KR20160046591A - Multi section type-LNG Feed gas pre-processing apparatus - Google Patents

Multi section type-LNG Feed gas pre-processing apparatus Download PDF

Info

Publication number
KR20160046591A
KR20160046591A KR1020140142717A KR20140142717A KR20160046591A KR 20160046591 A KR20160046591 A KR 20160046591A KR 1020140142717 A KR1020140142717 A KR 1020140142717A KR 20140142717 A KR20140142717 A KR 20140142717A KR 20160046591 A KR20160046591 A KR 20160046591A
Authority
KR
South Korea
Prior art keywords
supply line
amine
gas
rich
absorption
Prior art date
Application number
KR1020140142717A
Other languages
Korean (ko)
Inventor
이성기
남기일
김성은
이태영
황희원
Original Assignee
현대중공업 주식회사
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 현대중공업 주식회사 filed Critical 현대중공업 주식회사
Priority to KR1020140142717A priority Critical patent/KR20160046591A/en
Publication of KR20160046591A publication Critical patent/KR20160046591A/en

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/60—Details about pipelines, i.e. network, for feed or product distribution

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The present invention relates to a partition type natural gas pretreatment apparatus.
The present invention is characterized in that it is partitioned upward and downward so as to have different absorbents, and it discharges sweet gas by regenerated lean amine which is injected when natural gas (feed gas) An absorption tower for discharging rich amines absorbing an acid gas from the gas; A stripping tower which is divided into upper and lower portions and which is fed with rich amine which has absorbed acid gas from the absorption tower and which separates and discharges the acid gas and regenerates rich amine which is separated from acid gas into phosphorus amine; The recovered phosphorus amine exchanged with the rich amine absorbed from the absorption tower discharged from the absorption tower is cooled to a predetermined temperature to be injected into the absorption tower, And a plurality of supply lines connected to the rich amines so that the rich amines are continuously circulated while being injected into the demoulding tower.

Description

[0001] The present invention relates to a multi-section type LNG feed gas pre-processing apparatus,

The present invention relates to a partition type natural gas pretreatment apparatus. More particularly, the absorption tower and the stripping tower of a GSU (Gas Sweetening Unit) applied to a floating offshore plant such as a Liquefied Natural Gas-Floating Production (LNGFPSO) To thereby improve absorption and removal performance with respect to the acid gas.

In general, Liquefied Natural Gas-Floating Production (LNGFPSO) moves to the offshore gas field and floats in the ocean. LNG production, storage, And can be offloaded to a marine mobile multifunctional plant.

These offshore plants are composed of floating marine structures with pretreatment, liquefaction and storage facilities (GSU) for the natural gas introduced from the submarine gas field, It is possible to move when the gas field production is completed.

The natural gas from the offshore gas field is mainly composed of methane and other hydrocarbons such as ethane, propane and butane. The impurities include acid gas components such as carbon dioxide (CO2) and hydrogen sulfide (H2S) H 2 O) and mercury (Hg).

When the temperature of natural gas is low with natural gas, it may cause the problem of generating hydrate or ice and clogging of the plant equipment. Mercury may be caused by the brittleness of aluminum plate plate fin heat exchanger cause.

In addition, CO 2 and heavy gas components can cause CO 2 freezing problems in cryogenic plants, resulting in clogging.

Therefore, the pretreatment process is introduced before the impurities in the natural gas are sent to the liquefaction process. These impurities must be removed to a certain level or less, and the change of the natural gas composition of the marine gas field to be mined and the performance of the pretreatment process Design optimization is required in case of degradation.

In the LNG pretreatment process, as in Patent Publication No. 10-1351440 (Announcement 2014.01.15), it is possible to remove carbon dioxide and hydrogen sulfide, which are acid gas components contained in natural gas (LNG feed gas) An acid gas removing device is included.

The natural gas pretreatment apparatus for removing the acid gas mainly uses an amine absorption process. Examples of the amine-based absorbent used in the amine absorption process include MEA (Monoethanol amine), DEA (Diethanol amine) and the like. (BASF Licensor process) in which Piperazine is added as an additive to MDEA (Methyldiethanol amine) is mainly used. In case of a large amount of carbon dioxide, a K 2 CO 3 aqueous solution improved by Benfield process Piperazine has been used as an additive.

That is, in the conventional natural gas pretreatment apparatus, as shown in FIG. 1, an absorber 100 and a regeneration unit 200 are separated from each other and a natural gas (LNG Feed Gas The natural gas introduced into the lower part of the absorption tower 100 is introduced into the absorption tower 100 by the lean amine injected into the upper part of the absorption tower 100, And then discharged into a sweet gas.

The rich amine which absorbs the acid gas while passing through the absorption tower 100 and rich in the acid gas is introduced into the demixing tower 200 through the heat exchanger 300 do.

At this time, a large amount of CO 2 and H 2 S, which are acid gas components, are discharged from the upper part of the stripping tower 200 due to the introduction of the rich amine. Through the regeneration process, The lean amine discharged from the lower part of the stripping tower 200 is heat-exchanged with the rich amine discharged from the absorption tower 100 in the heat exchanger 300.

The heat exchanged phosphorus amine is cooled to a predetermined temperature by the cooler 400 and then sent to the absorption tower 100. The circulation process is continuously repeated to remove the acid gas from the natural gas .

The first heating unit 500 is connected to the deodorizing tower 200 because part of the rich amine in which the acid gas is separated from the deodorization tower 200 is partially discharged from the first heating unit 500 ) To regenerate it as lean amine.

However, in the above-mentioned conventional natural gas pretreatment apparatus, the rate of absorption of CO 2 in the MDEA aqueous solution used in the pretreatment of natural gas is relatively slow compared with that of H 2 S, and in addition to the concentration of H 2 S in the sweet gas in which the acid gas is removed, In order to satisfy the concentration emission regulations, the height of the absorption column and the column-column must be increased. Therefore, there is a disadvantage in that the installation area of the absorption tower and the demolition column is large when installed in a floating oceanic plant having a limited space. There is a problem that the piping is complicated.

In order to solve such a problem, the present invention relates to an absorption tower of a GSU (Gas Sweetening Unit) applied to a floating offshore plant such as a Liquefied Natural Gas-Floating Production (LNGFPSO) In addition to improving the absorption and removal performance of acid gas without mixing two kinds of absorbent in one GSU process by circulating the tower top and bottom in two loops, The purpose of this study is to simplify the connection of piping for connecting the separated absorption tower and demolition tower as well as minimizing the installation area of natural gas pretreatment equipment in floating floating offshore plant.

In order to achieve the above object, the present invention provides a method for producing a sweet gas, which is divided into upper and lower portions having different absorbents and is regenerated by lean amine, which is injected when a feed gas is introduced, An absorption tower for discharging the rich amine that has absorbed the acid gas from the introduced natural gas; A stripping tower which is divided into upper and lower portions and which is fed with rich amine which has absorbed acid gas from the absorption tower and which separates and discharges the acid gas and regenerates rich amine which is separated from acid gas into phosphorus amine; The recovered phosphorus amine exchanged with the rich amine absorbed from the absorption tower discharged from the absorption tower is cooled to a predetermined temperature to be injected into the absorption tower, And a plurality of supply lines connected to the rich amines so that the rich amines are continuously circulated while being injected into the demoulding tower.

When the natural gas is introduced into the absorber, the absorbed lean amine is injected from the stripping tower through the supply line, the sweet gas is discharged by the lean amine injected, and the acid gas is absorbed from the natural gas A first absorber for discharging the rich gas, a second absorber for discharging the rich gas, and a second absorber for discharging the rich gas, And a second absorber. The present invention also provides a pretreatment device for a partitioned natural gas.

The stripping tower is connected to receive the rich amine that has absorbed the acid gas discharged from the first absorption unit through the supply line. The acid gas is separated and discharged from the injected rich amine, and the acid gas is separated A second deodorization unit that receives the rich gas that has absorbed the acid gas from the second absorption unit through the supply line and regenerates the rich amine into the phosphorus amine by regenerating the rich amine into lean amine, Wherein the natural gas pretreatment apparatus comprises:

The supply line may include a first supply line through which lean amine regenerated from the first deodorization of the deodorization tower is injected into the first absorption section, And a second heat exchanger connected to the first and second supply lines for mutual heat exchange of the lean amine and the rich amine flowing in the second supply line, Wherein the first supply line is further connected to a cooler for cooling the regenerated lean amine heat-exchanged by the first heat exchanger to a predetermined temperature so as to be injected into the first absorber. A natural gas pretreatment device can be provided.

The supply line may include a third supply line for injecting regenerated lean amine from the lower portion of the second desorption to the upper portion of the second desorption portion, And a second heat exchanger connected to the third supply line and the fourth supply line so that the regenerated lean amine flowing through the fourth supply line and the rich amine absorbing the acid gas are exchanged with each other The natural gas pretreatment apparatus according to the present invention can be applied to a natural gas pretreatment apparatus.

In addition, the supply line includes a heating unit for heating a part of the rich amine from which the acid gas has been separated from the stripping tower to return to the denitrification and regenerating the rich amine as lean amine. .

Further, according to another embodiment of the present invention, there is provided a pretreatment device for a partitioned natural gas, characterized in that the supply line is connected to the upper part of the first absorption part via the second heat exchanger and the cooler, A second supply line connected from the lower portion of the first absorption portion to the upper portion of the second de-rejection via the second heat exchanger, a second absorption line passing through the first de-rejection from the lower portion of the first de- And a fourth supply line connected to the upper portion of the first absorber and connected to the upper portion of the first absorber via the first heat exchanger from the lower portion of the second absorber. A natural gas pretreatment device can be provided.

According to the present invention, an absorption tower and a demolition tower of a GSU (Gas Sweetening Unit) applied to a floating offshore plant such as a floating natural LNG liquefying plant (LNGFPSO) The upper and lower regions are divided into two loops to improve absorption and removal performance for acid gas without mixing two types of absorbents in one GSU process, It has the effect of simplifying the connection of the piping to connect the separated absorption tower and demolition tower, as well as minimizing the installation area when installing the natural gas pretreatment device in offshore plant.

1 is a block diagram schematically showing a structure of a conventional natural gas pretreatment apparatus,
2 is a block diagram schematically showing the structure of a partition type natural gas pretreatment apparatus according to an embodiment of the present invention,
3 is a block diagram schematically showing the structure of a partition type natural gas pretreatment apparatus according to another embodiment of the present invention.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the drawings, the same reference numerals are used to designate the same or similar components throughout the drawings. In the following description of the present invention, a detailed description of known functions and configurations incorporated herein will be omitted when it may make the subject matter of the present invention rather unclear.

FIG. 1 is a block diagram schematically showing a structure of a conventional natural gas pretreatment apparatus, FIG. 2 is a block diagram schematically showing a structure of a partition type natural gas pretreatment apparatus according to an embodiment of the present invention, and FIG. 3 FIG. 2 is a block diagram schematically showing the structure of a partition type natural gas pretreatment apparatus according to another embodiment of the present invention; FIG.

As shown in the figure, a pretreatment unit for a pretreatment type natural gas according to an embodiment of the present invention includes an absorption tower 10, a stripping tower 20, an absorption tower 10, And a plurality of supply lines (L) each connected to the tower top (20).

The absorption tower 10 is partitioned upward and downward so as to have absorbents having different functions, and improves absorption and removal performance for acid gases without mixing two types of absorbents in one GSU (Gas Sweetening Unit) process It plays a role.

The absorption tower 10 is divided into a plurality of regions each having an absorbent having a different function. When the natural gas (feed gas) flows in, A lean amine is injected and a sweet gas is discharged by the introduced lean amine and a first absorption which discharges a rich amine from which the acid gas is absorbed is discharged from the natural gas, And a rich gas which absorbs acid gas by the injected phosphorus amine and which absorbs the acid gas by the injected phosphorus amine, And a second absorber 14 for discharging the second absorber.

Here, the first absorption portion 12 corresponds to the upper region of the absorption tower 10 and is configured to circulate an absorbent mainly absorbing CO 2 from the natural gas to be introduced. Preferably, the second absorption portion 14 When the natural gas is introduced, the regenerated lean amine is injected through the feed line (L) connected to the upper part of the first absorption part (12) Rich amine that has absorbed the gas is discharged through the supply line (L) to the demixing tower (20).

The second absorption portion 12 is configured to introduce natural gas into the lower portion and circulate the absorbent mainly absorbing H 2 S from the incoming natural gas. Preferably, the second absorption portion 12 is connected to the upper portion of the second absorption portion 12 Rich amine recovered from the stripping tower 20 is introduced into the stripping tower 20 through the line L and the rich amine which has absorbed the acid gas from the natural gas by the injected phosphorus amine is introduced into the stripping tower 20 ).

The stripping tower 20 is divided into upper and lower portions and each of the rich amines discharged from the absorption tower 10 through the plurality of supply lines L is injected to separate and discharge the acid gas from the injected rich amine, It plays a role of regenerating with amine.

The demolition tower 20 includes a first deodorization 22 corresponding to the upper region and a second deodorization 24 corresponding to the lower region.

The first deodorizing unit 22 is connected to the upper portion of the first absorption unit 12 through a supply line L so as to receive rich amines absorbing the acidic gas discharged from the lower portion of the first absorption unit 12, The acidic gas is separated and discharged, and the injected acidic gas is regenerated as a lean amine into the separated rich amine and re-injected into the upper part of the first absorption part 12 through the supply line L.

The second deodorizing unit 24 receives the rich amine that has absorbed the acid gas from the second absorption unit 14 through the supply line L and regenerates the rich amine into the lean amine, Is connected to inject the lean amine recovered through the supply line (L) to the upper portion of the second absorption portion (14).

The supply line L is connected to the absorption tower 10 and the demolition tower 20 which are divided into the upper and lower regions so as to continuously circulate the two loops, To absorb and remove the acidic gas without mixing the absorbent.

The supply line L is a line for supplying lean amine recovered from the first deodorization 22 of the stripping tower 20 to the first absorption portion 12 when the natural gas is introduced into the lower portion of the second absorption portion 14. [ A second supply line L2 for allowing the rich amine that has absorbed the acid gas from the first absorption portion 12 to be injected into the first deodorization 22, And a first heat exchanger 30 connected to the first and second supply lines L1 and L2 so as to mutually heat exchange the lean amine and the rich amine flowing in the second supply line L2 .

The first supply line L1 is connected to the second supply line L2 through the first heat exchanger 30 from the lower part of the first deaerator 22 to the first absorption line (12).

At this time, as the cooler 32 is further connected to the first supply line L1, the regenerated lean amine heat-exchanged by the first heat exchanger 30 is cooled to a predetermined temperature to cool the first absorber 12 So as to be injected into the upper part.

In the second supply line L2, the rich amine that has absorbed the acidic gas discharged from the lower portion of the first absorption portion 12 flows through the first heat exchanger 30 and the lean amine Rich acid which has been heat-exchanged with the acid gas and heat-exchanged with the acid gas is injected into the upper part of the first deodorizer 22.

The first heat exchanger 30 is connected to the first supply line L1 and the second supply line L2 so that the regenerated lean amine and the rich amine that absorbs the acid gas are mutually heat- (L1) and a second supply line (L2).

The supply line L includes a third supply line L3 for injecting the regenerated lean amine into the upper portion of the second absorber 14 from the lower portion of the second absorber 24, A fourth supply line L4 for injecting rich amine that has absorbed acidic gas from the bottom of the second deodorization 24 to the fourth supply line L4, And a second heat exchanger (40) connected and configured to mutually exchange heat between the regenerated lean amine and the rich gas absorbing the acidic gas.

The third supply line L3 is a regenerated heat exchanger that is heat exchanged with the rich amine that has absorbed the acid gas flowing from the lower portion of the second deodorizer 24 through the second heat exchanger 40 to the fourth supply line L4 And the lean amine is injected into the upper part of the second absorbing part 14.

The fourth supply line L4 is connected to the third supply line L3 through the second heat exchanger 40 and the rich amine which has absorbed the acidic gas discharged from the lower portion of the second absorption portion 14, Rich amine which has been heat-exchanged with phosphorous amine and absorbed heat-exchanged acidic gas is injected into the upper part of the second deodorizer 24.

The second heat exchanger 40 is connected to the third and fourth supply lines L3 and L4 so that the regenerated lean amine flowing between the third and fourth supply lines L3 and L4 and the rich amine absorbing the acidic gas are exchanged with each other, L4).

As described above, the supply line L heats a part of the rich amine from which the acid gas flowing from the stripping tower 20 through the fourth supply line L4 has been separated to return to the second de- And a heating unit 50 for regenerating the heat.

Here, the heating unit 50 provides a heat source to regenerate a portion of the rich amine from which the acid gas has been separated into lean amine, and a portion of the rich amine is returned to the stripping tower 20 via a separate feed line, Lt; / RTI >

In the meantime, the partition type natural gas pretreatment apparatus according to another embodiment of the present invention will be described in detail, and a detailed description of the same configuration of the present invention will be omitted.

The natural gas pretreatment device according to another embodiment of the present invention is characterized in that when the natural gas flows into the lower part of the second absorption part 14 of the absorption tower 10, And the second supply line L2 is connected to the upper part of the first absorption part 12 through the second heat exchanger 40 and the cooler 32 from the lower part of the first absorption part 12, To the upper portion of the second deodorization (24) via the second heat exchanger (40).

That is, when the natural gas is introduced into the lower part of the second absorption part 14, the lean amine recovered from the lower part of the second deodorization part 24 flows into the second heat exchanger 40 and the cooler (32), is cooled to a predetermined temperature and heat exchange with the rich amine flowing through the second supply line (L2), and is injected into the upper part of the first absorption part (12) The sweet gas is discharged from the absorption section 12 while the rich gas which has absorbed the acid gas from the natural gas introduced into the absorption tower 10 by the lean amine injected into the absorption tower 10 is supplied to the first absorption section 12 Through a second supply line (L2) connected to the lower portion of the first supply line (L1) and is heat exchanged with the lean amine passing through the first supply line (L1) 24).

The third supply line L3 is connected to the upper part of the second absorption part 14 from the lower part of the first deodorization part 22 through the first heat exchanger 30 and the fourth supply line L4 is connected to the upper part of the second absorption part 14, 2 absorber 14 to the upper portion of the first deodorizer 22 via the first heat exchanger 30. [

That is, when the natural gas is introduced into the lower part of the second absorption part 14, the lean amine from which the acid gas is separated from the lower part of the first deodorization part 22 flows through the third supply line L3 into the first heat exchanger 30 The acid gas flowing through the fourth supply line L4 is heat-exchanged with the absorbed rich amine and is injected into the upper part of the second absorption part 14 while the second absorption part 14 is injected into the upper part of the second absorption part 14, The rich amine which has absorbed the acid gas from the natural gas introduced by the amine passes through the fourth heat exchanger 30 from the lower part of the second absorption part 14 through the fourth heat exchanger 30, L3) is injected into the upper portion of the first deodorizer (22).

The pretreatment device for the partitioned natural gas according to each embodiment of the present invention has the absorption tower 10 and the stripping tower 20 which are divided into the upper and lower regions and the absorption tower 10 and the stripping tower 20 And a plurality of supply lines L connected to each other so that the gas sweetening (GSU) applied to a floating offshore plant such as Liquefied Natural Gas-Floating Production (LNGFPSO) Units are divided into upper and lower zones, respectively, and circulated to two loops to improve absorption and removal performance for acid gases without mixing two types of sorbents in one GSU process In addition to minimizing the installation area of natural gas pretreatment equipment in a floating offshore plant with a limited space, it is also possible to minimize the installation area of piping, The invention with.

The foregoing description is merely illustrative of the technical idea of the present invention, and various changes and modifications may be made by those skilled in the art without departing from the essential characteristics of the present invention. Therefore, the embodiments disclosed in the present invention are intended to illustrate rather than limit the scope of the present invention, and the scope of the technical idea of the present invention is not limited by these embodiments. The scope of protection of the present invention should be construed according to the following claims, and all technical ideas within the scope of equivalents should be construed as falling within the scope of the present invention.

10. Absorption tower 20. Removal tower
30. First heat exchanger 32. Cooler
40. Second heat exchanger 50. Heating section

Claims (7)

And is divided into upper and lower portions so as to have different absorbents, and sweet gas is discharged by the regenerated lean amine which is injected when the feed gas is introduced, An absorption tower for discharging rich amines absorbing the gas (acid gas);
A stripping tower which is divided into upper and lower portions and which is fed with rich amine which has absorbed acid gas from the absorption tower and which separates and discharges the acid gas and regenerates rich amine which is separated from acid gas into phosphorus amine; And
Exchanges the lean amine recovered from the stripping tower and the rich amine absorbing the acid gas discharged from the absorption tower, and the heat exchanged regenerated lean amine is cooled to a predetermined temperature to be injected into the absorption tower, A plurality of supply lines configured to continuously circulate while allowing the absorbed rich amines to be injected into the demoulding tower;
Wherein the natural gas pre-processing unit comprises: The method according to claim 1,
Wherein the absorption tower is configured such that when the natural gas is introduced, the recovered lean amine is injected through the supply line, the sweet gas is discharged by the lean amine, and the rich gas And a second absorption section for introducing the natural gas into the first absorption section and introducing the lean amine regenerated from the stripping tower through the supply line and discharging the rich gas absorbing the acid gas by the lean amine, And an absorptive portion for absorbing the natural gas. 3. The method of claim 2,
The stripping tower is connected to receive the rich amine that has absorbed the acidic gas discharged from the first absorber through the supply line. The acidic gas is separated and discharged from the injected rich amine, And a second deodorization unit that receives the rich gas that has absorbed the acid gas from the second absorption unit through the supply line and regenerates the injected rich amine with the lean amine, Wherein the natural gas pretreatment device comprises: The method of claim 3,
Wherein the supply line includes a first supply line for allowing the lean amine recovered from the first desorption of the stripping tower to be injected into the first absorption section, And a first heat exchanger connected to the first and second supply lines for mutual heat exchange between the first supply line and the lean amine and rich amine flowing in the second supply line Wherein the first supply line is further connected to a cooler for cooling the regenerated lean amine heat-exchanged by the first heat exchanger to a predetermined temperature to be injected into the first absorber Pretreatment device. The method of claim 3,
Wherein the supply line includes a third supply line for introducing the regenerated lean amine from the lower portion of the second desorption to the upper portion of the second desorption portion, a third supply line for sucking the acid gas from the lower portion of the second absorption portion to the upper portion of the second desorption, And a second heat exchanger connected to the third supply line and the fourth supply line so that the regenerated lean amine flowing through the fourth supply line and the rich amine absorbing the acid gas are mutually heat exchanged Wherein the natural gas pre-processing unit is configured to process the natural gas. The method according to claim 1,
Wherein the supply line includes a heating unit for heating a part of the rich amine from which the acid gas has been separated from the stripping tower to return to the desorption and regenerate the lean amine. 4. The method according to claim 2 or 3,
The supply line being connected to the upper portion of the first absorption portion via the second heat exchanger and the cooler from the second de-rejection portion, the first supply line connected to the upper portion of the first absorption portion through the second heat exchanger, A second supply line connected to an upper portion of the second desorption, a third supply line connected to the upper portion of the second absorption portion via the first heat exchanger from the lower portion of the first desorption, And a fourth supply line connected to the upper part of the first de-rejecting part from the lower part through the first heat exchanger.
KR1020140142717A 2014-10-21 2014-10-21 Multi section type-LNG Feed gas pre-processing apparatus KR20160046591A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
KR1020140142717A KR20160046591A (en) 2014-10-21 2014-10-21 Multi section type-LNG Feed gas pre-processing apparatus

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
KR1020140142717A KR20160046591A (en) 2014-10-21 2014-10-21 Multi section type-LNG Feed gas pre-processing apparatus

Publications (1)

Publication Number Publication Date
KR20160046591A true KR20160046591A (en) 2016-04-29

Family

ID=55915725

Family Applications (1)

Application Number Title Priority Date Filing Date
KR1020140142717A KR20160046591A (en) 2014-10-21 2014-10-21 Multi section type-LNG Feed gas pre-processing apparatus

Country Status (1)

Country Link
KR (1) KR20160046591A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112546675A (en) * 2020-12-28 2021-03-26 大连福佳·大化石油化工有限公司 Improved steam stripping structure of adsorption tower for leaking agent from bed layer

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112546675A (en) * 2020-12-28 2021-03-26 大连福佳·大化石油化工有限公司 Improved steam stripping structure of adsorption tower for leaking agent from bed layer
CN112546675B (en) * 2020-12-28 2023-10-13 大连福佳·大化石油化工有限公司 Improved structure of adsorption tower stripping of bed leakage agent

Similar Documents

Publication Publication Date Title
US10150926B2 (en) Configurations and methods of flexible CO2 removal
CA2674874C (en) Method for purifying a gas mixture containing acid gases
US20130269525A1 (en) Absorption Media for Scrubbing CO2 from a Gas Stream and Methods Using the Same
RU2631295C2 (en) Deodorizing desulphurization of natural gas by means of membrane contactor
JP2012504494A (en) Configuration and method for removing high pressure acidic gas
SG192604A1 (en) Pressure-temperature swing adsorption process for the separation of heavy hydrocarbons from natural gas streams
CN105126576A (en) High-efficiency composite desulphurization solvent and system and method for removing acidic gas and organic sulfur
WO2017143215A1 (en) Cold solvent gas treating system for selective h2s removal
JP2013505123A (en) High pressure high CO2 removal configuration and method
CA2726640A1 (en) Carbon dioxide absorber partial pumparound for cooling semi-lean physical solvent
CN105008017A (en) Process for floating liquified natural gas pretreatment
KR101883878B1 (en) Apparatus and method for removing acidic gas containing natural gas
CN104936677A (en) System and method for recovering gas containing CO2 and H2S
KR101571771B1 (en) A natural gas regeneration system
KR20160046591A (en) Multi section type-LNG Feed gas pre-processing apparatus
Lu et al. Recent progress in carbon dioxide capture technologies: A review
CN105983310A (en) Absorbent for selectively absorbing sulfur dioxide and application thereof
KR101738335B1 (en) Apparatus for removing water and acid gas of a natural gas
CN105344205A (en) Absorber for selectively removing H2S from CO2-containing mixing gas
KR20160046592A (en) Energy savings type- LNG Feed gas pre-processing apparatus
KR20170080992A (en) Apparatus for removing moisture from natural gas and the method for removing moisture from natural gas by using the same
KR101351440B1 (en) Membrane-absorption hybrid pretreatment apparatus for lng-fpso
JP4758711B2 (en) Pretreatment method for gas hydrate production
KR20160034521A (en) Feed gas pre-processing apparatus
KR20170011889A (en) Acid gas absorbing apparatus and method for absorbing acid gas using the same

Legal Events

Date Code Title Description
A201 Request for examination
E902 Notification of reason for refusal
E601 Decision to refuse application