{"id":1633,"date":"2020-11-25T09:38:51","date_gmt":"2020-11-25T08:38:51","guid":{"rendered":"http:\/\/yvcharron.com\/?page_id=1633"},"modified":"2021-03-20T11:16:25","modified_gmt":"2021-03-20T10:16:25","slug":"gas-treatment","status":"publish","type":"page","link":"https:\/\/yvcharron.com\/index.php\/gas-treatment\/","title":{"rendered":"Gas treatment with two phase turbines – Sour gases, CO2, H2S, physical solvent, hybrid solvent, helico axial turbine, solvent cooling"},"content":{"rendered":"\n

Keywords: gas treatment sour acid physical chemical solvent multiphase turbine let down valve<\/p>\n\n\n\n

1_\nIntroduction<\/strong><\/h2>\n\n\n\n

Processing of a gas, for example, natural gas, synthesis gas, combustion\ngas, gas from integrated combined cycles, generally involves removal of impurities<\/strong> such as nitrogen\n(N2<\/sub>), ammonia (NH3<\/sub>), and acid compounds such as carbon dioxide (CO2<\/sub>), hydrogen\nsulfide (H2<\/sub>S),<\/strong> sulfur dioxide (SO2<\/sub>), COS, CS2 <\/sub>and\nmercaptans. These impurities are present in various proportions depending on\nthe origin of the gas. In the case of natural gas, CO2 <\/sub>and H2<\/sub>S\ncan be present as traces, some ppm, but they can also represent a quite\nsignificant proportion of the raw gas, up to 70% by volume. Other impurities\nsuch as COS, CS2 <\/sub>and mercaptans can also be encountered,\ngenerally, a few thousand ppm.<\/p>\n\n\n\n

According to the initial proportions of impurities in the gas to be\nprocessed, and also according to the specifications required for the processed\ngas, various scrubbing processes are used. Most gas treatment processes use\nsolvents. These solvents can be of physical or chemical nature. Solvents of physical nature<\/strong> are based\non the preferred solubility of the impurities in the solvent and are therefore\nfavoured by the high partial pressures of the impurities in the gas to be\nprocessed. Solvents of chemical nature<\/strong>\nare ideally used to reach the strictest specifications for the processed gas,\nby chemical consumption of the species absorbed by reaction with an active\nagent contained in the absorption solvent. There are also solvents of hybrid nature<\/strong> consisting of a mixture of physical and\nchemical solvents so as to cumulate the advantages of these two solvents.<\/p>\n\n\n\n

Whatever the origin of the gaseous effluent to be processed, the\npurification loop generally consists of an impurities collection stage using a\nsolvent and of a solvent regeneration stage. The regeneration stage is\nconditioned by the nature of the solvent used. In the case of a solvent involving a chemical reaction<\/strong>, a thermal regeneration is generally used to\nobtain a sufficient solvent purity<\/strong> allowing the desired specifications to\nbe reached. Thermal regeneration can be preceded by regeneration by expansion\nin order to limit the energy required for thermal regeneration. In the case of\na solvent of hybrid or physical nature<\/strong>,\nregeneration is essentially carried out\nby expansion<\/strong>, possibly completed by a thermal regeneration stage.<\/p>\n\n\n\n

The present document describes the improvement of solvent regeneration. It results from the expansion of laden solvents through two-phase turbines instead of letdown valves. This improvement is particularly significant with physical (or hybrid) solventsand with two phase turbines of the rotodynamic type<\/strong>.<\/p>\n\n\n\n

_<\/p>\n\n\n\n

2_ Gas\ntreatment principle and variants<\/strong><\/h2>\n\n\n\n

The treatment process is applied to a gas comprising various types of impurities.\nThese latest may be CO2<\/sub>, H2<\/sub>S, SO2<\/sub>, COS, CS2<\/sub>,\nmercaptans, N2 <\/sub>and NH3<\/sub>.<\/p>\n\n\n\n

2-a\n\u2013 BASIC CONFIGURATION –<\/strong>\nThe treatment process is carried out with the use of a single two-phase turbine\nsection through the following steps:<\/p>\n\n\n\n

a) contacting the gas<\/strong> with a\nsolvent absorbing the impurities so as to obtain an impurity-laden (charged) solvent\nand a scrubbed (cleaned) gas. The solvent may be of a physical or hybrid\nnature.<\/p>\n\n\n\n

b) expanding the impurity-laden solvent\nthrough a two-phase turbine<\/strong> so as to release an amount of impurities in\ngaseous form and to obtain an impurity-depleted solvent. The two-phase turbine section\nmay be of a rotodynamic type comprising one or several stages, each stage\nincluding one impeller (rotating element) and one diffuser (fixed element).<\/p>\n\n\n\n

c) separating<\/strong> these impurities\nfrom the impurity-depleted solvent.<\/p>\n\n\n\n

2-b\n\u2013 VARIANT 1 – <\/strong>Depending on gas\ncharacteristics and separation efficiency requirement, the system may include two\nadditional steps: <\/p>\n\n\n\n

d) expanding the solvent<\/strong>\noutleting the separation vessel c) through\na second two-phase turbine section<\/strong> so as to release a second amount of\nimpurities in gaseous form and to obtain an expanded solvent in a more purified\ncondition. As per step b), the two-phase turbine used in this step d) may\ncomprise one or several stages. The two turbine sections may be mounted on a\nsingle shaft and in the same casing.<\/p>\n\n\n\n

e) separating<\/strong> the second amount\nof impurities from said expanded solvent.<\/p>\n\n\n\n

2-c\n\u2013 VARIANT 2 – <\/strong>The regeneration\ncycle may be improved by using the following steps: <\/p>\n\n\n\n

f) distilling said impurity-depleted\nsolvent<\/strong> so as to separate the impurities from the solvent,<\/p>\n\n\n\n

g) recycling the distilled solvent<\/strong>\nto step a).<\/p>\n\n\n\n

The contacting vessel used in step a) can operate at a pressure ranging, in most cases, between 1 MPa abs. and 15 MPa abs. while in step b) the solvent can be expanded to a pressure ranging between 0.1 MPa abs. and 3 MPa abs.<\/p>\n\n\n\n

_<\/p>\n\n\n\n

3_ Detailed\ndescription<\/strong><\/h2>\n\n\n\n

3-a\n\u2013 Basic configuration with a single two phase turbine section<\/strong><\/p>\n\n\n\n

The operating principle of this configuration is presented in figure 1. The gas to be processed (comprising impurities) flows through line 10<\/strong>. It is possibly cooled in heat exchanger E1<\/strong> then fed through line 11<\/strong> into absorption column C1<\/strong>. The gas is then contacted with a liquid solvent fed through line 18<\/strong> into the top of column C1<\/strong>. The solvent absorbs the impurities contained in the gas. The scrubbed gas, i.e. depleted in impurities, is discharged at the top of column C1<\/strong> through line 19<\/strong>.<\/p>\n\n\n\n

\"Gas

Figure 1 \u2013 Gas treatment in basic configuration <\/figcaption><\/figure><\/div>\n\n\n\n

The solvent can be of physical or chemical nature. For example, it may be\nan alcohol, a glycol, a heavy hydrocarbon such as propylene carbonate, a\npotassium carbonate, a morpholine, a polyethylene glycol dimethylether, an\namine such as an alkanolamine or an alkylamine. The solvent can also be a mixture\nof two or more aforementioned solvents.<\/p>\n\n\n\n

The liquid impurity-laden solvent is discharged from column C1<\/strong> through\nline 12<\/strong> then expanded in two-phase turbine T1<\/strong>. The expanded\nsolvent is fed into separating drum B1<\/strong>. The impurities released in\ngaseous form upon expansion are discharged at the top of drum B1<\/strong> through\nline 20<\/strong>.<\/p>\n\n\n\n

The liquid solvent recovered at the bottom of drum B1<\/strong> through\nline 13<\/strong> is depleted in impurities. It can be pressurized by\npump P1<\/strong> then fed through line 18<\/strong> to the top of column C1<\/strong>.\nExpansion in turbine T1<\/strong> presents the advantage of cooling the\nsolvent. However, if the regenerated solvent is not sufficiently cold, it can\nbe super cooled by heat exchanger E5<\/strong> prior to being fed into column\nC1<\/strong>.<\/p>\n\n\n\n

3-b\n\u2013 Variant 1 using an additional two phase turbine section<\/strong><\/p>\n\n\n\n

The operating principle of this configuration is presented in figure 2. The stages carried out in exchanger E1<\/strong>, column C1<\/strong>, turbine T1<\/strong> and\ndrum B1<\/strong> of figure 2 are identical to the stages carried out in figure 1.<\/p>\n\n\n\n

In figure 2, the liquid solvent coming from the bottom of drum B1 <\/strong>through\nline 13<\/strong> is expanded in two-phase turbine T2<\/strong>. The\nexpanded solvent is fed into separating drum B2<\/strong>. The impurities released\nin form of gas upon expansion are discharged at the top of drum B2<\/strong> through\nline 21<\/strong>. The liquid solvent recovered at the bottom of drum B2<\/strong> through\nline 14<\/strong> is depleted in impurities. It can be pressurized by\npump P2<\/strong> (not represented) then fed through line 18<\/strong> to\nthe top of column C1<\/strong>.<\/p>\n\n\n\n

\"Gas

Figure 2 \u2013 Gas treatment with variants 1 and 2 <\/figcaption><\/figure><\/div>\n\n\n\n

3-c\n\u2013 Variant 2 using a distillation column<\/strong><\/p>\n\n\n\n

Expansion in turbine T2<\/strong> is optional, which means that, in the\nmethod described in connection with figure 2, elements T2<\/strong>, B2<\/strong> and 21<\/strong> can\nbe removed and line 13<\/strong> can be directly connected to line 14<\/strong>.<\/p>\n\n\n\n

The liquid solvent recovered at the bottom of drum B2<\/strong> through\nline 14<\/strong> is depleted in impurities. It is heated up in heat\nexchanger E4<\/strong> then fed into distillation column C2<\/strong>. The\ndistillation column allows to carry out advanced regeneration of the solvent,\ni.e. to reduce the proportion of impurities in the solvent to a very low level,\nin any case to a lower level than that obtained by means of regeneration by\nexpansion. Reboiler E2<\/strong> provides the heat required for distillation\nin column C2<\/strong>. The gas phase discharged at the top of column C2<\/strong> through\nline 15<\/strong> mainly comprises impurities. This gas phase is partly\ncondensed by cooling in heat exchanger E3<\/strong> then fed into separating drum\nB3<\/strong>. A gas phase mainly comprising impurities is discharged from drum B3<\/strong> through\nline 17<\/strong>. The condensates recovered at the bottom of drum B3<\/strong> are\ninjected through line 16<\/strong> to the top of column C2<\/strong> as\nreflux.<\/p>\n\n\n\n

The regenerated solvent available at the bottom of column C2<\/strong> is pumped by pump P1<\/strong>, cooled in heat exchanger E4<\/strong>, then injected to the top of absorption column C1<\/strong>. Expansion in turbines T1<\/strong> and T2<\/strong> has the advantage of cooling the solvent. Thus, the solvent obtained after expansion constitutes a coolant for cooling the regenerated solvent intended to be fed into column C1<\/strong>. However, if the regenerated solvent is not sufficiently cold, it can be super cooled by heat exchanger E5<\/strong> prior to being fed into column C1<\/strong>.<\/p>\n\n\n\n

_<\/p>\n\n\n\n

4_ Benefit\nof two phase turbines<\/strong><\/h2>\n\n\n\n

In the methods described in connection with figures 1 and 2, expansion of\nthe solvent is carried out by means of two-phase turbines T1 and T2. These turbines are of the rotodynamic type and more precisely of the\nhelico axial type. This turbine type provides the following advantages:<\/p>\n\n\n\n

  1. The pressure let down through turbines allows to release impurities in a gaseous form<\/strong>.<\/span><\/li>
  2. Expansion of the solvent by means of a turbine is accompanied by a temperature reduction of the solvent<\/strong> due to an expansion of the gas produced during the letdown. As a first approximation, expansion by means of a turbine is close to an isentropic process. This cold production allows to compensate for the temperature increase in the absorption column during the absorption reaction which is generally exothermic<\/strong>.<\/span><\/li>
  3. From the above it results that the use of two phase turbines permits to cancel or reduce the demand for an external cooling. The system may be designated as an auto thermal process<\/strong>. For example, when the solvent is regenerated only by expansion<\/em><\/strong>, the solvent obtained after expansion requires no or only a low temperature reduction before injection of the solvent into the absorption column. Similarly, when the solvent is regenerated by expansion and \u00a0distillation<\/em><\/strong>, the solvent obtained at low temperature after expansion constitutes a coolant allowing to cool the high-temperature regenerated solvent from the distillation column.<\/span><\/li>
  4. Expansion energy<\/strong> may be recovered at the shaft end of the two-phase turbine. This energy may be used for driving the solvent pump P1<\/strong>\u00a0and\/or for recompressing the impurities in gaseous form circulating in lines\u00a020<\/strong>\u00a0and\u00a021<\/strong>\u00a0at the outlet of drums B1<\/strong>\u00a0and B2<\/strong>.<\/span><\/li><\/ol>\n\n\n\n

    The two-phase turbines<\/strong> mentioned in the above processes are of the rotodynamic type. As a consequence, they can handle, mechanically wise, all gas fraction values (from 0 to 100 %)<\/strong> produced during solvent expansion. This mechanical property is generally not attributed to volumetric turbines (piston, gear).<\/p>\n\n\n\n

    During solvent expansion the gas fraction varies largely<\/strong>. It increases from 0% at turbine entrance (solvent strictly in a liquid phase condition) to a high gas fraction for which the value depends on the gas and solvent characteristics but also on the expansion conditions (pressure and temperature). The large gas fraction increase during solvent expansion corresponds to a large volume flow increase from the turbine entrance to its exit. This requires some geometrical adaptation at each hydraulic stage (impeller and diffuser) resulting with small dimensions at the inlet and large ones at the outlet. At the first stage, the impeller diameter is relatively small well adapted to the compression of a mixture with a large molecular weight (low gas fraction). To the contrary, at the last stage, the impeller diameter is relatively large well adapted to the compression of a mixture with a low molecular weight (large gas fraction) Geometrically wise, the rotor of the turbine presents some sort of conical shape with the impeller diameter increasing continuously from turbine inlet to outlet. <\/p>\n\n\n\n

    _<\/p>\n\n\n\n

    5_ Conclusion<\/strong><\/h2>\n\n\n\n

    The replacement of letdown valves by two phase turbines<\/strong> in a gas treatment system presents numerous advantages: a) the letdown of a laden solvent permits to release the impurities in a gas form; b) the release of this gas phase during let down generates an expansion of the gas providing some cooling of the solvent; c) the solvent regeneration approaches an auto thermal process; d) with the use of a distillation tower, the purified solvent may be cooled at the outlet of the boiling phase; e) the energy produced during the two phase expansion of the laden solvent may be used for pumping the solvent or for compressing the gas containing impurities.<\/p>\n\n\n\n

    \"yves<\/figure><\/div>\n\n\n\n

    _<\/p>\n","protected":false},"excerpt":{"rendered":"

    Keywords: gas treatment sour acid physical chemical solvent multiphase turbine let down valve 1_ Introduction Processing of a gas, for example, natural gas, synthesis gas, combustion gas, gas from integrated combined cycles, generally involves removal of impurities such as nitrogen (N2), ammonia (NH3), and acid compounds such as carbon dioxide (CO2), hydrogen sulfide (H2S), sulfur…
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