Description of design the device

Invention of the gas-oil industry to an drying absorption of hydro carbonic gas

The invention belongs to the gas-oil industry, in particular to an drying absorption of hydro carbonic gas, and can be used in processes of trade and factory handling of hydro carbonic gases. The method includes input in a flow of gas of flying inhibitor of hydrate formation, gas chilling, separation, input in an absorbent flow, removal and regeneration of the fulfilled inhibitor and absorbent. The removed flows of the fulfilled inhibitor and absorbent unite and send to a gas flow in the beginning of process, separate and give the allocated phase of saturated absorbent on regeneration. At the same time as flying inhibitor of hydrate formation use the lowest aliphatic alcohols or ketones, and as absorbent - glycols, or their air, and also mixes of glycols and their air. This invention allows to intensify process of an absorbing drying of gas by decrease in temperature of contact gas - absorbent. 1 z.p.f-la, 1 silt.

The invention belongs to the gas-oil industry, in particular, to an drying and can be used by absorption of hydro carbonic gas in processes of trade and factory handling of hydro carbonic gases.

The methods of an absorbing drying of hydro carbonic gas using as DEG absorbent - diethyl glycol [see Gukhman L. M. are known. Preparation of gas of northern fields for distant transport. - L.: A subsoil, 1980, page 89] or the TAG - Len glycol [see Kramer D. L., Cook of U. R. Osushk of gas: optimization of work of the operating installations, in. "Oil, gas and petro chemistry abroad", 1981, N2, page 16-19]. A lack of these methods is inefficiency of carrying out process in case of high temperatures of contact gas-absorbent (higher than 25 and 35oC for DEGA and the TAG, respectively).

In a number of almost important cases application of these methods doesn't provide the requirement for indicators of quality of the drained gas (on drying depth).

Also the method of an absorbing drying of natural gas directed to increase in efficiency of process at the expense of a possibility of carrying out absorption at lower temperatures of contact is known. The method includes input of methanol in a gas flow for prevention of hydrate formation, gas chilling, input of the concentrated absorbent (glycol) in an absorber and regeneration of the fulfilled solutions of glycol and methanol [see the Express train - information. Gas industry. The Transport series, conversion and use of gas in the national economy, M., 1984, the issue 10, page-1-6].

Lack of this method is need of input of a large amount of methanol for implementation of a possibility of chilling of sour gas without formation of gas hydrates (the consumption of methanol constitutes from 0,3 kg to 0,6 kg for 1000 nm3 the processed gas at temperatures of contact from 10 to 5oC and working pressure in an absorber of 6,0 MPas). At the same time more than 65% of the entered methanol are dissolved in the gas phase arriving on an drying in

absorber. Availability in a gas phase of a significant amount of vapors of methanol worsens absorption process indicators since in an absorber there is not only an extraction of steam moisture, but also methanol vapors.

Besides, regeneration of the fulfilled methanol is performed by a power-intensive method of rectification on separate installation.

The purpose of the expected invention is the intensification of process of an absorbing drying of gas by decrease in temperature of contact gas-absorbent.

The effective objectives are achieved by what in the known method including input in a flow of gas of flying inhibitor of hydrate formation, gas chilling, separation, input in an absorbent flow, removal of the fulfilled inhibitor and absorbent, the removed flows of the fulfilled inhibitor and absorbent unite and send to a gas flow in the beginning of process, is separated and the allocated phase of saturated absorbent is given on regeneration.

At the same time as flying inhibitor of hydrate formation use the lowest aliphatic alcohols (for example, methanol, ethanol, is propane) or ketones (for example, acetone, methylethylketone), and as absorbent - glycols (for example, ethylene glycol, diethylene glycol, triethyleneglycol, propylene glycol), or their air, and also mixes of glycols and their air.

In the offered method Dryfixol due to input in a gas flow in the beginning of engineering procedure of mix of the fulfilled inhibitors of hydrate formation and absorbent at the same time comes a partial drying of gas (initial moisture content of gas decreases) and saturation by its vapors of flying inhibitor of hydrate formation, and, thus, department of saturated absorbent from inhibitor. The evaporated inhibitor participates in prevention of hydrate formation in case of the subsequent chilling of gas. Thereby repeated circulation of flying inhibitor in the technological scheme is implemented: flying inhibitor evaporates in a flow gas at the beginning of process, is condensed when chilling gas and doulavlivatsya by absorbent in an absorber. Due to reduction of moisture content of gas at the beginning of process and recirculation of flying inhibitor sharp decrease in a required consumption of the fresh concentrated inhibitor entered on feed before a gas chilling stage is provided. Besides, need for regeneration of flying inhibitor of hydrate formation on separate installation as flying inhibitor "samoregenerirutsya" actually in a gas flow in the disappears.course of its recirculation

The method is explained by the drawing of figure 1 on which the scheme of carrying out process of an osushka is represented. The scheme contains the device (1) - a desorber-separator, the device of chilling (2) and an absorber (3).

Perform a method as follows.

Hydrocarbonic gas from wells arrives in the device (1) which includes the lower separation section (the liquid phase beats off here), and the upper contact section where there is an absorption desorption process.

In the upper section of the device (1) mix of the fulfilled solutions of flying inhibitor of hydrate formation and absorbent moves. Here at the same time there is a partial osushka of gas due to absorption of vapors of moisture from gas (i.e. its moisture content decreases, and depending on process parameters moisture content of gas decreases in 1,5 - 2,0 and more times), and also a desorption from a liquid phase of inhibitor of hydrate formation (i.e. evaporation of inhibitor in a gas phase).

At the same time residual content of flying inhibitor in saturated absorbent can be realized very low (% shares) and this size is determined by design features of contact section, and also process parameters. Saturated absorbent is directed to installation of regeneration and returned in a production cycle.

The hydrocarbonic gas which is partially drained and saturated with vapors of flying inhibitor of hydrate formation arrives in the device of chilling (2). It can be the air cooler (AC) that is especially effective in relation to northern gas and gas-condensate fields, or the device of water chilling (it is most acceptable for sea fields), or a refrigeration unit, for example, on propane - a butane cycle. In front of the device of chilling (2) on feed enter into a gas flow in quantity, necessary for prevention of hydrate formation, the concentrated solution of flying inhibitor of hydrate formation. As flying inhibitor of hydrate formation water-soluble organic substance with boiling point 55-120oC, in particular, the lowest aliphatic alcohols (methanol, ethanol, пропанол, isopropanol) and ketones (acetone, methylethylketone) can be used.

Further the cooled gas arrives in an absorber (3) in which lower separation section the water phase of the fulfilled hydrate formation inhibitor separates, and in the upper absorbing section (in which absorbent of required concentration moves) in case of contact absorbent-gas occurs a final osushka of gas up to the required depth (for example, in case of an osushka of natural gas up to the dew point temperature minus 20oC in a colder season according to OST 51.40-93), and also extraction of vapors of inhibitor of hydrate formation. As absorbent glycols (ethylene glycol, diethylene glycol, triethyleneglycol, propylene glycol), air of glycols and azeotropny mixes of glycols and their air can be used.

At the expense of the low temperature of contact gas-absorbent in the device (3) is provided high extent of extraction of vapors of flying inhibitor, and depending on the temperature level of process optimum inhibitor of hydrate formation which technological losses appear at economically acceptable level can be picked up (less than 50 g on 1000 normal m3 of the processed gas). Besides, the low temperature of contact in an absorber (3) promotes extraction by absorbent of heavy C5+ hydrocarbons the highest (to 80% of content in gas). Also requirements of concentration of the regenerated absorbent decrease that simplifies work of installation of regeneration and reduces technological losses of absorbent because of its destruction as temperature in the evaporator of system of regeneration decreases. For the same reason sharpness of a problem of salt sedimentation in system of regeneration of absorbent decreases. The method keeps the efficiency in case of connection of the supercharger (booster compressor station) in front of the chilling device (on figs. 1 connection of the compressor between devices (1) and (2)).

The declared method is checked by technological calculations and tested on installation of an osushka of the Urengoy GKM.

Natural gas of Cenomanian deposits arrived on installation of an osushka with pressure of 6,0 MPas. For chilling of gas used gas AVO. Temperature in an absorber was reduced to minus 5oC, as absorbent used 92-93 Mas regenerated diethylene glycol, concentration. %, giving of the regenerated DEGA in an absorber constituted from 7 to 10 kg on 1000 normal m3 of the processed gas. As flying inhibitor of hydrate formation used methanol, concentration 95 Mas. % which was given before gas AVO. General technological losses of methanol constituted 65-70 g on 1000 normal m3 of the processed gas, technological losses of diethylene glycol decreased from 19 g by 1000 m3 of gas to 14 g on 1000 m3 of gas. Concentration of the saturated DEGA arriving on regeneration installation made 89-90 Mas. %, and residual concentration of methanol in saturated DEGE didn't exceed 0,2-0,3%. Temperature of a dew point of the drained gas constituted minus 22oC.

Whereas in case of implementation of the known method (on a prototype) it was succeeded to reduce gas temperature in an absorber only to plus 5oC (in attempt of further decrease in temperature process of hydrate formation in gas AVO because of strong unevenness of chilling of gas on separate tubes of AVO began). At the same time technological losses of methanol constituted 460 g on 1000 m3 of gas, technological losses of DEGA remained at the level of 19 g / 1000 gas m3. The dew point of the drained gas measured by the device of the condensation Kharkiv-1M type is determined equal minus 14oC.

With use of the received results of trade testing the possibility of application as flying inhibitors of hydrate formation of other aliphatic alcohols is analysed. For example, settlement technological losses of isopropanol in case of the above-stated process parameters constituted 25-30 g on 1000 m3 of gas.

Thus, in the offered method of an absorbing osushka of gas multiple reducing a consumption of flying inhibitor of hydrate formation is provided, the technological operating mode of installation of regeneration of absorbent improves, technological losses of absorbent when preserving indicators of quality of the drained gas at the required technological level (in particular decrease, in case of an osushka of natural gas according to requirements of an industry standard OST 51.40-93).

1. The method of an absorbing drying of hydro carbonic gas including input in a flow of gas of flying inhibitor of hydrate formation, gas chilling, separation, input in the absorbent flow, removal and regeneration of the fulfilled inhibitor and absorbent differing in what the removed flows of the fulfilled absorbent and inhibitor unite and give to a gas flow in the beginning of process, is separated and the allocated phase of saturated absorbent is given on regeneration.

2. A method of an absorbing drying on item 1 differing in the fact that as flying inhibitor of hydrate formation the lowest aliphatic alcohols, for example use methanol, ethanol, пропанол, isopropanol, or ketones, for example acetone, methylethylketone, and as absorbent - glycols, for example ethylene glycol, diethylene glycol, triethyleneglycol, propylene glycol, or their air, and also mixes of glycols and their air.

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