Method of field preparation of a condensate-gaseous fluid and de-ethanization of the condensate

FIELD: natural gas industry.

SUBSTANCE: the invention is pertinent to the field of natural gas industry and may be used for the field preparation of products of gas condensate pools. The method provides for separation of a gas with a delivery and a low-temperature stage of separation, a phase separation of a condensate of a delivery and low-temperature stages of separation, degassing of a condensate and de-ethanization of a condensate in an evaporating rectifying column. The whole volume of a delivery stage of separation after a preliminary degassing and heating in a recuperative heat exchanger is fed into the middle part the evaporating rectifying column as a feeding. The condensate of the low-temperature stage of separation is divided into two streams. The first stream is fed into the upper part of the evaporating rectifying column as a sprinkling, the second stream is fed in the degasator. Adjustment of the technological mode and composition of products of de-ethanization depending on output and compositions of the condensate of the delivery and a low-temperature stages of separation is conducted by a change of volumes of the streams. The technical result is - maximum degree of separation of the de-ethanizated condensate at minimum losses with a dried gas.

EFFECT: the invention ensures maximum degree of separation of the de-ethanizated condensate at minimum losses with a dried gas.

1 dwg

 

The invention relates to the field of gas industry and can be used for commercial preparation of the products of gas condensate deposits.

There is a method of preparation of the products of gas-condensate wells by the method of the NTS with the degassing of the condensate distillation Stripping column at relatively high pressures ("Technology of processing of gas and condensate," Timbalero, Gaglanzgav, Moscow, Nedra, 1999, pages 332-334), including input and low-temperature separation stage, the degassing of the condensate Stripping distillation column, for the food which is served condensate from the inlet separator, and the water condensate from the low-temperature stage of separation, gas degassing is returned to the input of the low-temperature separation stage using ejection.

The disadvantages of this method are the high energy consumption for heating cube Stripping distillation column due to its operation at relatively high pressures and zateplenie” low-temperature separation stage gas degassing withdrawn from the Stripping distillation column at a relatively high temperature, resulting in the provision of conditionnot dry gas is impossible.

The closest analogue to the proposed technical solution is the method of preparation and processing uglevodorodnogo the raw material gas condensate deposits (patent No. 2182035), including input and low-temperature separation stage, the ejection gases degassing, deethanization condensate distillation Stripping column, power and irrigation which is the mixed condensate inlet and the low-temperature separation stage, and for irrigation of condensate served cold, and in the power part is preheated in a recuperator, kompremirovannyj gas directly and then cooled in the air cooler and regenerative gas-liquid heat exchanger and return to the input of the low-temperature stage of separation.

The disadvantage of this method are increased technological losses of liquid hydrocarbons (pentane + higher) gas directly due to the contact of the upper plate Stripping distillation columns exhaust gas from the column with heavy components and fractions deethanizing condensate, and also increased the probability of paraffin on the top plates of the Stripping distillation column (due to feed them chilled condensate containing heavy fractions) and in the low-temperature stage of separation (in the case of droplet entrainment of heavy fractions applied to the irrigation of condensate from gas directly).

The task of the invention is the optimization of technology the AI field gas condensate deposits and directly allocated condensate, providing flexible control process depending on the composition of the extracted gas condensate fluid.

The technical result for the solution of which the invention is directed, ensuring maximum selection deethanizing condensate with minimal technological losses of propane, butane and liquid hydrocarbons C5+ with dried gas, minimal risk of loss and paraffin and minimum energy consumption.

The task and the technical result is achieved by the fact that in the known method of preparing gas-condensate fluid and directly condensate, including two-stage separation of gas from the inlet and a low temperature stage separation, phase separation of the condensate inlet and the low-temperature stages of separation, the degassing of the condensate and deethanization condensate Stripping distillation column, unlike the prototype of all condensate from the input stage of separation after the preliminary degassing and heated in a recuperator serves in the middle part of the Stripping distillation column as a power supply, the low-temperature condensate separation stage is divided into two streams, the first serves in the upper part of the Stripping distillation column as irrigation, and the second in the crystallizer, the adjustment of the process conditions and composition ol the products directly depending on the yields and compositions of the condensate inlet and the low-temperature stages of separation is realized by changing the volume flow based on the relation 0< V2/V1<1, where V1- the volume of flow of condensate to the low stage of separation in the upper part of the Stripping distillation column, V2- volume flow of low-temperature condensate separation stage to the input of the degasser, the second stream is pre-heated in a regenerative gas-liquid heat exchanger with compressed gas directly, measuring the degree of heating partial vipasyana regenerative gas-liquid heat exchanger through this additional regulation of process conditions and compositions of the products directly condensate and at the same time providing the necessary cooling of the compressed gas directly returned to the input of the low-temperature stage of separation.

The drawing shows a schematic diagram of the method for the commercial preparation of gas-condensate fluid and directly condensate.

The circuit includes an input stage separation 1, recuperative gas heat exchanger 2, the ejector 3, the low-temperature stage separation 4, three-phase separator condensate inlet separation stage 5, the three-phase separator condensate low-temperature separation stage 6, degasser 7, recuperative heat exchanger 8, a Stripping distillation column for directly condensate 9, gas compressor 10 directly, the device is zaushnogo cooling 11 and regenerative gas-liquid heat exchanger 12.

The method is implemented as follows. Production of gas condensate wells with pressure up to 16 MPa in the inlet separator 1, where separate water from gas and condensate. The separated gas is cooled in the regenerative gas heat exchanger 2, drossellied in the ejector 3 to pressure from 5.5 to 8.5 MPa and served in the low-temperature separator 4. Drained the gas after the low-temperature separator 4 is heated in a regenerative gas heat exchanger 2 and output as a commercial product.

Unstable condensate (NC) of the input stage of separation 1 drossellied to a pressure below the pressure in the low-temperature separation stage 4 and serves in a three-phase separator condensate input stage of separation 5. The TC of the low-temperature separation stage 4 drossellied to a pressure of not more than two times lower than the output pressure of the ejector 3 and serves in a three-phase separator condensate low-temperature separation stage 6. In three-phase separators condensate inlet and the low-temperature stages of separation 5 and 6 produce separation from NC photometering solution (BMP) and partially Tegaserod NC (due to the metered pressure relief after separators). Gas degassing of the three-phase separators condensate inlet and the low-temperature stages of separation 5 and 6 return to the line of the drying gas from treif the EIT separator condensate inlet separation stage 5 it is served in the gas stream after the ejector 3 to the low-temperature stage separation 4 under its own pressure, of the three-phase separator condensate low-temperature separation stage 6 serves on the ejector 3 as a passive gas.

To prevent condensation in gathering systems and gas used odometery solution (BMP). Injection of BMP perform at wellhead (in the case of gas plumes in the hydrated mode), and also before the regenerative gas heat exchanger 2. With the aim of reducing the consumption of methanol using scheme recirculation BMP from the separator second stage: fresh concentrated BMP injected into the gas stream before recuperative gas heat exchanger 2 to prevent condensation at the lowest temperatures, and partly BMP exhaust from the three-phase separator condensate low-temperature separation stage 6 (with a sufficiently high concentration of methanol) use re - directed to the wellheads. In the input stage of separation 1 make separation from the gas flow to the main mass of water. Of the three-phase separator condensate inlet separation stage 5 fully exhaust BMP (with a minimum concentration of methanol) away from installation to disposal.

All of the TC of the three-phase separator condensate input stage of separation 5 drossellied to a pressure of not more than two times lower than the output pressure of the ejector 3 and send the degasser 7. Gas degassing of the degasser 7 combined with a stream of gas degassing of the three-phase separator condensate low-temperature separation stage 6 and serves on the ejector 3 as a passive gas. Weathered condensate (MC) of the degasser 7 heat detalizirovannym condensate regenerative heat exchanger 8 and is served in the middle part of the Stripping distillation column 9 as a power supply.

MK from the three-phase separator condensate low-temperature separation stage 6 is divided into two streams. The first stream is gradually heated in a regenerative gas-liquid heat exchanger 12 by the compressed gas directly and served in the upper part of the Stripping distillation column 9 as cold irrigation. For regulating the degree of heating a portion of the condensate is passed by regenerative gas-liquid heat exchanger 12 through the bypass, and then mixed with pre-heated in a regenerative gas-liquid heat exchanger flow and further mixed stream to a specified temperature, which regulate the ratio of costs to be heated and bypasing flows, served in the upper part of the Stripping distillation column 9 as irrigation.

Use as irrigation Stripping distillation column 9 cold light condensate from the low-temperature separation stage (instead of the more heavy the CSOs mixed flow input and the low-temperature stages of separation) allows to minimize the selection of liquid hydrocarbons C5+ gas directly and, accordingly, their technological losses from drained marketable gas in the absence of gas comes into contact directly with the heavy fractions of the condensate on the top plates of the Stripping distillation column 9, and to prevent waxing the top of the Stripping plates of the distillation column and drip ash heavy fractions of the condensate from the gas directly in the low-stage separation 4, which also prevents the deposition and the deposition of paraffins. Temperature control supplied to the Stripping distillation column 9 irrigation helps to ensure optimal technological mode directly condensate and the desired degree of separation of hydrocarbons.

The second stream of condensate from the three-phase separator condensate low-temperature separation stage 6 serves together with the condensate from the three-phase separator condensate inlet separation stage 5 in the degasser 7. Depending on the composition of the extracted fluid, the ratio of the volume flows can change within the following range: 0<V2/V1<1, where

V1- volume flow of low-temperature condensate separation stage 4 in the upper part of the Stripping distillation column 9, V2- volume flow of low-temperature condensate separation stage 4 at the input of the degasser 7. Regulirovaniya threads allows the flexibility to regulate and ensure the optimal technological mode directly condensate and the desired degree of separation of hydrocarbons.

Gas directly from the top of a Stripping distillation column 9 is compressed by the gas compressor 10 directly to a pressure of 0.2-0.5 MPa higher than the pressure in the low stage of separation (the amount of hydraulic losses), cooled in an air cooler (DAC) 11, Doklady regenerative gas-liquid heat exchanger 12 and fed to the input of the low-temperature separation stage 4. For regulating the degree of cooling gas directly after the air cooling unit 11 is divided into two streams, one of which passed through a regenerative gas-liquid heat exchanger 12 and is cooled therein, and the second without direct cooling by-pass mixing with the cool flow of the regenerative gas-liquid heat exchanger 12. Next, a mixed gas stream directly to a specified temperature, which regulate the ratio of the volume of cooled and bypasing streams fed to the input of the low-temperature separation stage 4.

Defnitively condensate away from the installation as a commercial product for stabilization and further processing.

Recirculation gas directly (return it to the stream of dried gas) significantly improves the quality of separation of the components of the extracted raw material: increases the concentration of ethane in dry natural gas and reduces to a minimum its content is detalizirovannoi condensate. As a result, increases the calorific value of marketable gas (while maintaining the desired dew point). In addition, provided a low content of gaseous hydrocarbons (methane and ethane) in detalizirovannoi condensate, allowing it to stabilize to get propanebutane fraction (LPG)in satisfying the requirements of the standards for liquefied gases, household use (methane and ethane, and other characteristics), without resetting the flare gas stabilisation.

The way the commercial preparation of gas-condensate fluid and directly condensate, including two-stage separation of gas from the inlet and a low temperature stage separation, phase separation of the condensate inlet and the low-temperature separation stage, the degassing of the condensate and deethanization condensate Stripping distillation column, characterized in that all condensate from the input stage of separation after the preliminary degassing and heated in a recuperator serves in the middle part of the Stripping distillation column as a power supply, the low-temperature condensate separation stage is divided into two streams, the first serves in the upper part of the Stripping distillation column as irrigation, and the second in the degasser, the adjustment of the process conditions and the composition of products Deaton the organizations depending on the yields and compositions of the condensate inlet and the low-temperature stages of separation is realized by changing the volume flow, based on the relation 0<V2/V1<1, where V1- the volume of flow of condensate to the low stage of separation in the upper part of the Stripping distillation column, V2- volume flow of low-temperature condensate separation stage to the input of the degasser, the second stream is pre-heated in a regenerative gas-liquid heat exchanger with compressed gas directly, measuring the degree of heating partial vipasyana regenerative gas-liquid heat exchanger through this additional regulation of process conditions and compositions of the products directly condensate and at the same time providing the necessary cooling of the compressed gas directly returned to the input of the low-temperature stage of separation.



 

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