CN103865601A - Heavy hydrocarbon recovery method of propane precooling and deethanizer top reflux - Google Patents
Heavy hydrocarbon recovery method of propane precooling and deethanizer top reflux Download PDFInfo
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- CN103865601A CN103865601A CN201410091169.2A CN201410091169A CN103865601A CN 103865601 A CN103865601 A CN 103865601A CN 201410091169 A CN201410091169 A CN 201410091169A CN 103865601 A CN103865601 A CN 103865601A
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Abstract
The invention provides a heavy hydrocarbon recovery method of propane precooling and deethanizer top reflux and belongs to the technical field of chemical engineering and low temperatures. The heavy hydrocarbon recovery method is designed modularly, and a liquefaction process is composed of propane precooling circulation, deethanizer top product reflux gas-liquid separation, gas-liquid separation of natural gas and natural gas heavy hydrocarbon removal, wherein the propane circulation is used for precooling a natural gas, the LPG (Liquefied Petroleum Gas), a nitrogen gas refrigerant and a deethanizer top product reflux material flow, the deethanizer top product is returned to a precooling cold box and further cooled and recycled, and the deethanizer top product does not go through gas-liquid separation after being cooled. A liquid phase obtained by virtue of the gas-liquid separation of the natural gas is returned to the precooling cold box to intensify the cooling capacity, and the process is added with a reflux part. The heavy hydrocarbon recovery method is applicable to heavy hydrocarbon recovery of the offshore liquefied petroleum gas, and the yield of the heavy hydrocarbon and the yield of the LPG both are high.
Description
Technical field:
The present invention relates to the method that in the upper a kind of high-pressure natural gas of FPSO, heavy hydrocarbon reclaims, particularly, the design that adopts deethanizer overhead gas phase to reflux, removes the heavy constituent in high-pressure natural gas in conjunction with propane pre-cooling, Sweet natural gas self expansion process.Adopt this kind of recovery process, both improved propane recovery, avoid again producing too much fuel gas, cause waste.Meanwhile, this processing unit is simple, has higher economy, is highly suitable for removing of heavy hydrocarbon in FPSO high-pressure natural gas.
Background technology:
It is abundant that China has verified coastal waters natural gas source, and the processing of gas field, deep-sea, marginal gas field and low grade natural gas resource is considerable.For the exploitation of this type of source of the gas, adopt the mode such as traditional ocean platform and seabed relation can be subject to the restriction of cost and technology, therefore adopt LNG Floating Production storage handler (LNG-FPSO), both can flexible configuration, can meet again the needs of Natural gas extraction.LNG-FPSO has is convenient to migration, reusable, production efficiency advantages of higher, and this,, to promoting China's especially gas field, deep-sea, small-sized gas field development of marine site, makes full use of hydrocarbon resources significant.
Liquefaction process is one of core technology of LNG-FPSO, meet that safety, flow process are simple, strong adaptability, start-stop car rapidly and level of automation high.As the important step in liquefaction process, heavy hydrocarbon recovery process needs equally to meet following requirement: the Sweet natural gas after (1) de-heavy hydrocarbon enters before liquefaction unit wherein C6+ component concentration and meets liquefaction process requirement; (2) process operation is stable, and fluctuation is little; (3) strong adaptability to different sources of the gas; (4) many recovery heavy hydrocarbon as far as possible, to improve the economy of device; (5) technique is simple, and equipment is as far as possible few, and floor space is little; (6) safe and reliable.Before natural gas liquefaction, must remove heavy hydrocarbon, otherwise, may in liquefaction process, freeze and occluding device.Land liquefaction factory generally adopts distillation method to remove heavy hydrocarbon in pretreatment technology, adopts deethanizing column and liquefied gas tower production fluid in next life liquefied oil gas, remains a small amount of heavy hydrocarbon and separates and remove in cold zone.And land technical process complexity, floor space are large and be difficult for installing, afloat suitability is poor.Therefore, existingly generally can not be directly used in LNG-FPSO for land heavy hydrocarbon recovery process, need to study a kind of novel process that is applicable to ocean environment.
Summary of the invention:
Object of the present invention is intended to propose a kind of heavy hydrocarbon recovery method ocean environment, that propane pre-cooling deethanizing tower top simple, that have high propane recovery refluxes that is applicable to.
The present invention is that the general thought that realizes its object is: utilize the cold of propane pre-cooling unit and Sweet natural gas self expansion step-down cooling to remove the heavy hydrocarbon in high-pressure natural gas, in order to improve the output of propane recovery, minimizing fuel gas, increase the technique that deethanizing top gaseous phase is back to contact tower, utilize HYSYS to simulate and parameter optimization technique, make it reach good separating effect.
Object of the present invention is achieved through the following technical solutions: the production equipment that is used for realizing technical scheme comprises a propane pre-cooling section ice chest, two separators, Natural gas expander, multiple throttling valve, a contact tower, a deethanizing column, a debutanizing tower and a mixing tank.First Sweet natural gas by seabed extraction carries out pre-treatment, remove silt wherein, water, sour gas, mercury, after benzene and impurity, enter propane pre-cooling ice chest unit, through expanding after propane pre-cooling section ice chest, enter deethanizing tower top product reflux gas-liquid separation unit, Sweet natural gas gas-liquid separation unit and natural qi exhaustion heavy hydrocarbon unit, make full use of the cold that propane refrigerant provides, realizing heavy hydrocarbon in conjunction with Sweet natural gas self expansion step-down cooling removes, the product obtaining is further cut apart, obtain liquefied petroleum gas (LPG) and condensate oil, enter respectively storage tank stores, the Sweet natural gas removing after heavy hydrocarbon enters liquefaction unit.
In propane pre-cooling ice chest unit, adopt the cold mode of three tier structure, propane passes through high-pressure separator, MP (medium pressure) separator and light pressure separator successively, isolated gas phase recycles respectively after propane compressor, water-cooled, throttling, and liquid phase enters precooling ice chest precooling Sweet natural gas, LPG, nitrogen gas refrigerant and the logistics of deethanizing tower top product reflux as low-temperature receiver.Propane first by compressor boost to 1.36MPa, propane after throttling to pressure is 0.55MPa and one-level re-heat enters separator jointly, gas phase after separation enters three-stage compressor entrance, liquid phase is divided into two portions, part liquid phase enters ice chest for cooled natural gas and nitrogen, another part throttling to pressure is that 0.29MPa enters second stage separator and separates, the gas phase separating enters two stage compressor compression, isolated liquid phase is divided into two portions, a part enters ice chest for cooled natural gas and nitrogen, another part throttling to pressure is that 0.13MPa enters third stage separator and separates, the gas phase separating enters one-level compressor compresses, the liquid phase separating enters ice chest for cooled natural gas and nitrogen.Come precooling Sweet natural gas and follow-up liquefaction unit by nitrogen gas refrigerant, and simultaneously for deethanizing tower top product LPG provides cold.36 ℃ of Sweet natural gases, the 7.14MPa of depickling dehydration, through propane pre-cooling to temperature for-32 ℃, pressure be 7.09MPa, enter gas-liquid two-phase separator, separator outlet gas phase enter Natural gas expander be expanded to temperature for-55.35 ℃, pressure be 4.5MPa, as contact tower charging; Separator outlet liquid phase section flow to temperature for-40.14 ℃, pressure be 4.7MPa, return to propane pre-cooling ice chest cooling after temperature rise to 31 ℃, pressure 4.65MPa, as contact tower charging.For guaranteeing the needs of follow-up liquefaction unit to gas pressure, reduce as far as possible liquefaction energy consumption, the pressure after Sweet natural gas expands can not be too low, but will meet the needs that heavy hydrocarbon reclaims simultaneously, is chosen to be 4.5MPa herein after optimizing.
In deethanizing tower top product reflux gas-liquid separation unit, deethanizing top gaseous phase product enters gas-liquid separator after precooling ice chest is cooling, isolate implication phase and enter dinitrogen swell refrigeration liquefaction unit with contacting top gaseous phase Product mix, separator outlet liquid phase with after Sweet natural gas precooling, separate liquid-phase mixing as the charging of contact tower tower top.
The Sweet natural gas of contact tower top outlet-49.7 ℃, 4.4MPa enters follow-up liquefaction unit, and at the bottom of tower, to flow to pressure be that 2.95MPa enters deethanizing column top for-55.53 ℃, the liquid phase section of 4.45MPa.-22.67 ℃ of deethanizing tower top outlet, gas compression to the temperature of 2.85MPa are that 8.2 ℃, pressure are 4.45MPa, be back to again propane pre-cooling ice chest be cooled to temperature for-32 ℃, pressure be 4.42MPa, carry out gas-liquid separation, isolated liquid phase with from the liquid-phase mixing of natural-gas separator as contact tower charging, isolated gas phase with contact top gaseous phase Sweet natural gas mix, enter contact tower; At the bottom of tower, to flow to pressure be after 0.65MPa, to enter debutanizing tower top for 110 ℃, the liquid phase section of 2.9MPa.Debutanizing tower top liquid-phase product is 11.13 ℃, the LPG of 0.55MPa, is that 0.12MPa enters storage tank stores through propane-cooled to temperature for-32 ℃ of deutomerite flow to pressure; At the bottom of tower, liquid-phase product is 120 ℃, the condensate oil of 0.6MPa, and the cooling throttling of this product is to entering storage tank stores after normal pressure under-32 ℃, 0.12MPa condition.
In Sweet natural gas gas-liquid separation unit, enter gas-liquid separator through the Sweet natural gas of precooling, isolated liquid phase is returned to precooling ice chest cold is provided after throttling, and gas phase enters deethanizing column bottom after decompressor expands.
In natural qi exhaustion heavy hydrocarbon unit, expand into 4.5MPa from decompressor Sweet natural gas out, after-55.35 ℃, enter heavy hydrocarbon separating unit, in heavy hydrocarbon separating unit, utilize a deethanizing column and a debutanizing tower to realize removing of Sweet natural gas heavy hydrocarbon, deethanizing tower top product reflux is cooling to precooling ice chest, and it is cooling that debutylize tower top product is that LPG is back to precooling ice chest.
This heavy hydrocarbon recovery process structure is more land simple, and the light constituent content in the LPG simultaneously obtaining and condensate oil product is all well controlled, and is qualified product.Take full advantage of the pressure energy of high-pressure natural gas, the Sweet natural gas after de-heavy hydrocarbon meets the needs of liquefaction process.Utilize HYSYS flowsheeting software to carry out simulation, parameter optimization and sensitivity analysis to technique, improved propane recovery, verified the stability of technique.The treatment capacity of this technique reaches 2,760,000 tons/year, and LPG product is 11.49 ten thousand tons/year, and condensate yield is 7.34 ten thousand tons/year.
For assurance device safe and reliable operation under the condition of rocking, type selecting to equipment and installation have proposed following requirement: in flow process, gas conditioning amount is larger, decompressor is recommended to select turbo-expander, and size is little, working stability, better to the adaptability of marine operating mode; Propane pre-cooling ice chest adopts plate-fin heat exchanger, and compact construction, stable performance, be a kind of interchanger that current liquefied natural gas (LNG) plant is generally used.Separator should be arranged on the axis of hull as far as possible, and tower should be controlled tower height as far as possible, rocks the impact on separating effect to reduce hull.
The invention has the beneficial effects as follows: the heavy hydrocarbon recovery process that adopts propane pre-cooling to be combined with Sweet natural gas expansion phase, deethanizing top gaseous phase is back to contact tower, increase considerably propane recovery, improve the economy of technique.Make full use of the cold of propane pre-cooling unit, and utilize the pressure energy of high-pressure natural gas self, reclaim the heavy constituent in high-pressure natural gas.Employing blocking design, facility compact, is convenient to install.Flow process valve member is few, equipment is simple, adopts unitary system cryogen, has reduced the start time of a lot of utility appliance, and without carrying out the operations such as refrigeration agent proportioning, control texture is simple, and start-stop car is rapid.Propane pre-cooling circulation can effectively utilize the propane latent heat of vaporization, reduces the energy consumption of flow process.The defect that preferably resolves existing heavy hydrocarbon recovery process equipment complexity, is applicable to ocean production environment.The conditions such as the composition of this recovery process to Sweet natural gas, temperature, pressure are insensitive, and product all meets the requirements.
Accompanying drawing explanation:
Fig. 1 is LNG Lquified Process Flow figure of the present invention.
Fig. 2 is the precooling ice chest cell schematics of liquefaction process.
Fig. 3 is gas-liquid separation schematic diagram after deethanizing tower top product reflux.
Fig. 4 is Sweet natural gas gas-liquid separation unit schematic diagram.
Fig. 5 is the heavy hydrocarbon separating unit schematic diagram of liquefaction process.
In figure, 1-precooling zone ice chest, 2-contact tower, 3-deethanizing column, 4-debutanizing tower, 5-stabilizer tower, 6-first throttle valve, 7-gas-liquid separator, 8-Natural gas expander, 10-the second throttling valve, 11-the first splitter, 12-compressor, 13-the 3rd throttling valve, 14-the first water cooler, 15-the 4th throttling valve, 16-the 5th throttling valve, 17-LPG storage tank, 18-pump, 19-the second water cooler, 20-the first mixing tank, 21-the 3rd water cooler, 22-NGL storage tank, 26-the first circulator, 27-first paragraph pipeline, 28-second segment pipeline, 29-the 3rd segment pipe, 30-high-pressure separator, 31-the second splitter, 32-the 4th segment pipe, 33-the second circulator, 34-the 6th throttling valve, 35-MP (medium pressure) separator, 36-the 3rd splitter, 37-the 5th segment pipe, 38-the 3rd circulator, 39-the 7th throttling valve, 40-light pressure separator, 41-the 6th segment pipe, 42-the 4th circulator, 43-the 5th circulator, 44-propane compressor I, 45-the 6th circulator, 46-the second mixing tank, 47-propane compressor II, 48-the 7th circulator, 49-the 3rd mixing tank, 50-propane compressor III, 51-the 4th water cooler, 52-the 8th circulator, 53-propane throttling valve, the logistics of 61～62-deethanizing tower top product reflux, 63～64-LPG logistics, 65～66-nitrogen stream, 67～68-natural gas stream, 69～70-reflux stream, the logistics of 71～76-propane, 77～82-natural gas stream.
Embodiment:
Below in conjunction with drawings and Examples, the present invention is described further.
As shown in Figure 1, suppose that pretreated gas pressure is 7.14MPa, temperature is 36.0 ℃, and this flow process is made up of propane pre-cooling circulation and natural qi exhaustion heavy hydrocarbon technique.
In propane pre-cooling ice chest unit, adopt three grades of precoolings.Propane is first separated into gas-liquid two-phase through high-pressure separator 30, gas phase flows in propane compressor III 50 after mixing with the gas compressing through propane compressor II 47, being compressed to temperature and being 52.2 ℃, pressure is to be cooled to 31 ℃ through the 4th water cooler 51 after 1.36MPa, propane is all liquefied, be depressurized to 0.55MPa through propane throttling valve 53 again, temperature is down to 5 ℃, mixes, then flow in high-pressure separator 30 with the propane from ice chest re-heat.Be 4.7 ℃ from the isolated liquidus temperature of high-pressure separator 30, this liquid phase part flows into precooling zone ice chest 1 and carries out first step precooling Sweet natural gas, LPG, nitrogen gas refrigerant and the logistics of deethanizing tower top product reflux, thereby completes first step propane pre-cooling.The isolated another part liquid phase of high-pressure separator 30 is depressurized to 0.29MPa through the 6th throttling valve 34, be cooled to-15 ℃, after mixing with the fluid after the precooling of the second stage, flow into MP (medium pressure) separator 35 and carry out gas-liquid separation, isolated gas phase flows into propane compressor II 47 after mixing with the gas compressing through propane compressor I 44 and compresses, now liquidus temperature is-15 ℃, this liquid phase part flows into precooling zone ice chest 1 and carries out second stage precooling Sweet natural gas, LPG, nitrogen gas refrigerant and the logistics of deethanizing tower top product reflux, completes second stage propane pre-cooling.The isolated another part liquid phase of MP (medium pressure) separator 35 is depressurized to 0.13MPa through the 7th throttling valve 39, be cooled to-36 ℃, mix with the fluid after third stage precooling, flow into again light pressure separator 40 and carry out gas-liquid separation, isolated gas phase enters propane compressor I 44, and to be compressed to pressure be 0.29MPa, liquid phase flows into precooling zone ice chest 1 and carries out third stage precooling Sweet natural gas, LPG, nitrogen gas refrigerant and the logistics of deethanizing tower top product reflux, thereby realizes third stage precooling.
In natural qi exhaustion heavy hydrocarbon unit, Sweet natural gas is-32 ℃ through precooling zone ice chest 1 by propane pre-cooling to temperature after the preprocessing process such as depickling, removing impurities matter, then enter gas-liquid separator 7 and carry out gas-liquid separation, isolated gas phase, after Natural gas expander 8 is expanded to pressure and is 4.5MPa, enters contact tower 2 bottoms; After isolated liquid phase throttling, be back to precooling zone ice chest 1 precooling Sweet natural gas, LPG and nitrogen gas refrigerant as low-temperature receiver, enter afterwards the top of contact tower 2.The gaseous products of contact tower 2 tower tops enters natural gas liquefaction unit, at the bottom of contact tower 2 towers liquid phase after the second throttling valve 10 throttlings as the charging of deethanizing column 3, it is that 8.2 ℃, pressure are 4.45MPa that deethanizing column 3 top gaseous phase products are compressed to temperature through compressors 12, be back to precooling zone ice chest 1 and be cooled to temperature and be-32 ℃, as the charging of contact tower 2 tower tops.At the bottom of deethanizing column 3 towers liquid phase after the 3rd throttling valve 13 throttlings as the charging of debutanizing tower 4.The overhead product of debutanizing tower 4 is LPG, is back to that precooling zone ice chest 1 is cooling, flows into LPG storage tank 17 after throttling, and debutanizing tower 4 bottom products are condensate oil.
Fig. 2 is the precooling ice chest cell schematics of liquefaction process, wherein the logistics 61～62 of deethanizing tower top product reflux as thermal source in heat exchange ice chest by the process of precooling, the process that LPG logistics 63～64 is cooled as thermal source for LPG in heat exchange ice chest, the process that nitrogen stream 65～66 is cooled in heat exchange ice chest for nitrogen, natural gas stream 67～68 be Sweet natural gas in heat exchange ice chest by the process of precooling, reflux stream 69～70 is that reflux stream is as low-temperature receiver precooling Sweet natural gas in heat exchange ice chest, LPG, the process of nitrogen gas refrigerant and the logistics of deethanizing tower top product reflux, propane logistics 71～76 is as low-temperature receiver precooling Sweet natural gas in heat exchange ice chest after propane refrigerant throttling, LPG, the process of nitrogen gas refrigerant and the logistics of deethanizing tower top product reflux.This precooling ice chest unit is made up of heat exchange ice chest 1 and 16 throttling valve.
Fig. 3 is gas-liquid separation schematic diagram after deethanizing tower top product reflux, deethanizing tower top product reflux logistics 62 is through the logistics of the cooled deethanizing tower top of precooling ice chest product reflux, natural gas stream 77 is deethanizing tower top product reflux logistics liquid phase streams after gas-liquid separation, natural gas stream 78 and natural gas stream 79 are deethanizing tower top product reflux logistics gaseous streams after gas-liquid separation, natural gas stream 78 enters Article 2 line, and natural gas stream 79 goes dinitrogen swell refrigeration liquefaction unit.After this deethanizing tower top product reflux, gas-liquid separation unit is made up of gas-liquid separator 2 and splitter 11.
Fig. 4 is the gas-liquid separation unit schematic diagram of liquefaction process, and natural gas stream 68 is the Sweet natural gases from precooling zone ice chest 1, and reflux stream 69 is back to precooling zone ice chest 1 as low-temperature receiver, at the bottom of natural gas stream 80 removes contact tower tower.The gas-liquid separation unit of this liquefaction process is made up of gas-liquid separator 7, Natural gas expander 8 and throttling valve 10.
Fig. 5 is the heavy hydrocarbon separating unit schematic diagram of liquefaction process, natural gas stream 80 is the Sweet natural gases from gas-liquid separation unit, reflux stream 70 is reflux streams that cold is provided for precooling zone ice chest 1, natural gas stream 77 is the deethanizing tower top product reflux logistics after gas-liquid separation, natural gas stream 81 goes to liquefaction stages ice chest unit, deethanizing tower top product reflux logistics 61 is that deethanizing top gaseous phase product goes precooling zone ice chest 1 to be cooled, LPG logistics 63 is LPG products, go precooling zone ice chest 1 cooling, after throttling, remove LPG storage tank, natural gas stream 82 is condensate oils, through water-cooled, after throttling, remove NGL storage tank.The heavy hydrocarbon separating unit of this liquefaction process is made up of the tower 3 with reboiler, tower 4, separator 2, compressor 12, throttling valve 10 and throttling valve 13.
Claims (1)
1. the heavy hydrocarbon recovery method that propane pre-cooling deethanizing tower top refluxes, is divided into propane pre-cooling ice chest unit, deethanizing tower top product reflux gas-liquid separation unit, Sweet natural gas gas-liquid separation unit and natural qi exhaustion heavy hydrocarbon unit design, and its production equipment comprises a propane pre-cooling section ice chest, two separators, a Natural gas expander, multiple throttling valve, a contact tower, a deethanizing column, a debutanizing tower and a mixing tank, first carry out pre-treatment by the Sweet natural gas of seabed extraction, removes silt wherein, water, sour gas, mercury, after benzene and impurity, enter propane pre-cooling ice chest unit, through expanding after propane pre-cooling section ice chest, enter deethanizing tower top product reflux gas-liquid separation unit, Sweet natural gas gas-liquid separation unit and natural qi exhaustion heavy hydrocarbon unit, make full use of the cold that propane refrigerant provides, realizing heavy hydrocarbon in conjunction with Sweet natural gas self expansion step-down cooling removes, the product obtaining is further cut apart, obtain liquefied petroleum gas (LPG) and condensate oil, enter respectively storage tank stores, it is characterized in that according to the following steps:
1. in propane pre-cooling ice chest unit, employing three tier structure is cold, propane passes through high-pressure separator, MP (medium pressure) separator and light pressure separator successively, isolated gas phase recycles respectively after propane compressor, water-cooled, throttling, liquid phase enters precooling ice chest precooling Sweet natural gas, LPG, nitrogen gas refrigerant and the logistics of deethanizing tower top product reflux as low-temperature receiver, and the propane temperature that three grades of precoolings enter ice chest is respectively 4.7 ℃ ,-15 ℃ ,-36 ℃;
2. in deethanizing tower top product reflux gas-liquid separation unit, deethanizing top gaseous phase product enters gas-liquid separator after precooling ice chest is cooling, isolate implication phase and enter dinitrogen swell refrigeration liquefaction unit with contacting top gaseous phase Product mix, separator outlet liquid phase with after Sweet natural gas precooling, separate liquid-phase mixing as the charging of contact tower tower top;
3. in Sweet natural gas gas-liquid separation unit, enter gas-liquid separator through the Sweet natural gas of precooling, isolated liquid phase is returned to precooling ice chest cold is provided after throttling, and gas phase enters deethanizing column bottom after decompressor expands;
4. in natural qi exhaustion heavy hydrocarbon unit, from expanding into 4.5MPa, decompressor Sweet natural gas out enters heavy hydrocarbon separating unit, in heavy hydrocarbon separating unit, utilize a deethanizing column and a debutanizing tower to realize removing of Sweet natural gas heavy hydrocarbon, deethanizing tower top product reflux is cooling to precooling ice chest, and it is cooling that debutylize tower top product is that LPG is back to precooling ice chest.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104296499A (en) * | 2014-10-21 | 2015-01-21 | 杭州中泰深冷技术股份有限公司 | Double-turbine boosting expansion machine propane dehydrogenation cold box separation system and technique |
| CN104792115A (en) * | 2015-04-29 | 2015-07-22 | 中国海洋石油总公司 | Heavy hydrocarbon recycling system and technology for LNG-FPSO |
| CN104833175A (en) * | 2015-04-15 | 2015-08-12 | 中国海洋石油总公司 | FLNG/FLPG oil gas pretreatment and liquefaction method |
| CN105016965A (en) * | 2015-07-06 | 2015-11-04 | 淮阴师范学院 | Separation of chloromethane and chloroethane mixture by throttling expansion method |
| CN106595223A (en) * | 2016-11-22 | 2017-04-26 | 西安长庆科技工程有限责任公司 | System and method for recycling propane and C3<+> hybrid hydrocarbon in natural gas |
| CN107163975A (en) * | 2017-05-27 | 2017-09-15 | 中国石油集团工程设计有限责任公司 | The device and method that a kind of lighter hydrocarbons depth is reclaimed |
| CN111133081A (en) * | 2017-09-06 | 2020-05-08 | 林德工程北美有限公司 | Method for providing refrigeration in a natural gas liquids recovery plant |
| RU2739738C2 (en) * | 2019-04-30 | 2020-12-28 | Андрей Владиславович Курочкин | Deethanization unit of mains gas (versions) |
| CN112852514A (en) * | 2019-11-27 | 2021-05-28 | 中国石油天然气股份有限公司 | Natural gas recovery device |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040244415A1 (en) * | 2003-06-02 | 2004-12-09 | Technip France And Total S.A. | Process and plant for the simultaneous production of an liquefiable natural gas and a cut of natural gas liquids |
| CN1743418A (en) * | 2005-09-23 | 2006-03-08 | 河南中原绿能高科有限责任公司 | Method for removing heavy hydrocarbon in natural gas by adsorption of heavy hydrocarbon |
| WO2006047098A2 (en) * | 2004-10-25 | 2006-05-04 | Conocophillips Company | Lng system employing stacked vertical heat exchangers to provide liquid reflux stream |
| US20100132405A1 (en) * | 2007-06-22 | 2010-06-03 | Kanfa Aragon As | Method and system for producing LNG |
| CN101787314A (en) * | 2010-04-01 | 2010-07-28 | 中国石油大学(华东) | Process for compact natural gas liquefying and floating production |
| CN101948706A (en) * | 2010-08-18 | 2011-01-19 | 中国海洋石油总公司 | Mixed refrigerant and nitrogen expansion combinational refrigeration type natural gas liquefying method |
| CN102093921A (en) * | 2011-01-20 | 2011-06-15 | 中国海洋石油总公司 | Offshore natural gas liquefying method and device |
| CN103438661A (en) * | 2013-08-30 | 2013-12-11 | 北京麦科直通石化工程设计有限公司 | Novel low-energy-consumption natural gas liquefaction technology |
-
2014
- 2014-03-13 CN CN201410091169.2A patent/CN103865601B/en not_active Expired - Fee Related
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040244415A1 (en) * | 2003-06-02 | 2004-12-09 | Technip France And Total S.A. | Process and plant for the simultaneous production of an liquefiable natural gas and a cut of natural gas liquids |
| WO2006047098A2 (en) * | 2004-10-25 | 2006-05-04 | Conocophillips Company | Lng system employing stacked vertical heat exchangers to provide liquid reflux stream |
| CN1743418A (en) * | 2005-09-23 | 2006-03-08 | 河南中原绿能高科有限责任公司 | Method for removing heavy hydrocarbon in natural gas by adsorption of heavy hydrocarbon |
| US20100132405A1 (en) * | 2007-06-22 | 2010-06-03 | Kanfa Aragon As | Method and system for producing LNG |
| CN101787314A (en) * | 2010-04-01 | 2010-07-28 | 中国石油大学(华东) | Process for compact natural gas liquefying and floating production |
| CN101948706A (en) * | 2010-08-18 | 2011-01-19 | 中国海洋石油总公司 | Mixed refrigerant and nitrogen expansion combinational refrigeration type natural gas liquefying method |
| CN102093921A (en) * | 2011-01-20 | 2011-06-15 | 中国海洋石油总公司 | Offshore natural gas liquefying method and device |
| CN103438661A (en) * | 2013-08-30 | 2013-12-11 | 北京麦科直通石化工程设计有限公司 | Novel low-energy-consumption natural gas liquefaction technology |
Non-Patent Citations (2)
| Title |
|---|
| 朱建鲁等: "CO2预冷双氮膨胀天然气液化工艺的海上适应性分析", 《天然气工业》 * |
| 朱建鲁等: "海上天然气液化工艺流程优选", 《天然气工业》 * |
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