><li>Condensed liquid passes through a <a href="/facts/Joule%25E2%2580%2593Thomson_effect/9MLL4NeG">Joule-Thomson</a> valve reducing the pressure to 20 bar and enters the demethanizer as the lower feed at -44.7 °C.</li>
<li>Some of the vapour is routed through a turbo-expander and enters the demethanizer as the upper feed at -64 °C.</li>
<li>The remaining vapor is chilled by the demethanizer overhead product and Joule-Thomson cooling (through a valve) and enters the column as <a href="/facts/Reflux/Elav2kgM">reflux</a> at -96 °C.<a class="footnote-ref" id="fnref:42" href="#fn:42">42</a></li></ul>
The overhead product is mainly methane at 20 bar and -98 °C. This is heated and compressed to yield a sales gas at 20 bar and 40 °C. The bottom product is NGL at 20 barg which is fed to the deethanizer.  
The overhead product from the deethanizer is ethane and the bottoms are fed to the depropanizer. The overhead product from the depropanizer is propane and the bottoms are fed to the debutanizer. The overhead product from the debutanizer is a mixture of normal and iso-butane, and the bottoms product is a C5+ gasoline mixture.
The operating conditions of the vessels in the NGL fractionation train are typically as follows.<a class="footnote-ref" id="fnref:43" href="#fn:43">43</a><a class="footnote-ref" id="fnref:44" href="#fn:44">44</a><a class="footnote-ref" id="fnref:45" href="#fn:45">45</a>

NGL column operating conditions<table><tbody><tr><td></td><th>Demethanizer</th><th>Deethanizer</th><th>Depropanizer</th><th>Debutanizer</th><th>Butane Splitter</th></tr><tr><th>Feed pressure</th><td>60 barg</td><td>30 barg</td><td></td><td></td><td></td></tr><tr><th>Feed temperature</th><td>37 °C</td><td>25 °C</td><td>37 °C</td><td>125 °C</td><td>59 °C</td></tr><tr><th>Column operating pressure</th><td>20 barg</td><td>26-30 barg</td><td>10-16.2 barg</td><td>3.8-17 barg</td><td>4.9-7 barg</td></tr><tr><th>Overhead product temperature</th><td>-98°C</td><td></td><td>50 °C</td><td>59 °C</td><td>49 °C</td></tr><tr><th>Bottom product temperature</th><td>12 °C</td><td>37 °C</td><td>125 °C</td><td>118 °C</td><td>67 °C</td></tr><tr><th>Overhead product</th><td>Methane (natural gas)</td><td>Ethane</td><td>Propane</td><td>Butane</td><td>Isobutane</td></tr><tr><th>Bottom product</th><td>Natural gas liquids</td><td>(Depropanizer feed)</td><td>(Debutanizer feed)</td><td>Gasoline</td><td>Normal Butane</td></tr></tbody></table>
A typical composition of the feed and product is as follows.<a class="footnote-ref" id="fnref:46" href="#fn:46">46</a>

Stream composition, % volume<table><tbody><tr><th>Component</th><th>Feed</th><th>NGL</th><th>Ethane</th><th>Propane</th><th>Isobutane</th><th>n-Butane</th><th>Gasoline</th></tr><tr><td>Methane</td><td>89.4</td><td>0.5</td><td>1.36</td><td></td><td></td><td></td><td></td></tr><tr><td>Ethane</td><td>4.9</td><td>37.0</td><td>95.14</td><td>7.32</td><td></td><td></td><td></td></tr><tr><td>Propane</td><td>2.2</td><td>26.0</td><td>3.5</td><td>90.18</td><td>2.0</td><td></td><td></td></tr><tr><td>Isobutane</td><td>1.3</td><td>7.2</td><td></td><td rowspan="2">2.5</td><td>96.0</td><td>4.5</td><td></td></tr><tr><td>n-Butane</td><td rowspan="5">2.2</td><td>14.8</td><td></td><td>2.0</td><td>95.0</td><td>3.0</td></tr><tr><td>Isopentane</td><td>5.0</td><td></td><td></td><td></td><td></td><td>33.13</td></tr><tr><td>n-Pentane</td><td>3.5</td><td></td><td></td><td></td><td>0.5</td><td>23.52</td></tr><tr><td>n-Hexane</td><td>4.0</td><td></td><td></td><td></td><td></td><td>26.9</td></tr><tr><td>n-Heptane</td><td>2.0</td><td></td><td></td><td></td><td></td><td>13.45</td></tr><tr><td>Total</td><td>100</td><td>100</td><td>100</td><td>100</td><td>100</td><td>100</td><td>100</td></tr></tbody></table>
<h3>Sweetening Units</h3>
The recovered streams of propane, butanes and C5+ may be "sweetened" in a <a href="/facts/Merox/KJ8FSH8Q">Merox</a> process unit to convert undesirable mercaptans into <a href="/facts/Disulfide/eDx5Xtlg">disulfides</a> and, along with the recovered ethane, are the final NGL by-products from the gas processing plant. Currently, most cryogenic plants do not include fractionation for economic reasons, and the NGL stream is instead transported as a mixed product to standalone fractionation complexes located near refineries or chemical plants that use the components for <a href="/facts/Feedstock/cthCpclF">feedstock</a>. In case laying pipeline is not possible for geographical reason, or the distance between source and consumer exceed 3000 km, natural gas is then transported by ship as <a href="/facts/LNG/HIm7BbAl">LNG</a> (<a href="/facts/Liquefied_natural_gas/HIm7BbAl">liquefied natural gas</a>) and again converted into its gaseous state in the vicinity of the consumer.

<h3>Products</h3>
The residue gas from the NGL recovery section is the final, purified sales gas which is pipelined to the end-user markets. Rules and agreements are made between buyer and seller regarding the quality of the gas. These usually specify the maximum allowable concentration of CO2, H2S and H2O as well as requiring the gas to be commercially free from objectionable odours and materials, and dust or other solid or liquid matter, waxes, gums and gum forming constituents, which might damage or adversely affect operation of the buyers equipment. When an upset occurs on the treatment plant buyers can usually refuse to accept the gas, lower the flow rate or re-negotiate the price.

<h3>Helium recovery</h3>
If the gas has significant <a href="/facts/Helium/yRul93TG">helium</a> content, the helium may be recovered by <a href="/facts/Fractional_distillation/DdNf0k8I">fractional distillation</a>. Natural gas may contain as much as 7% helium, and is the commercial source of the <a href="/facts/Noble_gas/j0yHMEAE">noble gas</a>.<a class="footnote-ref" id="fnref:47" href="#fn:47">47</a> For instance, the <a href="/facts/Hugoton_Gas_Field/2w7UauAl">Hugoton Gas Field</a> in Kansas and Oklahoma in the United States contains concentrations of helium from 0.3% to 1.9%, which is separated out as a valuable byproduct.<a class="footnote-ref" id="fnref:48" href="#fn:48">48</a>

<h2 id="see-also">See also</h2>
<ul><li><a href="/facts/Liquid_carryover/Dk0rkWUc">Liquid carryover</a></li>
<li><a href="/facts/Natural_gas_prices/VQMR4Pel">Natural gas prices</a></li>
<li><a href="/facts/Petroleum_extraction/GyyC7lTo">Petroleum extraction</a></li>
<li><a href="/facts/Oil_refinery/yeaW0UMv">Oil refinery</a></li>
<li><a href="/facts/List_of_natural_gas_and_oil_production_accidents_in_the_United_States/GAfgRWPN">List of natural gas and oil production accidents in the United States</a></li></ul>

<h2 id="external-links">External links</h2>
<ul><li><a href="https://web.archive.org/web/20171216113613/http://aspentech.com/products/engineering/aspen-HYSYS-upstream-midstream-solutions/">Simulate natural gas processing using Aspen HYSYS</a></li>
<li><a href="https://www.ucalgary.ca/ENCH/class_notes/ench607/mainmenu.pdf">Natural Gas Processing Principles and Technology</a> (an extensive and detailed course text by Dr. A.H. Younger, <a href="/facts/University_of_Calgary/CXY7Ab7e">University of Calgary, Alberta, Canada</a>).</li>
<li><a href="https://web.archive.org/web/20110101053431/http://naturalgas.org/naturalgas/processing_ng.asp">Processing Natural Gas</a>, Website of the Natural Gas Supply Association (NGSA).</li>
<li><a href="http://www.epa.gov/ttn/chief/ap42/ch05/final/c05s03.pdf">Natural Gas Processing</a> (part of the <a href="/facts/AP_42_Compilation_of_Air_Pollutant_Emission_Factors/jPCf9J5f">US EPA's AP-42 publication</a>)</li>
<li><a href="http://primis.phmsa.dot.gov/comm/FactSheets/FSNaturalGasProcessingPlants.htm">Natural Gas Processing Plants</a> (a <a href="/facts/US_Department_of_Transportation/qgNCJ1tF">US Department of Transportation</a> website)</li>
<li><a href="http://gpaglobal.org/">Gas Processors Association</a>, Website of the Gas Processors Association (GPA) headquartered in Tulsa, Oklahoma, United States.</li>
<li><a href="http://uijs.ui.ac.ir/gpj">Gas Processing Journal</a> (Publisher: College of Engineering, University of Isfahan, Iran.)</li>
<li><a href="http://www.ima.co.uk/system/images/1126/original/process-vision-technical-bulletin-05-07-16-3-pv007.pdf?1468424671">Increasing Efficiency of Gas Processing Plants</a></li>
<li><a href="https://www.sulpetro.com/natural-gas-news">[1]</a></li></ul>
<h2 id="further-reading">Further reading</h2>
<ul><li>Haring, H.W. (2008). Industrial Gases Processing. Weinheim, Germany: WILEY-VCH Verlag Gmbh & CO. KGaA</li>
<li>Kohl, A., & Nielsen, R. (1997). Gas Purification. 5TH Edition. Houston, Texas: Gulf Publishing Company</li></ul>

<h2 id="references">References</h2>

<ol>
<li id="fn:1">"PHMSA: Stakeholder Communications - NG Processing Plants". primis.phmsa.dot.gov. Retrieved 9 April 2018. <a href="http://primis.phmsa.dot.gov/comm/FactSheets/FSNaturalGasProcessingPlants.htm" target="_blank">http://primis.phmsa.dot.gov/comm/FactSheets/FSNaturalGasProcessingPlants.htm</a> <a href="#fnref:1" class="footnote-back-ref">↩</a></li>
<li id="fn:2">Speight, James G. (2015). Handbook of Petroleum Product Analysis, Second Edition. Hoboken, NJ: John Wiley & Sons. p. 71. ISBN 978-1-118-36926-5. <a href="978-1-118-36926-5" target="_blank">978-1-118-36926-5</a> <a href="#fnref:2" class="footnote-back-ref">↩</a></li>
<li id="fn:3">"Archived copy" (PDF). Archived from the original (PDF) on 2016-03-05. Retrieved 2014-09-21.{{cite web}}: CS1 maint: archived copy as title (link) <a href="https://web.archive.org/web/20160305070520/https://mitei.mit.edu/system/files/NaturalGas_Chapter2_Supply.pdf" target="_blank">https://web.archive.org/web/20160305070520/https://mitei.mit.edu/system/files/NaturalGas_Chapter2_Supply.pdf</a> <a href="#fnref:3" class="footnote-back-ref">↩</a></li>
<li id="fn:4">Kidnay, Arthur J.; Parrish, William R.; McCartney, Daniel G. (2019). Fundamentals of Natural Gas Processing, Third Edition. Boca Raton, FL: CRC Press. p. 165. ISBN 978-0-429-87715-5. <a href="978-0-429-87715-5" target="_blank">978-0-429-87715-5</a> <a href="#fnref:4" class="footnote-back-ref">↩</a></li>
<li id="fn:5">Agency, United States Central Intelligence (1977). Natural Gas. Washington, D.C.: U.S. Central Intelligence Agency. p. 25. <a href="#fnref:5" class="footnote-back-ref">↩</a></li>
<li id="fn:6">Speight, James G. (2015). Handbook of Petroleum Product Analysis, Second Edition. Hoboken, NJ: John Wiley & Sons. p. 71. ISBN 978-1-118-36926-5. <a href="978-1-118-36926-5" target="_blank">978-1-118-36926-5</a> <a href="#fnref:6" class="footnote-back-ref">↩</a></li>
<li id="fn:7">U.S. Crude Oil Production Forecast- Analysis of Crude Types (PDF), Washington, DC: U.S. Energy Information Administration, 29 May 2014, p. 7, A final point to consider involves the distinction between the very light grades of lease condensate (which are included in EIA's oil production data) and hydrocarbon gas liquids (HGL) that are produced from the wellhead as gas but are converted to liquids when separated from methane at a natural gas processing plant. These hydrocarbons include ethane, propane, butanes, and hydrocarbons with five or more carbon atoms – referred to as pentanes plus, naptha, or plant condensate. Plant condensate can also be blended with crude oil, which would change both the distribution and total volume of oil received by refineries. <a href="http://www.eia.gov/analysis/petroleum/crudetypes/pdf/crudetypes.pdf" target="_blank">http://www.eia.gov/analysis/petroleum/crudetypes/pdf/crudetypes.pdf</a> <a href="#fnref:7" class="footnote-back-ref">↩</a></li>
<li id="fn:8">U.S. Crude Oil Production Forecast- Analysis of Crude Types (PDF), Washington, DC: U.S. Energy Information Administration, 29 May 2014, p. 7, A final point to consider involves the distinction between the very light grades of lease condensate (which are included in EIA's oil production data) and hydrocarbon gas liquids (HGL) that are produced from the wellhead as gas but are converted to liquids when separated from methane at a natural gas processing plant. These hydrocarbons include ethane, propane, butanes, and hydrocarbons with five or more carbon atoms – referred to as pentanes plus, naptha, or plant condensate. Plant condensate can also be blended with crude oil, which would change both the distribution and total volume of oil received by refineries. <a href="http://www.eia.gov/analysis/petroleum/crudetypes/pdf/crudetypes.pdf" target="_blank">http://www.eia.gov/analysis/petroleum/crudetypes/pdf/crudetypes.pdf</a> <a href="#fnref:8" class="footnote-back-ref">↩</a></li>
<li id="fn:9">"Mercury Removal from Natural Gas and Liquids" (PDF). UOP LLC. Archived from the original (PDF) on 2011-01-01. <a href="https://web.archive.org/web/20110101194809/http://www.uop.com/objects/87MercuryRemoval.pdf" target="_blank">https://web.archive.org/web/20110101194809/http://www.uop.com/objects/87MercuryRemoval.pdf</a> <a href="#fnref:9" class="footnote-back-ref">↩</a></li>
<li id="fn:10">"Radium in Piping". <a href="https://pubs.rsc.org/en/content/getauthorversionpdf/C8EM00336J" target="_blank">https://pubs.rsc.org/en/content/getauthorversionpdf/C8EM00336J</a> <a href="#fnref:10" class="footnote-back-ref">↩</a></li>
<li id="fn:11">"Gas Safety (Management) Regulations 1996". legislation.co.uk. 1996. Retrieved 13 June 2020. <a href="http://www.legislation.gov.uk/uksi/1996/551/contents/made" target="_blank">http://www.legislation.gov.uk/uksi/1996/551/contents/made</a> <a href="#fnref:11" class="footnote-back-ref">↩</a></li>
<li id="fn:12">"Gas Safety (Management) Regulations 1996". legislation.co.uk. 1996. Retrieved 13 June 2020. <a href="http://www.legislation.gov.uk/uksi/1996/551/contents/made" target="_blank">http://www.legislation.gov.uk/uksi/1996/551/contents/made</a> <a href="#fnref:12" class="footnote-back-ref">↩</a></li>
<li id="fn:13">Institute of Petroleum (1978). A guide to North Sea oil and gas technology. London: Heyden & Son. p. 133. ISBN 0855013168. <a href="0855013168" target="_blank">0855013168</a> <a href="#fnref:13" class="footnote-back-ref">↩</a></li>
<li id="fn:14">Dehydration of Natural Gas Archived 2007-02-24 at the Wayback Machine by Prof. Jon Steiner Gudmundsson, Norwegian University of Science and Technology <a href="http://www.ipt.ntnu.no/~jsg/undervisning/naturgass/parlaktuna/Chap7.pdf" target="_blank">http://www.ipt.ntnu.no/~jsg/undervisning/naturgass/parlaktuna/Chap7.pdf</a> <a href="#fnref:14" class="footnote-back-ref">↩</a></li>
<li id="fn:15">Glycol Dehydration Archived 2009-09-12 at the Wayback Machine (includes a flow diagram) <a href="http://www.processgroup.com.au/Technologies/GasProcessing/GlycolDehyrdation/tabid/84/Default.aspx" target="_blank">http://www.processgroup.com.au/Technologies/GasProcessing/GlycolDehyrdation/tabid/84/Default.aspx</a> <a href="#fnref:15" class="footnote-back-ref">↩</a></li>
<li id="fn:16">"Gas Safety (Management) Regulations 1996". legislation.co.uk. 1996. Retrieved 13 June 2020. <a href="http://www.legislation.gov.uk/uksi/1996/551/contents/made" target="_blank">http://www.legislation.gov.uk/uksi/1996/551/contents/made</a> <a href="#fnref:16" class="footnote-back-ref">↩</a></li>
<li id="fn:17">"Gas Safety (Management) Regulations 1996". legislation.co.uk. 1996. Retrieved 13 June 2020. <a href="http://www.legislation.gov.uk/uksi/1996/551/contents/made" target="_blank">http://www.legislation.gov.uk/uksi/1996/551/contents/made</a> <a href="#fnref:17" class="footnote-back-ref">↩</a></li>
<li id="fn:18">"Mercury Removal from Natural Gas and Liquids" (PDF). UOP LLC. Archived from the original (PDF) on 2011-01-01. <a href="https://web.archive.org/web/20110101194809/http://www.uop.com/objects/87MercuryRemoval.pdf" target="_blank">https://web.archive.org/web/20110101194809/http://www.uop.com/objects/87MercuryRemoval.pdf</a> <a href="#fnref:18" class="footnote-back-ref">↩</a></li>
<li id="fn:19">Desulfurization of and Mercury Removal From Natural Gas Archived 2008-03-03 at the Wayback Machine by Bourke, M.J. and Mazzoni, A.F., Laurance Reid Gas Conditioning Conference, Norman, Oklahoma, March 1989. <a href="http://www.tigg.com/ACTIVATED-CARBON/desulfurization.html" target="_blank">http://www.tigg.com/ACTIVATED-CARBON/desulfurization.html</a> <a href="#fnref:19" class="footnote-back-ref">↩</a></li>
<li id="fn:20">Using Gas Geochemistry to Assess Mercury Risk Archived 2015-08-28 at the Wayback Machine, OilTracers, 2006 <a href="http://www.gaschem.com/mercur.html" target="_blank">http://www.gaschem.com/mercur.html</a> <a href="#fnref:20" class="footnote-back-ref">↩</a></li>
<li id="fn:21">Natural Gas Processing: The Crucial Link Between Natural Gas Production and Its Transportation to Market Archived 2011-03-04 at the Wayback Machine <a href="http://www.eia.doe.gov/pub/oil_gas/natural_gas/feature_articles/2006/ngprocess/ngprocess.pdf" target="_blank">http://www.eia.doe.gov/pub/oil_gas/natural_gas/feature_articles/2006/ngprocess/ngprocess.pdf</a> <a href="#fnref:21" class="footnote-back-ref">↩</a></li>
<li id="fn:22">Example Gas Plant Archived 2010-12-01 at the Wayback Machine <a href="http://www.uop.com/gasprocessing/6070.html" target="_blank">http://www.uop.com/gasprocessing/6070.html</a> <a href="#fnref:22" class="footnote-back-ref">↩</a></li>
<li id="fn:23">From Purification to Liquefaction Gas Processing Archived 2010-01-15 at the Wayback Machine <a href="http://www.axens.net/upload/presentations/fichier/axens_gpagcc_2004v2.pdf" target="_blank">http://www.axens.net/upload/presentations/fichier/axens_gpagcc_2004v2.pdf</a> <a href="#fnref:23" class="footnote-back-ref">↩</a></li>
<li id="fn:24">"Feed-Gas Treatment Design for the Pearl GTL Project" (PDF). spe.org. Retrieved 9 April 2018. <a href="http://www.spe.org/specma/binary/files/5804785Syn10682.pdf" target="_blank">http://www.spe.org/specma/binary/files/5804785Syn10682.pdf</a> <a href="#fnref:24" class="footnote-back-ref">↩</a></li>
<li id="fn:25">Benefits of integrating NGL extraction and LNG liquefaction Archived 2013-06-26 at the Wayback Machine <a href="http://lnglicensing.conocophillips.com/EN/publications/documents/AICHELNGNGLIntegrationPaper.pdf" target="_blank">http://lnglicensing.conocophillips.com/EN/publications/documents/AICHELNGNGLIntegrationPaper.pdf</a> <a href="#fnref:25" class="footnote-back-ref">↩</a></li>
<li id="fn:26">"MSDS: Natural gas liquids" (PDF). ConocoPhillips. <a href="http://www.conocophillips.com/sustainable-development/Documents/SMID_213_Natural%20Gas%20Liquids.pdf" target="_blank">http://www.conocophillips.com/sustainable-development/Documents/SMID_213_Natural%20Gas%20Liquids.pdf</a> <a href="#fnref:26" class="footnote-back-ref">↩</a></li>
<li id="fn:27">"What are natural gas liquids and how are they used?". United States Energy Information Administration. April 20, 2012. <a href="http://www.eia.gov/todayinenergy/detail.php?id=5930" target="_blank">http://www.eia.gov/todayinenergy/detail.php?id=5930</a> <a href="#fnref:27" class="footnote-back-ref">↩</a></li>
<li id="fn:28">"Guide to Understanding Natural Gas and Natural Gas Liquids". STI Group. 2014-02-19. <a href="http://setxind.com/energy-markets/guide-to-understanding-natural-gas-and-natural-gas-liquids/" target="_blank">http://setxind.com/energy-markets/guide-to-understanding-natural-gas-and-natural-gas-liquids/</a> <a href="#fnref:28" class="footnote-back-ref">↩</a></li>
<li id="fn:29">"Liquid / Gas Separation Technology - Oil & Gas | Pall Corporation". www.pall.com. Retrieved 2023-04-22. <a href="https://www.pall.com/en/oil-gas/midstream/liquid-gas-separation-technology.html" target="_blank">https://www.pall.com/en/oil-gas/midstream/liquid-gas-separation-technology.html</a> <a href="#fnref:29" class="footnote-back-ref">↩</a></li>
<li id="fn:30">Baker, R. W. "Future Directions of Membrane Gas Separation Technology" Ind. Eng. Chem. Res. 2002, volume 41, pages 1393-1411. doi:10.1021/ie0108088 <a href="/wiki/Doi_(identifier)" target="_blank">/wiki/Doi_(identifier)</a> <a href="#fnref:30" class="footnote-back-ref">↩</a></li>
<li id="fn:31">Glycol Dehydration Archived 2009-09-12 at the Wayback Machine (includes a flow diagram) <a href="http://www.processgroup.com.au/Technologies/GasProcessing/GlycolDehyrdation/tabid/84/Default.aspx" target="_blank">http://www.processgroup.com.au/Technologies/GasProcessing/GlycolDehyrdation/tabid/84/Default.aspx</a> <a href="#fnref:31" class="footnote-back-ref">↩</a></li>
<li id="fn:32">Molecular Sieves Archived 2011-01-01 at the Wayback Machine (includes a flow diagram of a PSA unit) <a href="http://www.uop.com/objects/96%20MolecularSieves.pdf" target="_blank">http://www.uop.com/objects/96%20MolecularSieves.pdf</a> <a href="#fnref:32" class="footnote-back-ref">↩</a></li>
<li id="fn:33">"Mercury Removal from Natural Gas and Liquids" (PDF). UOP LLC. Archived from the original (PDF) on 2011-01-01. <a href="https://web.archive.org/web/20110101194809/http://www.uop.com/objects/87MercuryRemoval.pdf" target="_blank">https://web.archive.org/web/20110101194809/http://www.uop.com/objects/87MercuryRemoval.pdf</a> <a href="#fnref:33" class="footnote-back-ref">↩</a></li>
<li id="fn:34">Gas Processes 2002, Hydrocarbon Processing, pages 84–86, May 2002 (schematic flow diagrams and descriptions of the Nitrogen Rejection and Nitrogen Removal processes) <a href="#fnref:34" class="footnote-back-ref">↩</a></li>
<li id="fn:35">Market-Driven Evolution of Gas Processing Technologies for NGLs Advanced Extraction Technology Inc. website page <a href="http://www.aet.com/gtip1.htm" target="_blank">http://www.aet.com/gtip1.htm</a> <a href="#fnref:35" class="footnote-back-ref">↩</a></li>
<li id="fn:36">AET Process Nitrogen Rejection Unit Advanced Extraction Technology Inc. website page <a href="http://www.aet.com/aetnrubig.pdf" target="_blank">http://www.aet.com/aetnrubig.pdf</a> <a href="#fnref:36" class="footnote-back-ref">↩</a></li>
<li id="fn:37">Manley, D. B. (1998). "Thermodynamically efficient distillation: NGL Fractionation". Latin American Applied Research. <a href="#fnref:37" class="footnote-back-ref">↩</a></li>
<li id="fn:38">Cryogenic Turbo-Expander Process Advanced Extraction Technology Inc. website page <a href="http://www.aet.com/turbo.htm" target="_blank">http://www.aet.com/turbo.htm</a> <a href="#fnref:38" class="footnote-back-ref">↩</a></li>
<li id="fn:39">Gas Processes 2002, Hydrocarbon Processing, pages 83–84, May 2002 (schematic flow diagrams and descriptions of the NGL-Pro and NGL Recovery processes) <a href="#fnref:39" class="footnote-back-ref">↩</a></li>
<li id="fn:40">Market-Driven Evolution of Gas Processing Technologies for NGLs Advanced Extraction Technology Inc. website page <a href="http://www.aet.com/gtip1.htm" target="_blank">http://www.aet.com/gtip1.htm</a> <a href="#fnref:40" class="footnote-back-ref">↩</a></li>
<li id="fn:41">Muneeb Nawaz ‘Synthesis and Design of Demethaniser Flowsheets for Low Temperature Separation Processes,' University of Manchester, unpublished PhD thesis, 2011, pp. 137, 138, 154 <a href="#fnref:41" class="footnote-back-ref">↩</a></li>
<li id="fn:42">Muneeb Nawaz ‘Synthesis and Design of Demethaniser Flowsheets for Low Temperature Separation Processes,' University of Manchester, unpublished PhD thesis, 2011, pp. 137, 138, 154 <a href="#fnref:42" class="footnote-back-ref">↩</a></li>
<li id="fn:43">Manley, D. B. (1998). "Thermodynamically efficient distillation: NGL Fractionation". Latin American Applied Research. <a href="#fnref:43" class="footnote-back-ref">↩</a></li>
<li id="fn:44">Luyben, W. L. (2013). "Control of a Train of Distillation Columns for the Separation of natural gas". Industrial and Engineering Chemistry Research. 52: 5710741–10753. doi:10.1021/ie400869v. <a href="/wiki/Doi_(identifier)" target="_blank">/wiki/Doi_(identifier)</a> <a href="#fnref:44" class="footnote-back-ref">↩</a></li>
<li id="fn:45">ElBadawy, K. M.; Teamah, M. A.; Shehata, A. I.; Hanfy, A. A. (2017). "Simulation of LPG Production from Natural Gas using Fractionation Towers". International Journal of Advanced Scientific and Technical Research. 6 (7). <a href="#fnref:45" class="footnote-back-ref">↩</a></li>
<li id="fn:46">Muneeb Nawaz ‘Synthesis and Design of Demethaniser Flowsheets for Low Temperature Separation Processes,' University of Manchester, unpublished PhD thesis, 2011, pp. 137, 138, 154 <a href="#fnref:46" class="footnote-back-ref">↩</a></li>
<li id="fn:47">Winter, Mark (2008). "Helium: the essentials". University of Sheffield. Retrieved 2008-07-14. <a href="http://www.webelements.com/helium/" target="_blank">http://www.webelements.com/helium/</a> <a href="#fnref:47" class="footnote-back-ref">↩</a></li>
<li id="fn:48">Dwight E. Ward and Arthur P. Pierce (1973) "Helium" in United States Mineral Resources, US Geological Survey, Professional Paper 820, p.285-290. <a href="#fnref:48" class="footnote-back-ref">↩</a></li>
</ol>

Natural-gas processing open-in-new

Natural-gas processing