RU2570736C1 - Natural gas or associated petroleum gas processing method - Google Patents

Abstract

FIELD: oil and gas industry.

SUBSTANCE: in the bottom part and/or contact deceives of the rectification tower ultrasound wave field is generated with the preset frequency and power using ultrasound generator, radiation sources of ultrasound wave field with magnetorestrictive ore piezoceramic converters and waveguides, natural gas or associated petroleum gas is separated into methane fraction and broad fraction of light hydrocarbons at the preset pressure and temperature and the broad fraction of light hydrocarbons is separated.

EFFECT: increased transfer rate in the rectification tower, improved intensity of vapour phase generation and clarity in separation of natural gas or associated petroleum gas thus reducing number of baffle pans and power of heating equipment.

6 cl, 2 dwg

Description

The invention relates to the production of ethane fraction, liquefied petroleum gas (hereinafter - LHG) and the preparation of natural or associated petroleum gas for the production of liquefied natural gas (hereinafter - LNG) and can be implemented at the facilities of the oil, petrochemical and gas industries, mainly in factories and installations for the preparation and processing of oil, natural and associated petroleum gases, a wide fraction of light hydrocarbons (hereinafter - BFLH), including for the production of LNG, LPG and ethane fraction (as oil and gas chemical raw materials).

A known method of separating hydrocarbon fractions in a distillation column with heaters (furnaces) (see Murin V.I., Kislenko N.N., Surkov Yu.V., Afanasyev A.I., Afanasyev Yu.M., Bekirov T.M. ., Barsuk S.D., Blinov V.V., Grunvald V.R., Ismaylova H.I., Nabokov S.V. Nabutovsky Z.A., Podlegaev N.I., Stryuchkov V.M., Fishman LL Processing of natural gas and condensate: Reference: At 2 p.m. - M .: Nedra-Biznescentr LLC, 2002. - Part 1. - 517 p.: Ill.).

Closer is the method of separation of natural gas or associated petroleum gas by distillation into methane fraction and BFLH in a distillation column with heaters (furnaces) (see source indicated above.).

The disadvantage of the above methods is the use of heaters (furnaces) in the separation of hydrocarbon distillation columns, which leads to the need to use natural gas as a fuel, significant heat and energy costs and environmental pollution by combustion products, to complicate the process flow of the rectification process.

The objective of the claimed invention is to create a method of processing natural or associated petroleum gas, the implementation of which will reduce energy costs for the processing of these raw materials, increase the rate of mass transfer in a distillation column, and also reduce the metal consumption of the distillation column.

The technical result of the claimed invention is to increase the rate of mass transfer in a distillation column, as well as the intensity of the vapor phase formation and the clarity of separation of natural or associated petroleum gas, which will reduce the number of distillation plates and the power of the heating equipment.

The technical result is ensured by the fact that in a method for processing natural or associated petroleum gas, comprising separating natural or associated petroleum gas in a distillation column into a methane fraction and NGL, in the bottom and / or contact devices of the distillation column using an ultrasonic generator and ultrasonic wave emitters with magnetostrictive or piezoceramic transducers and waveguides create an ultrasonic wave field with a given frequency and power , separate natural or associated petroleum gases into the methane fraction and NGL at given pressure and temperature and separate NGL.

The claimed method is also characterized by the fact that NGL is separated into an ethane fraction, mainly containing ethane, and a C3 + fraction in a distillation column at pressures from 0.5 to 9.0 MPa, temperatures from -60 to + 20 ° C and when exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW.

The claimed method is also characterized by the fact that NGL is separated into a propane-butane fraction (hereinafter referred to as PBP) and C5 + fractions in a distillation column at pressures from 0.2 to 4.0 MPa, temperatures from -10 to + 40 ° C and when exposed to ultrasound wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW.

The claimed method is also characterized by the fact that NGL is separated into PBP, mainly containing propane, and a butane-butylene fraction (hereinafter referred to as BBP), mainly containing butanes, in a distillation column at pressures from 0.2 to 4.0 MPa, temperatures from -10 up to + 40 ° C and when exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW.

The claimed method is also characterized in that the PBP is separated into propane and BBP in a distillation column at pressures from 0.2 to 4.0 MPa, temperatures from -10 to + 40 ° C and when exposed to an ultrasonic wave field with a radiation frequency from 16 to 100 kHz and power from 0.25 to 10 kW.

The claimed method is also characterized in that the BBP is separated into n-butane and isobutane in a distillation column at pressures from 0.2 to 4.0 MPa, temperatures from -10 to + 40 ° C and when exposed to an ultrasonic wave field with a radiation frequency of 16 up to 100 kHz and power from 0.25 to 10 kW.

The energy of an ultrasonic wave field created using an ultrasonic generator and emitters of a wave ultrasonic field with magnetostrictive or piezoceramic transducers and waveguides, introduced into a shared hydrocarbon system, increases the energy state and reduces the stability of the system, which, in turn, significantly increases compared to thermal heating mass transfer rate, vapor phase formation rate, clarity of separation and, as a result, reduces the number of of distillation trays in the column, i.e. reduce the metal consumption of the distillation column, and the power of the heating equipment, i.e. reduce energy costs for the processing of natural or associated petroleum gas.

Thus, when implementing the inventive method, energy costs are reduced by 40-50%, the mass transfer rate in the distillation column is increased by 3-10 times, and the metal consumption of the distillation column is reduced by 15-25%, which is confirmed by calculated and experimental data.

A schematic diagram illustrating the operation of the claimed method is shown in FIG. 1, and in FIG. 2 shows a section aa in figure 1, where:

1 - distillation column;

2 - an ultrasonic generator;

3 - emitters of a wave ultrasonic field with magnetostrictive or piezoelectric transducers and waveguides;

and for better understanding in roman numerals the following streams are indicated:

I - raw materials;

II - distillate;

III - the remainder.

The essence and operation of the claimed method is illustrated by the following examples.

EXAMPLE 1

Raw material (natural gas or associated petroleum gas) through line I enters the distillation column 1. Depending on the composition of the raw materials, the technological mode of operation of the distillation column 1 is maintained at pressures from 0.5 to 9.0 MPa and temperatures from -60 to + 20 ° C. The values of temperatures and pressures in the distillation column 1 are determined on the basis of calculation. Depending on the composition of the feed, the hydrocarbon mixture to be separated in the still part of the distillation column 1 is exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW using emitters 3 connected to an ultrasonic generator 2. The indicated frequency values and radiation powers are determined empirically in the framework of a field experiment. From the top of distillation column 1, methane fraction, mainly containing methane, is taken from line II; from the bottom of distillation column 2, NGL is taken from line III. In the distillation column 1, methods are used to create irrigation, based on the use of throttling of the methane fraction leaving the top of the distillation column, or refrigerants. The installation is equipped with the necessary shut-off and / or shut-off and control valves.

EXAMPLE 2

Raw materials (NGL) through line I enter the distillation column 1. Depending on the composition of the raw materials, the technological mode of operation of the distillation column 1 is maintained at pressures from 0.5 to 9.0 MPa and temperatures from -60 to + 20 ° C. The values of temperatures and pressures in the distillation column 1 are determined on the basis of calculation. Depending on the composition of the feed, the hydrocarbon mixture to be separated in the still part of the distillation column 1 is exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW using emitters 3 connected to an ultrasonic generator 2. The indicated frequency values and radiation powers are determined empirically in the framework of a field experiment. An ethane fraction predominantly containing ethane was taken from the top of the distillation column 1 along line II, and the C3 + fraction was taken from the bottom of the distillation column 2 along line III. In the distillation column 1, methods are used to create irrigation based on the use of throttling of the ethane fraction leaving the top of the distillation column or refrigerants. The installation is equipped with the necessary shut-off and / or shut-off and control valves.

EXAMPLE 3

Raw materials (BFLH) through line I enter distillation column 1. Depending on the composition of the raw materials, the technological mode of operation of distillation column 1 is maintained at pressures from 0.5 to 9.0 MPa and temperatures from -10 to + 40 ° C. The values of temperatures and pressures in the distillation column 1 are determined on the basis of calculation. Depending on the composition of the feed, the hydrocarbon mixture to be separated in the still part of the distillation column 1 is exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW using emitters 3 connected to an ultrasonic generator 2. The indicated frequency values and radiation powers are determined empirically in the framework of a field experiment. From the top of distillation column 1, a propane-butane fraction (hereinafter referred to as PBP), mainly containing propane and butanes, is taken from line II of the distillation column 1, and the C5 + fraction is taken from the bottom of distillation column 2 through line III. In the distillation column 1, methods are used to create irrigation, based on the use of throttling of PBP leaving the top of the distillation column, or refrigerants. The installation is equipped with the necessary shut-off and / or shut-off and control valves.

EXAMPLE 4

Raw materials (NGL) through line I enters the distillation column 1.

Depending on the composition of the raw materials, the technological mode of operation of the distillation column 1 is maintained at pressures from 0.5 to 9.0 MPa and temperatures from -10 to + 40 ° C. The values of temperatures and pressures in the distillation column 1 are determined on the basis of calculation. Depending on the composition of the feed, the hydrocarbon mixture to be separated in the still part of the distillation column 1 is exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW using emitters 3 connected to an ultrasonic generator 2. The indicated frequency values and radiation powers are determined empirically in the framework of a field experiment. From the top of distillation column 1 through line II, PBF, predominantly containing propane, is taken; from the bottom of distillation column 2, along line III, a butane-butylene fraction (hereinafter referred to as BBP), mainly containing butanes, is taken. In the distillation column 1, methods are used to create irrigation, based on the use of throttling of PBP leaving the top of the distillation column, or refrigerants. The installation is equipped with the necessary shut-off and / or shut-off and control valves.

EXAMPLE 5

Raw materials (PBP) through line I enter distillation column 1. Depending on the composition of the raw materials, the technological mode of operation of distillation column 1 is maintained at pressures from 0.5 to 9.0 MPa and temperatures from -10 to + 40 ° C. The values of temperatures and pressures in the distillation column 1 are determined on the basis of calculation. Depending on the composition of the feed, the hydrocarbon mixture to be separated in the still part of the distillation column 1 is exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW using emitters 3 connected to an ultrasonic generator 2. The indicated frequency values and radiation powers are determined empirically in the framework of a field experiment. Propane is taken from the top of the distillation column 1 along line II, and BBP, mainly containing butanes, is taken from the bottom of the distillation column 2 along line III. The installation is equipped with the necessary shut-off and / or shut-off and control valves.

EXAMPLE 6

Raw materials (BBF) through line I enters the distillation column 1. The pressure in the distillation column is 0.2-4.0 MPa. Depending on the composition of the raw materials, the technological mode of operation of the distillation column 1 is maintained at pressures from 0.5 to 9.0 MPa and temperatures from -10 to + 40 ° C. The values of temperatures and pressures in the distillation column 1 are determined on the basis of calculation. Depending on the composition of the feed, the hydrocarbon mixture to be separated in the still part of the distillation column 1 is exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW using emitters 3 connected to an ultrasonic generator 2. The indicated frequency values and radiation powers are determined empirically in the framework of a field experiment. Isobutane is taken from the top of the distillation column 1 along line II, and n-butane is taken from the bottom of the distillation column 2 along line III. In the distillation column 1, methods are used to create irrigation based on the use of throttling of isobutane leaving the top of the distillation column, or refrigerants. The installation is equipped with the necessary shut-off and / or shut-off and control valves.

Claims (6)

1. A method of processing natural or associated petroleum gas, which consists in dividing, respectively, natural or associated petroleum gas in a distillation column into a methane fraction and a wide fraction of light hydrocarbons (hereinafter - NGL), characterized in that in the bottom and / or contact devices of the distillation column using an ultrasonic generator and emitters of a wave ultrasonic field with magnetostrictive or piezoelectric transducers and waveguides create an ultrasonic wave th field with given frequency and power, respectively, separated natural or associated gas oil fraction to methane and NGL under given pressure and temperature, and the separated natural gas liquids. 2. The method according to p. 1, characterized in that the NGL is divided into an ethane fraction, mainly containing ethane, and a C3 + fraction in a distillation column at pressures from 0.5 to 9.0 MPa, temperatures from -60 to + 20 ° C and when exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW. 3. The method according to p. 1, characterized in that the NGL is divided into a propane-butane fraction (hereinafter referred to as PBP) and a C5 + fraction in a distillation column at pressures from 0.2 to 4.0 MPa, temperatures from -10 to + 40 ° C and when exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW. 4. The method according to p. 1, characterized in that the NGL is divided into PBP, mainly containing propane, and a butane-butylene fraction (hereinafter referred to as BBP), mainly containing butanes, in a distillation column at pressures from 0.2 to 4.0 MPa , temperatures from -10 to + 40 ° C and when exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW. 5. The method according to any one of paragraphs. 3 or 4, characterized in that the PBP is separated into propane and BBP in a distillation column at pressures from 0.2 to 4.0 MPa, temperatures from -10 to + 40 ° C and when exposed to an ultrasonic wave field with a radiation frequency from 16 to 100 kHz and power from 0.25 to 10 kW. 6. The method according to p. 4, characterized in that the BBP is separated into n-butane and isobutane in a distillation column at pressures from 0.2 to 4.0 MPa, temperatures from -10 to + 40 ° C and when exposed to an ultrasonic wave field with a radiation frequency of 16 to 100 kHz and a power of 0.25 to 10 kW.

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