CN108165333A - A kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique - Google Patents
A kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique Download PDFInfo
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- CN108165333A CN108165333A CN201711445082.0A CN201711445082A CN108165333A CN 108165333 A CN108165333 A CN 108165333A CN 201711445082 A CN201711445082 A CN 201711445082A CN 108165333 A CN108165333 A CN 108165333A
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- lighter hydrocarbons
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- heat exchanger
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The present invention provides a kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons techniques, coproduction lighter hydrocarbons while by natural gas liquefaction, using the hybrid refrigeration cycle of liquefaction process cold is provided for lighter hydrocarbons recovery, the heavy constituent in unstripped gas is detached by lighter hydrocarbons recovery process, is processed simultaneously, technique is broadly divided into mix refrigerant refrigeration cycle part and natural gas liquefaction, lighter hydrocarbons recovery part, the present invention being capable of realization device stable operation, flow is simple, equipment investment is low and thermal energy and cold energy can be comprehensively utilized fully.
Description
Technical field
The present invention relates to natural gas processing field, specifically, being to be related to a kind of azeotrope refrigeration liquefying natural gas simultaneously
Coproduction lighter hydrocarbons technique.
Background technology
Natural gas occupies more and more important role as clean energy resource in energy-consuming.In recent years, with environment dirt
The influence of dye, coal change gas and have become trend, and under the overall situation for changing gas in coal, remote districts are for the dependence of liquefied natural gas
It gradually increases, the importance of liquefied natural gas also gradually highlights.It is natural that lighter hydrocarbons recovery in natural gas is on the one hand to control
The hydrocarbon dew point of gas to reach commodity makings figureofmerit, avoids gas liquid two-phase flow；On the other hand, the liquid hydrocarbon of recycling has very big
Economic value, can both be directly used as exotic fuels, it is also possible to make industrial chemicals.For liquefied natural gas (LNG) plant, due to light
The added value higher of hydrocarbon, therefore pass through the cold of refrigeration equipment offer lighter hydrocarbons recovery, realization production in the process of natural gas liquefaction
Coproduction lighter hydrocarbons during liquefied natural gas.
The main recycling ethane of light hydrocarbon in natural gas recycling, liquefied petroleum gas and petroleum benzin etc., the technique mainly used
Method mainly has cold oil absorption technique, refrigerated separation technique, natural gas expansion process and the natural gas expansion with propane pre-cooling
Technique.Wherein natural expansion process and natural gas expansion process with propane pre-cooling are most widely used, and relative to other techniques, this two
The gas component range that kind technique uses is wide, and light hydrocarbon recovery rate is high, and the energy consumption for reaching identical yield is relatively low.But the technique also has
It has the disadvantage that, flow and equipment are relative complex, and technique employs expansion unit, and expand the core that unit is whole device and set
It is standby so that device is more demanding in design, operation and control etc., when raw material components or treating capacity change greatly, expansion
Engine efficiency declines soon, and operation can also become unstable, and technological operation is produced bigger effect.Natural gas expansion process is to air inlet pressure
Power requirement is high, when raw gas pressure is relatively low, it is also necessary to when setting outer defeated pressure higher, it is also necessary to the outer gas transmission compressor of setting.
When gas component is heavier, the natural gas expansion process of propane refrigeration need to be generally used.
Medium scale liquefied natural gas (LNG) plant uses mixed refrigeration process, and process for recovering light hydrocarbon is by hybrid refrigeration cryogen
Shallow cold section of cold is provided, but in operation, it is shallow cold since shallow cold section and cryogenic realize that cold transmits in ice chest
The temperature of section is not easy to adjust, so as to influence the stabilization of whole system operation.If additionally addition propane pre-cooling or expanding machine, meeting
The complexity of flow is further increased, and improves the overall investment of full factory.How the realization liquefied natural gas of simple economy joins
Lighter hydrocarbons technique after the meeting is produced, is the problem of needing thinking.
Invention content
It is an object of the invention to overcome the shortcoming of above-mentioned traditional technology, a kind of azeotrope refrigeration liquefying day is provided
Right gas co-production lighter hydrocarbons technique, can realization device stable operation, flow is simple, and equipment investment is low and thermal energy and cold energy energy
Enough fully comprehensive utilizations.
The purpose of the present invention is what is reached by following technical measures：A kind of azeotrope refrigeration liquefying natural gas co-production
Lighter hydrocarbons technique, coproduction lighter hydrocarbons while by natural gas liquefaction, is carried using the hybrid refrigeration cycle of liquefaction process for lighter hydrocarbons recovery
Semen donors, while by lighter hydrocarbons recovery process the heavy constituent in unstripped gas is detached, processed, technique is broadly divided into mixing system
Cryogen refrigeration cyclic part and natural gas liquefaction, lighter hydrocarbons recovery part, it is characterised in that comprise the steps of：
(1) it is pre-chilled：Natural gas is pre-chilled by precool heat exchanger device, and the cold in precool heat exchanger device is by refrigerant compressor group level-one
Liquid phase throttling provides；
(2) component detaches：The natural gas of precooling enters light hydrocarbon separator, and sub-argument goes out light component and heavy constituent, light component into
Enter and re-contact tower, heavy constituent enters lighter hydrocarbons heat exchanger after reducing pressure by regulating flow cools down and recycles cold, and heavy constituent exchanges heat by lighter hydrocarbons
Enter dethanizer after device heating；
(3) it refines：Enter from the gas of deethanizer overhead out laggard into lighter hydrocarbons reflux pump after lighter hydrocarbons heat exchanger
Enter to re-contact tower and carry out heavy hydrocarbon washing, re-contact the heavy constituent that tower bottom comes out and enter dethanizer progress rectifying, dethanizer
Lower part connects reboiler, is further detached after collecting mixed light-hydrocarbon from Deethanizer bottom, is come out from column overhead is re-contacted
Natural gas enter ice chest, by becoming liquefied natural gas after further cooling down.
(4) hybrid refrigeration cycle：The liquid isolated from refrigerant compressor group level-one enters precool heat exchanger device and cools down
Reducing pressure by regulating flow enters refrigerant compressor group import after providing cold, comes out gas from refrigerant compressor two level and liquid respectively enters
Ice chest carries out cooling reducing pressure by regulating flow and provides cold, enters system to refrigerant compressor group import by the gas and liquid reflux of ice chest
SAPMAC method.
Natural gas enters light hydrocarbon separator after precool heat exchanger device is pre-chilled to -30 DEG C.
The heavy constituent of dethanizer is exited into from light hydrocarbon separator with entering reclosing after being come out from deethanizer overhead
The gas for touching tower exchanges cold, heavy constituent heating, the gas cooling come out from deethanizer overhead at lighter hydrocarbons heat exchanger.
By adopting the above-described technical solution, compared with prior art, it is an advantage of the invention that：
Natural gas enters back into light hydrocarbon separator after precool heat exchanger device is pre-chilled to -30 DEG C, utilizes azeotrope compressor
The heavy constituent of level-one is first pre-chilled, and while reducing unit, stablizes subsequent natural gas liquefaction flow；
The heavy constituent cold isolated by the recycling of lighter hydrocarbons heat exchanger, and heavy constituent can by entering after further throttling
More colds are provided, the heavy constituent of whereabouts dethanizer from dethanizer whereabouts with re-contacting the gas of tower in lighter hydrocarbons heat exchanger
Place carries out Cooling capacity exchanging, can simplify production equipment, equipment investment is low, and flow is simple；
Using from the rate of recovery for re-contacting tower raising C3, the economic benefit of device product is further improved；
Dethanizer is combined with reboiler, and component is made to reach the separation of high-purity.
The invention will be further described with reference to the accompanying drawings and detailed description.
Description of the drawings
Attached drawing 1 is a kind of structural representation of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique of the present invention
Figure.
Wherein, 1- precool heat exchangers device, 2- light hydrocarbon separators, 3- lighter hydrocarbons heat exchangers, 4- lighter hydrocarbons recoveries pump, 5- re-contact tower,
6- dethanizers, 7- reboilers, 8- ice chests, 9- refrigerant compressor groups.
Specific embodiment
Embodiment：As shown in Figure 1, natural gas first passes around precool heat exchanger device 1 and is cooled to -30 DEG C, precool heat exchanger device 1
In cold throttled and provide by 9 level-one liquid phase of refrigerant compressor group, detach light component and heavy constituent into light hydrocarbon separator 2,
Middle light component, which enters, re-contacts tower 5, and heavy constituent enters lighter hydrocarbons heat exchanger 3 after cooling down by reducing pressure by regulating flow and recycles ice chest, heavy constituent
Enter 6 rejecting ethane of dethanizer after heating, the gas come out from 6 tower top of dethanizer, which enters after lighter hydrocarbons heat exchanger 3, to be entered
Enter after lighter hydrocarbons reflux pump 4 and re-contact the progress heavy hydrocarbon washing of tower 5.It re-contacts the heavy constituent that 5 bottom of tower comes out and enters dethanizer 6
Rectifying is carried out, enters from the mixed light-hydrocarbon of 6 bottom of dethanizer and is subsequently further detached.It is come out from 5 tower top of tower is re-contacted
Natural gas enter ice chest 8, by becoming liquefied natural gas after further cooling down.
Natural gas enters back into light hydrocarbon separator 2 after precool heat exchanger device 1 is pre-chilled to -30 DEG C, utilizes refrigerant compressor group 9
The heavy constituent of level-one is first pre-chilled, and while reducing unit, stablizes subsequent natural gas liquefaction flow.
Liquefied natural gas and heavy hydrocarbon are produced using mixed refrigeration process, wherein shallow cold separate section uses azeotrope level-one
Cryogen is pre-chilled, using lighter hydrocarbons heat exchanger 3 recycle separation heavy hydrocarbon cold, and the gas for 6 tower top of dethanizer provide it is cold
Quantitative change re-contacts tower 5 into entering after liquid, and the setting of lighter hydrocarbons heat exchanger 3 simplifies production equipment, and equipment investment is low, flow letter
It is single.
For azeotrope part, the liquid isolated from 9 level-one of refrigerant compressor group enters precool heat exchanger device 1 and is dropped
Warm reducing pressure by regulating flow enters 9 import of refrigerant compressor group after providing cold.Gas and liquid point are come out from 9 two level of refrigerant compressor group
Not Jin Ru ice chest 8 carry out cooling reducing pressure by regulating flow cold, gas and liquid reflux by ice chest 8 to refrigerant compressor group 9 be provided
Import enters refrigeration cycle.
Claims (3)
1. a kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique, coproduction lighter hydrocarbons while by natural gas liquefaction,
Cold is provided for lighter hydrocarbons recovery, while by lighter hydrocarbons recovery process in unstripped gas using the hybrid refrigeration cycle of liquefaction process
Heavy constituent is detached, is processed, and technique is broadly divided into mix refrigerant refrigeration cycle part and natural gas liquefaction, lighter hydrocarbons recovery portion
Point, it is characterised in that it comprises the steps of：
(1) it is pre-chilled：Natural gas is pre-chilled by precool heat exchanger device, and the cold in precool heat exchanger device is by refrigerant compressor group level-one liquid phase
Throttling provides；
(2) component detaches：The natural gas of precooling enters light hydrocarbon separator, and sub-argument goes out light component and heavy constituent, and light component enters weight
Contact tower, heavy constituent enter lighter hydrocarbons heat exchanger after reducing pressure by regulating flow cools down and recycle cold, and heavy constituent passes through lighter hydrocarbons heat exchanger liter
Enter dethanizer after temperature；
(3) it refines：Enter after lighter hydrocarbons heat exchanger from the gas of deethanizer overhead out after entering lighter hydrocarbons reflux pump and enter weight
Contact tower carries out heavy hydrocarbon washing, re-contacts the heavy constituent that tower bottom comes out and enters dethanizer progress rectifying, dethanizer lower part
Connect reboiler, from Deethanizer bottom collect mixed light-hydrocarbon after further detached, from re-contact column overhead come out day
Right gas enters ice chest, by becoming liquefied natural gas after further cooling down.
(4) hybrid refrigeration cycle：The liquid isolated from refrigerant compressor group level-one enters precool heat exchanger device and carries out cooling throttling
Decompression enters refrigerant compressor group import after providing cold, comes out gas from refrigerant compressor two level and liquid respectively enters ice chest
It carries out cooling reducing pressure by regulating flow and cold is provided, enter refrigeration to refrigerant compressor group import by the gas and liquid reflux of ice chest and follow
Ring.
2. a kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique according to claim 1, it is characterised in that：
Natural gas enters light hydrocarbon separator after precool heat exchanger device is pre-chilled to -30 DEG C.
3. a kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique according to claim 1, it is characterised in that：
The heavy constituent that dethanizer is exited into from light hydrocarbon separator re-contacts the gas of tower with entering after being come out from deethanizer overhead
Body exchanges cold, heavy constituent heating, the gas cooling come out from deethanizer overhead at lighter hydrocarbons heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201711445082.0A CN108165333A (en) | 2017-12-27 | 2017-12-27 | A kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201711445082.0A CN108165333A (en) | 2017-12-27 | 2017-12-27 | A kind of azeotrope refrigeration liquefying natural gas co-production lighter hydrocarbons technique |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109810740A (en) * | 2019-03-07 | 2019-05-28 | 四川迅升油气工程技术有限公司 | One kind being used for sulfur-containing gas Development & Multipurpose use system and technique |
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| CN103555382A (en) * | 2013-10-24 | 2014-02-05 | 西南石油大学 | Coproduction technology employing mixed-refrigerant cycle (MRC) natural gas liquefaction and direct heat exchange (DHX) tower light hydrocarbon recovery |
| CN205223141U (en) * | 2015-12-21 | 2016-05-11 | 杰瑞石油天然气工程有限公司 | Utilize natural qi exhaustion heavy hydrocarbon device of cold volume of high -pressure cryogen |
| CN105783421A (en) * | 2016-04-07 | 2016-07-20 | 成都赛普瑞兴科技有限公司 | Natural gas light hydrocarbon recovery method and device |
| CN106397087A (en) * | 2016-08-30 | 2017-02-15 | 西安长庆科技工程有限责任公司 | Method for recovering ethane, liquefied gas and natural gasoline from CO2-containing natural gas |
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2017
- 2017-12-27 CN CN201711445082.0A patent/CN108165333A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103555382A (en) * | 2013-10-24 | 2014-02-05 | 西南石油大学 | Coproduction technology employing mixed-refrigerant cycle (MRC) natural gas liquefaction and direct heat exchange (DHX) tower light hydrocarbon recovery |
| CN205223141U (en) * | 2015-12-21 | 2016-05-11 | 杰瑞石油天然气工程有限公司 | Utilize natural qi exhaustion heavy hydrocarbon device of cold volume of high -pressure cryogen |
| CN105783421A (en) * | 2016-04-07 | 2016-07-20 | 成都赛普瑞兴科技有限公司 | Natural gas light hydrocarbon recovery method and device |
| CN106397087A (en) * | 2016-08-30 | 2017-02-15 | 西安长庆科技工程有限责任公司 | Method for recovering ethane, liquefied gas and natural gasoline from CO2-containing natural gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109810740A (en) * | 2019-03-07 | 2019-05-28 | 四川迅升油气工程技术有限公司 | One kind being used for sulfur-containing gas Development & Multipurpose use system and technique |
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Application publication date: 20180615 |
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