KR20160046591A - Multi section type-LNG Feed gas pre-processing apparatus - Google Patents
Multi section type-LNG Feed gas pre-processing apparatus Download PDFInfo
- 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
Links
- 238000007781 pre-processing Methods 0.000 title claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 122
- 150000001412 amines Chemical class 0.000 claims abstract description 113
- 239000007789 gas Substances 0.000 claims abstract description 109
- 238000010521 absorption reaction Methods 0.000 claims abstract description 95
- 239000003345 natural gas Substances 0.000 claims abstract description 60
- 239000002253 acid Substances 0.000 claims abstract description 58
- 239000002250 absorbent Substances 0.000 claims abstract description 12
- 230000002745 absorbent Effects 0.000 claims abstract description 12
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 10
- 239000011574 phosphorus Substances 0.000 claims abstract description 10
- 235000009508 confectionery Nutrition 0.000 claims abstract description 9
- -1 phosphorus amine Chemical class 0.000 claims abstract description 9
- 238000007599 discharging Methods 0.000 claims abstract description 8
- 238000000034 method Methods 0.000 claims description 21
- 239000006096 absorbing agent Substances 0.000 claims description 18
- 238000004332 deodorization Methods 0.000 claims description 14
- 230000002378 acidificating effect Effects 0.000 claims description 12
- 238000003795 desorption Methods 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 2
- 238000005192 partition Methods 0.000 abstract description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 238000009434 installation Methods 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 230000001172 regenerating effect Effects 0.000 description 4
- 230000001877 deodorizing effect Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 2
- 229940043237 diethanolamine Drugs 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
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
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
The rich amine which absorbs the acid gas while passing through the
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
The heat exchanged phosphorus amine is cooled to a predetermined temperature by the cooler 400 and then sent to the
The
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
The
The
Here, the
The
The
The
The
The second deodorizing
The supply line L is connected to the
The supply line L is a line for supplying lean amine recovered from the
The first supply line L1 is connected to the second supply line L2 through the
At this time, as the
In the second supply line L2, the rich amine that has absorbed the acidic gas discharged from the lower portion of the
The
The supply line L includes a third supply line L3 for injecting the regenerated lean amine into the upper portion of the
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
The fourth supply line L4 is connected to the third supply line L3 through the
The
As described above, the supply line L heats a part of the rich amine from which the acid gas flowing from the stripping
Here, the
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
That is, when the natural gas is introduced into the lower part of the
The third supply line L3 is connected to the upper part of the
That is, when the natural gas is introduced into the lower part of the
The pretreatment device for the partitioned natural gas according to each embodiment of the present invention has the
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.
30.
40.
Claims (7)
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:
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.
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:
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.
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.
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.
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.
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)
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 |
-
2014
- 2014-10-21 KR KR1020140142717A patent/KR20160046591A/en not_active Application Discontinuation
Cited By (2)
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 |