CN103555382A - Coproduction technology employing mixed-refrigerant cycle (MRC) natural gas liquefaction and direct heat exchange (DHX) tower light hydrocarbon recovery - Google Patents
Coproduction technology employing mixed-refrigerant cycle (MRC) natural gas liquefaction and direct heat exchange (DHX) tower light hydrocarbon recovery Download PDFInfo
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- CN103555382A CN103555382A CN201310504664.7A CN201310504664A CN103555382A CN 103555382 A CN103555382 A CN 103555382A CN 201310504664 A CN201310504664 A CN 201310504664A CN 103555382 A CN103555382 A CN 103555382A
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Abstract
A mixed refrigeratory technology is mainly adopted by natural gas liquefaction at the present stage; a direct heat exchange (DHX) tower or expander refrigeratory technology is mainly adopted by light hydrocarbon recovery; the refrigeratory technology is adopted by the natural gas liquefaction and the light hydrocarbon recovery. The invention provides a novel coproduction technology employing mixed-refrigerant cycle (MRC) natural gas liquefaction and DHX tower light hydrocarbon recovery. Cold flow is supplied for light hydrocarbon recovery by using a mixed refrigerant cycle of a liquefaction process in the coproduction technology of combining the MRC natural gas liquefaction with the DHX tower light hydrocarbon recovery; meanwhile, heavy constituents in a feed gas are separated and processed in the light hydrocarbon recovery process. The separation efficiency of the heavy constituents in the liquefaction process can be improved by analyzing the coproduction technology, so that the C3 content is smaller than or equal to 0.3%; the content of C4 and C4<+> is reduced to about 0%; meanwhile, the coproduction technology is applicable to the feed gas of which the C2<+> content is greater than or equal to 0.1%; the mean increase of the liquefied natural gas (LNG) yield can be up to 71.89%; the mean reduction of unit energy consumption can be up to 17.64%.
Description
Technical field
The present invention relates to natural gas processing technical field, particularly the technique of a kind of MRC natural gas liquefaction and the coproduction of DHX tower lighter hydrocarbons recovery.
Background technology
Sweet natural gas is the fastest-rising energy of 21 century consumption, and the proportion that accounts for disposable energy expenditure is increasing.But global natural gas source skewness, mainly concentrates on the Middle East and USSR (Union of Soviet Socialist Republics) state district.The Sweet natural gas of China is mainly distributed in western part and eastern region.Therefore, in the rich place of production of some Sweet natural gases or side area, must by its by manage defeated or with the form of liquefaction be transported to gas production little, consume large area.To manage defeated process and, because cooling causes heavy hydrocarbon condensation, icing, blocking pipe, need heavy hydrocarbon to be separated by process for recovering light hydrocarbon in order preventing, reduce hydrocarbon dew point, meet the requirement of pipe gas transmission.At present, natural gas processing major part is all by two processes separately, first Sweet natural gas is carried out to lighter hydrocarbons recovery, then by its liquefaction.
The key of lighter hydrocarbons recovery is how to freeze, and allows C
2 +liquefaction, separation more.Main means have expander refrigeration and adopt DHX tower weight absorption technique at present, and the former is only for high pressure lean gas, and the latter also requires C
3content is not more than 11%.The use of two techniques all has certain requirement to unstripped gas, if adopt conventional mix refrigerant refrigeration techniques in natural gas liquefaction, has increased again complicacy, the cost of investment of technique.In liquefaction process, if rely on separately refrigeration agent refrigeration can not reach-160 ℃, therefore, after the refrigeration of being everlasting, by a throttling valve, reach the effect of throttling cooling.Throttling cooling is mainly by reducing pressure, making the CH that boiling point is minimum
4partial gasification, need to absorb heat while utilizing gasification and reach the object of cooling.If the heavy hydrocarbon component containing in Sweet natural gas too much can affect the effect of throttling cooling.
In the last few years, about adopting which kind of technique to freeze to lighter hydrocarbons recovery process and the technology of relevant natural gas liquefaction joint process has had relevant elaboration.CN202968508U, CN102994184A, CN102517108 etc. have had and have been described in further detail for utilizing gas deliquescence process to carry out the technique of liquid nitrogen coproduction and device thereof, it is mainly in liquefaction process, to add rectifying tower and then by methane and nitrogen separation, utilize refrigeration cycle by liquefaction of nitrogen simultaneously, and then reach the object of coproduction.The proposition such as CN202246578U, CN102408910A applies to hybrid refrigeration cycle the technique of lighter hydrocarbons recovery process, by this technique, can effectively improve C
3yield, the benefit of increase device reduces energy consumption, the adaptability of intensifier simultaneously.
Therefore, the mix refrigerant circulating in natural gas liquefaction can be used for not only needing the unstripped gas that reclaims lighter hydrocarbons but also must liquefy for the joint process of lighter hydrocarbons recovery process, and there is larger economic benefit.
Summary of the invention
The present invention proposes the technique of a kind of MRC natural gas liquefaction and the coproduction of DHX tower lighter hydrocarbons recovery.Lighter hydrocarbons recovery processing object is C
2 +, natural gas liquefaction processing object is C
1, C
2, the hybrid refrigeration cycle of utilizing liquefaction process provides cold for lighter hydrocarbons recovery, simultaneously by the heavy constituent in lighter hydrocarbons recovery separate raw materials gas processing.On the one hand, avoided heavy constituent separation thoroughly not cause the phenomenon that super cooled sect load increases, liquefied fraction reduces.On the other hand, avoided separately hybrid refrigeration cycle is complicated for the equipment of lighter hydrocarbons recovery, invest the problems such as large.In a word, this technical process is simple, energy consumption is low, can effectively improve the comprehensive utilization ratio of Sweet natural gas.
The present invention is that the technical scheme that its technical problem of solution is taked is:
The joint process that MRC natural gas liquefaction is combined with DHX tower process for recovering light hydrocarbon, the hybrid refrigeration cycle of utilizing liquefaction process provides cold for lighter hydrocarbons recovery, utilizes deethanizing column, debutanizing tower in lighter hydrocarbons recovery process that the heavy hydrocarbon in Sweet natural gas is removed simultaneously.Mix refrigerant enters main ice chest, after being cooled to-70 ℃ by separating tank separation give vent to anger, liquid two-phase.Gas phase passed into ice chest cooling and by throttling valve throttling, was cooled to-155 ℃ of left and right again, as low-temperature receiver, for crossing ice chest, provided cold.After liquid phase is lowered the temperature by throttling and by refrigerant mixed re-heat in main ice chest of crossing ice chest backflow.After re-heat, by supercharging, cooling, loop back main ice chest.Unstripped gas passes into low-temperature separator after being cooled to-80 ℃ by main ice chest, and gas phase enters heavy contact tower, and liquid phase is heated up and entered deethanizing column by ice chest.The tactile column overhead of reclosing is worked off one's feeling vent one's spleen and was passed into mutually ice chest cooling, then enters storage tank after being cooled to-161.5 ℃ by throttling valve.Deethanizer overhead gas phase by ice chest, lower the temperature after as the absorption agent of heavy contact tower, at the bottom of tower, liquid phase passes into debutanizing tower rectifying and obtains liquefied petroleum gas (LPG) and stable light oil.
Beneficial effect:
1. avoided heavy constituent separation thoroughly not cause the phenomenon that super cooled sect load increases, liquefied fraction reduces.
2. avoided separately hybrid refrigeration cycle is complicated for the equipment of lighter hydrocarbons recovery, invest the problems such as large.
3. be applicable to C
2 +the unstripped gas of content>=0.1, under this condition, LNG output increase rate average out to 71.89%, unit consumption of energy reduce amplitude average out to 17.64%.
4. can improve liquefaction process heavy constituent separation efficiency, make C
3content≤0.3%, C
4and C
4 +content drops to 0% left and right.
Accompanying drawing explanation
Accompanying drawing 1 is technical process of the present invention.
Mark in figure: A1 is ice chest, and B1, B2 are separating tanks, and B3 is absorption tower, and B4 is deethanizing column, and B5 is debutanizing tower, and B6 is condenser, and B7 is compressor; A is unstripped gas, and b is natural gas liquids (LNG), and c is liquefied petroleum gas (LPG) (LPG), and d is for stablizing light oil, and 1～17 is logistics numbering.
Embodiment
Below by example, the present invention is further described.
Embodiment 1:
The present embodiment unstripped gas mole forms (mol%): C
180.2, C
23.95, C
36.63, i-C
41.67, n-C
42.7, i-C
51.22, n-C
51.14, C
6 +1.49, N
20.96, CO
20.04.Feeding temperature is 25 ℃, and pressure is 2.8MPa, and flow is 740kmol/h.
Mix refrigerant enters main ice chest, after being cooled to-70 ℃ by separating tank separation give vent to anger, liquid two-phase.Gas phase passed into ice chest cooling and by throttling valve throttling, was cooled to-155 ℃ of left and right again, as low-temperature receiver, for crossing ice chest, provided cold.After liquid phase is lowered the temperature by throttling and by refrigerant mixed re-heat in main ice chest of crossing ice chest backflow.After re-heat, by supercharging, cooling, loop back main ice chest.Unstripped gas passes into low-temperature separator after being cooled to-80 ℃ by main ice chest, and gas phase enters heavy contact tower, and liquid phase is heated up and entered deethanizing column by ice chest.The tactile column overhead of reclosing is worked off one's feeling vent one's spleen and was passed into mutually ice chest cooling, then enters storage tank after being cooled to-161.5 ℃ by throttling valve.Deethanizer overhead gas phase by ice chest, lower the temperature after as the absorption agent of heavy contact tower, at the bottom of tower, liquid phase passes into debutanizing tower rectifying and obtains liquefied petroleum gas (LPG) and stable light oil.The stage number of deethanizing column is 10, and tower top pressure is 1800kPa, is 1850kPa at the bottom of tower, and feed entrance point is the 4th block of column plate.The stage number of debutanizing tower is 12, and tower top pressure is 1300kPa, is 1350kPa at the bottom of tower, and feed entrance point is the 6th block of column plate.
The output that the product of final joint process and traditional technology is stablized light oil and liquefied petroleum gas (LPG) changes not quite with composition, C in LNG
3content is that 0.08%, C4 is that 0.00%, LNG output is 190.65t/d, and unit consumption of energy is 423.88MJ/t, under the same conditions, and C in the LNG of traditional technology
3content is that 1.48%, C4 is that 0.21%, LNG output is 116.52t/d, and unit consumption of energy is 524.05MJ/t.Two techniques are contrasted, and joint process LNG output improves 63.62%, and unit consumption of energy reduces by 19.11%.
Claims (5)
1.MRC natural gas liquefaction and DHX tower lighter hydrocarbons recovery joint process, in by natural gas liquefaction, also can coproduction lighter hydrocarbons, the hybrid refrigeration cycle of utilizing liquefaction process provides cold for lighter hydrocarbons recovery, by lighter hydrocarbons recovery process, the heavy constituent in unstripped gas is carried out to separation, processing simultaneously, technique is mainly divided into mix refrigerant refrigeration cycle part and natural gas liquefaction, lighter hydrocarbons recovery part, it is characterized in that comprising following steps:
(1) compression section: by mix refrigerant supercharging 1～5MPa;
(2) hybrid refrigeration cycle: the mix refrigerant after supercharging enters main ice chest, through cooling after by separating tank separation give vent to anger, liquid two-phase;
Gas phase passed into ice chest cooling lowers the temperature by throttling valve throttling again, as low-temperature receiver, for crossing ice chest, provides cold;
After liquid phase is lowered the temperature by throttling and by refrigerant mixed re-heat in main ice chest of crossing ice chest backflow;
After re-heat, by supercharging, cooling, loop back compression section section;
(3) unstripped gas complete processing section: unstripped gas passes into low-temperature separator by main ice chest cooling, and gas phase enters heavy contact tower, and liquid phase is heated up and entered deethanizing column by ice chest,
The tactile column overhead of reclosing is worked off one's feeling vent one's spleen and was passed into mutually ice chest cooling, then flows to storage tank after lowering the temperature by throttling valve,
Deethanizer overhead gas phase by ice chest, lower the temperature after as the absorption agent of heavy contact tower, at the bottom of tower, liquid phase passes into debutanizing tower rectifying and obtains liquefied petroleum gas (LPG) and stable light oil.
2. according to processing method claimed in claim 1, it is characterized in that: mix refrigerant is mainly comprised of methane, ethane, propane, nitrogen, and wherein ratio of components is about: 5:3:1:1; Its intake pressure is about 0.1MPa, and temperature is about 25 ℃.
3. according to processing method claimed in claim 1, it is characterized in that: the temperature that mix refrigerant goes out main ice chest is about-70 ℃; Mix refrigerant pressure after throttling valve step-down is about 200kPa.
4. according to processing method claimed in claim 1, it is characterized in that: the temperature that unstripped gas goes out main ice chest is about-70 ℃.
5. according to processing method claimed in claim 1, it is characterized in that: the stage number of deethanizing column is 10, feed entrance point is the 4th block of column plate; The stage number of debutanizing tower is 12, and feed entrance point is the 6th block of column plate.
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| CN201310504664.7A CN103555382A (en) | 2013-10-24 | 2013-10-24 | Coproduction technology employing mixed-refrigerant cycle (MRC) natural gas liquefaction and direct heat exchange (DHX) tower light hydrocarbon recovery |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108165333A (en) * | 2017-12-27 | 2018-06-15 | 四川杰瑞恒日天然气工程有限公司 | A kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique |
| CN111670329A (en) * | 2017-12-15 | 2020-09-15 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111670329A (en) * | 2017-12-15 | 2020-09-15 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
| US11226154B2 (en) | 2017-12-15 | 2022-01-18 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| US11231227B2 (en) | 2017-12-15 | 2022-01-25 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| US11231226B2 (en) | 2017-12-15 | 2022-01-25 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| US11248840B2 (en) | 2017-12-15 | 2022-02-15 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| US11248839B2 (en) | 2017-12-15 | 2022-02-15 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| US11320196B2 (en) | 2017-12-15 | 2022-05-03 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| CN111670329B (en) * | 2017-12-15 | 2022-07-08 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
| US11428464B2 (en) | 2017-12-15 | 2022-08-30 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| US11644235B2 (en) | 2017-12-15 | 2023-05-09 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| CN108165333A (en) * | 2017-12-27 | 2018-06-15 | 四川杰瑞恒日天然气工程有限公司 | A kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique |
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Application publication date: 20140205 |