Mode of transportation of natural gas along the main pipeline

FIELD: the invention refers to energy-conservation technologies of pipeline transportation of natural gas.

SUBSTANCE: it may be used for controlling the technological process of the main pipeline with simultaneous selection out of gas of valuable ethane, propane, butane components. The technical result of the invention is reduction of energy inputs for maintaining pressure in the main pipeline, provision of stabilization of pressure in the main pipeline. The mode of transportation of natural gas along the main pipeline includes its feeding into the main pipeline on the first and the following compressor stations and giving out natural gas from the main pipeline through gas reducing stations and divide it on two flows one of them is directed into the pipeline of high pressure, and the other into a consumer pipe-bend. At that the gas of consumer pipe-bend is preliminary cooled and cleared from condensed and hard fraction, and then further cooling is executed till the temperature below the point of condensation of methane and division of cryogenic liquid and directed to the user, and out of received cryogenic liquid methane is separated from liquid ethane-propane-butane fraction which is returned into the pipeline of high pressure and further into the main pipeline, and detailed methane is directed into the pipe-bend. At that the gas in the pipeline of high pressure is preliminary additionally cooled, compremirated and returned into the main pipeline.

EFFECT: reduces power inputs.

7 cl, 1 dwg

 

The invention relates to energy-saving technologies, pipeline transportation of natural gas and can be used for process control pipeline with simultaneous selection of valuable gas ethane-, propane-, butane components.

The closest to the technical essence and the achieved result is known and accepted in the practice of the method of pipeline transportation of natural gas, including gas production by field, enter it into the pipeline, kompremirovannyj on the first (head) and subsequent compressor stations (CS), which provides the average pressure in the main pipeline of 3.5-7.5 MPa, and delivery to the consumer via the gas reducing station (GDS) with a pressure of 0.6 (1,2) MPa.

(For example: Bportal, OOO, Aphelinid, Smoov, Ashopton, Kahotea, Fundamentals of energy-saving technologies pipeline transportation of natural gas. - M.: state oil and gas University. I.M. Gubkin. 2004. - 3-70) [1] (prototype)

The disadvantages of this process are the high cost of energy (combustion gas) on CA (in the Russian Federation up to 15% of the produced gas), the inability of the method in the presence of high content of ethane-propane-butane fractions (3% or more) in natural gas without selection on the field, complete loss of these fractions when Amersham content, in the case of low profitability or unprofitability of their units in the field. Also the drawbacks include the necessity of heating dekompilirovanie gas at GDS and/or use their inhibitors, hydrate (methanol).

The technical effect is expected from the use of this invention is the reduction of energy consumption (quantity combusted at KS natural gas) to maintain the pressure in the main pipeline, the stabilization of the pressure in the main pipeline despite changes in the quantities of gas to the consumer during the day and seasons of the year, ensuring alignment of the load on the compressors COP, reduction (exception) losses ethane-propane-butane fractions at any percentage of its contents and without separation of the field, simplifying the management of gas transportation system, improving conditionnot supplied to the gas consumer.

To achieve the above effect in the way of transporting natural gas by pipeline, including feeding it into the pipeline, the first and subsequent compressor station and delivery to the consumer through gazoregulirujushchego stations (GDS) of pipelines, natural gas pipeline selected and divided into two streams, one of which healthy lifestyles is between the high pressure pipeline, and the other in consumer outlet, and the gas consumer challenge pre-cooled and cleaned from the droplet and solid fractions, and then produce further cooling to a temperature below the condensation point of methane and separation cryogenic liquid and direct to consumer, and from the resulting cryogenic liquid separating methane from liquid ethane-propane-butane fraction, which returns in the high pressure pipeline and later in the pipeline, as highlighted in the methane sent to the consumer outlet, when the gas is under high pressure pipeline, pre-advanced, cool, komprimiert and return to the main pipeline.

And the fact that the low-pressure gas is passed through an additional heat exchanger on the high pressure pipeline compressor after additional cooling gas of high pressure and optional heating consumer of gas;

the fact that part of the methane demethanization with a high content of13CH4separated as an independent raw materials;

what remained after liquefaction in the unit heavy methane13The IC4gas komprimiert until the pressure in the consumer outlet and direct to consumers;

the fact that the liquefaction part of the consumer gas and the pressure increase castpodder the main gas is carried out on the expander-compressor units;

the fact that the liquefaction part of the consumer gas and increase the pressure for part of the main gas is performed with the use of wave expanders;

and the fact that the cooled part of the main gas obtained in the expander-compressor installation or wave expander high pressure is injected into the pipeline after GDS.

The basis for the implementation of this method consists of two main components: the presence of the bargain, at the present time, energy, pressure drop at GDS and the fact that the boiling point of methane, ethane, propane and butane under normal conditions, respectively (-162°C); (-82°C); (-40° (C) and (-5°).

The first term can be disposed of energy on industrial output expander-compressor units, using it to increase the pressure passing through the gas pipeline, which reduces the required energy for pumping gas through the pipeline, stabilizes the pressure in the main pipeline and evens out the load on the compressors COP. The last two conditions ensure that the increase in gas extraction at GDS (an increase in the degree of decrease of gas pressure in the line after selection at GDS) increase the number of recyclable energy and, hence, the degree of increase of pressure of the main gas. When the reduction of the selection gas is at GDS - the situation is different, but in any case, there is a "pressure" of the main gas is the greater (smaller) the more (less) fell the pressure in the line by taking gas at GDS. Modern expander-compressor unit (corporate governance) allow dekompilirovanie-kompremirovannyj the same gas volume by a factor of 0.8 and above. This gives grounds to assert that the use of this method will allow you to save up to 50% of the energy required for pumping gas through pipelines, especially as compressed in the compressor of the corporate governance gas pre-and/or after compression is cooled in heat exchangers due to the cold gas which has passed the expander, and the cold produced by demethanization liquefied gas, i.e. practically all the energy of the pressure drop at GDS is used to increase pressure in the line after the selection of gas at GDS.

Getting ethane-propane-butane liquid at GDS is also evident based on the above physical properties of gases and the availability of proven technology liquefaction part passing through the GDS gas. Liquefy able to 10-12% of the flowing gas, and the concentration of ethane-propane-butane fractions in liquefied gas increases 10-20 times compared to the original. Since the proposed method is demethanization liquefied gas, i.e. there is an additional refrigerant liquefaction in the W to bring up to 15-17%. In such regimes is to allocate not less than 95% of the ethane-propane-butane fraction from contained. Special methods (absorption high performance absorbents) selection can be significantly enhanced if it is necessary. Due to the return in line on each GDS, as the movement of gas on the highway, the concentration of ethane-propane-butane fractions increases to concentrations at which their selection becomes profitable, that is.

As consumer gas and compromiseby gas heat exchange for the above technological purposes, the consumer receives a "dry" clean gas to the required temperature, while the cost of energy for heating gas consumption and the use of inhibitors of hydrate formation.

The invention differs from known methods of distant transportation of gas described method trunk pipeline transport of gas with a significant reduction of energy consumption and reduction (exception) loss of valuable hydrocarbons. Also improve the operational conditions of pipelines and compressor stations and reduces the need for variation modes of the latter, i.e. simplifies management of the entire system.

First, the proposed approach is to use existing fuel pipelines at the same time as the fuel-produktoprovoda is no loss of valuable products in the selection by the consumer of the fuel components. For the first time a method of passing (without cost) to produce a concentrated raw material for the production of heavy isotope of carbon. The method according to the invention is fully implemented with the use of industrially produced devices and equipment.

The invention is illustrated in the drawing, which shows the major nodes of the technological scheme of implementation of the method according to the invention.

According to the technological scheme of the equipment GDS for implementing the method according to the invention includes a main pipeline - 1; expander - 2; compressor - 3; unit - 4 branches of liquefied natural gas (LNG); recuperative heat exchanger - 5; heat exchanger - 6; block - 7 demethanization; block - 8 Department of heavy methane (13CH4); pipeline (P1) - 9 high pressure; consumer challenge (C2) - 10; the allotment (L3) - 11 gas demethanization; pipe (L4) 12 return ethane-propane-butane fractions.

The method according to the invention is carried out as follows: natural gas pipeline - 1 is selected and divided into two streams in a pipeline (P1) - 9 high pressure and consumer challenge (C2) - 10. Gas consumer challenge (C2) - 10 pre-cooled in the regenerative heat exchanger 5 and is cleaned from the droplet and the solid fraction on separation-filtration system (not shown). Cleaned and pre is varicella cooled gas serves for the actuation pressure and simultaneous cooling expander 2, in which the cooling gas below the point of condensation of methane. Supercooled gas serves to block 4 of the branch liquefied natural gas (LNG), which produces the separation of cryogenic liquid from gas, low-pressure gas on the continuation of the consumer challenge (C2) - 10 through the regenerative heat exchanger 5 and the heat exchanger 6 is sent to the consumer. Received cryogenic liquid serves in block 7 of demethanization where they separate the methane from the liquid ethane-propane-butane fraction, using the evaporation of methane gas heat, high pressure, passed through a compressor - 3, installed on the pipeline (P1) - 9 high pressure. The remaining cryogenic ethane-propane-butane fluid return pipeline (P1) - 9 high pressure; by ejection or a cryogenic pump (not shown). Ethane-propane-butane liquid is gasified in the pipeline (P1) - 9 high pressure while lowering the temperature of the gas after the compressor. Pre-cooled first gas stream pipeline (P1) - 9 high pressure after the compression and additional cooling with a higher pressure than the main return to main pipe 1 in an optimal way (e.g., by a well-known principle of the jet pump compressor), resulting compensate (partially compensate) Pade is their pressure gas main pipeline 1, the incident by taking consumer of gas. The resulting demethanization in block 7 of demethanization methane sent to the consumer outlet.

Gas demethanization can pass through an additional heat exchanger in the consumer challenge than advanced obespechivajut the pre-cooling gas before the expander (not shown).

Low-pressure gas can pass through an additional heat exchanger in the pipeline (P1) - 9 high pressure after the compressor, which provides additional cooling of high pressure gas and an additional heater consumer of gas (not shown).

In the process of liquefaction of natural gas along with the ethane-propane-butane fraction in block 4 of the branch liquefied natural gas (LNG) in the liquid increases the concentration of heavy methane (13CH4due to the fact that the boiling point of heavy methane is higher than methane with a light isotope of carbon. For the same reason, in the process of demethanization the concentration of heavy methane in the liquid (at the bottom of the column block - 7 demethanization) also increases. Using this fact, at the experimentally determined plate columns demethanization selected methane with high concentration of heavy methane which is sent in block 8 of the Department of heavy methane (13CH4, by throttling the gas and re-liquefaction of part of selected liquid with a maximum concentration of heavy methane. Remaining after liquefaction in the unit heavy methane gas komprimiert until the pressure in the consumer challenge (C2) - 10 and sent to the customer (not shown).

The remaining liquefied gas can be actinovate in consumer drain (not shown).

Thus, in the invention for the first time provided the use of fuel gas as fuel pipelines without loss of valuable hydrocarbons in the selection of the fuel gas to the consumer. This invention eliminates the need for costly construction of new gas separation and processing facilities in remote gas and gas condensate fields with a high content of ethane-propane-butane fractions. Simultaneously, the invention eliminates the need for separate transportation detachable fields of fractions and/or products of their processing remote from the consumer of the regions where deposits. However, due to the accumulation of valuable fractions in main pipelines road transport, there is a possibility of profitable from the selection, even if the initial concentration was low and did not provide them cost-effective the Department is s when using modern equipment and technology.

At the same time significantly reduces the cost of energy (the amount of burned natural gas)required for the transportation of gas through pipelines, stabilize the pressure in them, are aligned load on the compressor main compressor stations. As a result, simplifies the whole system management transportation gas, increase the operating life of the system without replacement of its elements.

Finally, there is a possibility of side (without cost of energy, raw materials and refrigerants) separation of a concentrate containing a heavy isotope of carbon, expensive raw material for medicine and other industries.

1. The method of transporting natural gas by pipeline, including feeding it into the pipeline, the first and subsequent compressor station and delivery to the consumer via the gas-reducing station pipelines, characterized in that the natural gas pipeline selected and divided into two streams, one of which is sent to the high pressure pipeline, and the other in consumer outlet, and the gas consumer challenge pre-cooled and cleaned from the droplet and solid fractions, and then produce further cooling to a temperature below the condensation point of methane and separation cryogenic liquid and direction is given to the consumer, and from the resulting cryogenic liquid separating methane from the liquid itemproperties faction, which has returned to the high pressure pipeline and later in the pipeline, as highlighted in the methane sent to the consumer outlet, when the gas is under high pressure pipeline, pre-advanced, cool, komprimiert and return to the main pipeline.

2. The method according to claim 1, characterized in that the low-pressure gas is passed through an additional heat exchanger on the high pressure pipeline compressor after additional cooling gas of high pressure and optional heating consumer of gas.

3. The method according to claim 1, characterized in that the part of the methane demethanization with a high content of13CH4separated as an independent raw material.

4. The method according to claim 1, characterized in that remaining after liquefaction in the unit heavy methane13CH4gas komprimiert until the pressure in the consumer outlet and direct to the consumer.

5. The method according to claim 1, characterized in that the liquefaction part of the consumer gas and increase the pressure for part of the main gas is carried out on the expander-compressor units.

6. The method according to claim 1, characterized in that the liquefaction part of the consumer gas and increasing the pressure the Oia for part of the main gas is performed with the use of wave expanders.

7. The method according to claim 1, characterized in that the cooled part of the main gas obtained in the expander-compressor installation or wave expander high pressure is injected into the pipeline after GDS.



 

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