CN101787314A - Process for compact natural gas liquefying and floating production - Google Patents
Process for compact natural gas liquefying and floating production Download PDFInfo
- Publication number
- CN101787314A CN101787314A CN 201010140435 CN201010140435A CN101787314A CN 101787314 A CN101787314 A CN 101787314A CN 201010140435 CN201010140435 CN 201010140435 CN 201010140435 A CN201010140435 A CN 201010140435A CN 101787314 A CN101787314 A CN 101787314A
- Authority
- CN
- China
- Prior art keywords
- natural gas
- liquefaction
- nitrogen
- circulation
- propane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 238000000034 method Methods 0.000 title claims abstract description 63
- 239000003345 natural gas Substances 0.000 title claims abstract description 44
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 238000007667 floating Methods 0.000 title claims abstract description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 105
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000001294 propane Substances 0.000 claims abstract description 29
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 26
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 26
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 26
- 238000013461 design Methods 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 239000002826 coolant Substances 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 21
- 235000009508 confectionery Nutrition 0.000 claims description 17
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 12
- 238000005057 refrigeration Methods 0.000 claims description 11
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000010276 construction Methods 0.000 claims description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 2
- 238000000605 extraction Methods 0.000 claims description 2
- 239000012535 impurity Substances 0.000 claims description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 2
- 229910052753 mercury Inorganic materials 0.000 claims description 2
- 239000013535 sea water Substances 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 48
- 239000003949 liquefied natural gas Substances 0.000 abstract description 17
- 238000001816 cooling Methods 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract 1
- 210000000038 chest Anatomy 0.000 description 36
- 239000007788 liquid Substances 0.000 description 17
- 239000003915 liquefied petroleum gas Substances 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 9
- 238000007906 compression Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 8
- 238000003860 storage Methods 0.000 description 8
- 230000006835 compression Effects 0.000 description 6
- 239000003507 refrigerant Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 238000009434 installation Methods 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000005457 optimization Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000003653 coastal water Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000010977 jade Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000004172 nitrogen cycle Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 210000000689 upper leg Anatomy 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
Abstract
The invention provides a process for compact natural gas liquefying and floating production and belongs to the field of chemical and cryogenic techniques. In the process, a modular design is adopted, and a liquefaction process consists of propane precooling circulation, double nitrogen expansion cooling circulation, natural gas heavy hydrocarbon removal and liquefaction pipe, wherein propane circulation is used for precooling natural gas and providing a nitrogen coolant; the double nitrogen expansion cooling circulation is used for deeply cooling and liquefying the natural gas; and the heavy hydrocarbon separation is realized by the cold energy generated in liquefaction. The process is suitable for producing liquid natural gas offshore and can prevent the influences of the shaking of a ship on a liquefying process.
Description
Technical field
The present invention relates to the production technique of a kind of natural gas liquids (LNG), particularly, realize that by utilizing the cold in the liquefaction process heavy hydrocarbon separates and the modular design of liquefaction process, expand by the dinitrogen that adopts the propane precooling simultaneously and design and the process flow operation Parameter Optimization, improve efficient, processing power and the seaworthiness of technology, be applicable to ocean environment LNG production preferably.
Background technology
China's coastal waters natural gas source is abundant, and total geological resource amount is about 5.9 tcms.Yet the marine natural gas source of China disperses, and is distributed widely in basin, the mouth of the Zhujiang River, Yinggehai Basin ground, basin, the fine jade southeast, EAST CHINA SEA CONTINENTAL SHELF basin and basin, Bohai Sea Gulf, and wherein quite a few is gas field, deep-sea, marginal little gas field and low taste natural gas source.For these sources of the gas, if adopt modes such as traditional ocean stationary platform or submerged pipeline, exploitation then can can't be dropped into because of cost or technical limitation in most gas fields.Adopt natural gas liquids Floating Production storage handler (LNG-FPSO), can be according to the production status flexible configuration of marine natural-gas field, natural gas liquids aboard ship, be transported to the point of destination again, have and be convenient to migration, reusable, production efficiency advantages of higher, this is to promoting China's especially gas field, deep-sea, small-sized gas field development of marine site, and it is significant to make full use of hydrocarbon resources.
As one of core of LNG-FPSO, the design of liquefaction process will produce very big influence to capital construction cost, working cost, serviceability and the security of engineering.Simultaneously, because the particular surroundings of offshore operation has proposed following requirement to process program: (1) flow process is simple, facility compact, occupation of land less, satisfy marine installation needs; (2) liquefaction flow path is eager to excel to the Sweet natural gas adaptability in the different places of production, and it is high that thermo-efficiency is wanted; (3) safe and reliable, the motion of hull can not influence its performance significantly.(4) can quick shutdown when facing severe weather, can start shooting rapidly after moving to another production position; (5) production automation degree height, the device serviceability is strong.Before Sweet natural gas is liquefied, remove heavy hydrocarbon, otherwise heavy hydrocarbon may freeze and occluding device.By land in the liquefied natural gas (LNG) plant, heavy hydrocarbon generally is to adopt distillation method to remove in advance in pretreatment technology, and in order to reclaim liquefied petroleum gas (LPG) (LPG), general deethanizing column and the liquefied gas tower of adopting realized, remaining a spot of heavy hydrocarbon is removed in the one or more separators in cold zone usually, but the flow process complexity of distillation tower, floor space are big and be difficult for installing, and marine suitability is relatively poor.Therefore, land existing natural gas liquefaction flow process generally can not be directly used among the LNG-FPSO, and the Floating Production of natural gas liquids is as a kind of new technology, and at present domestic and international rarely seen relevant report does not more have the real marine LNG production project of implementing.
Summary of the invention
For overcoming little, the inefficient defective of marine the suitability relatively poor and conventional nitrogen expansion process processing power of existing natural gas liquefaction technology, the objective of the invention is to propose a kind of process for compact natural gas liquefying and floating production, by utilizing the cold in the liquefaction process to realize that heavy hydrocarbon separates, the modular design and the process flow operation Parameter Optimization of liquefaction process, can be applicable to well that the LNG of ocean environment produces.
Purpose of the present invention is achieved through the following technical solutions: utilize two separators and a rectifying tower to realize that heavy hydrocarbon separates, tripping device is fully in liquefaction unit, can make full use of the cold in the liquefaction process, isolated heavy hydrocarbon advances tank stores, wait to transport to and carry out the lime set stabilizing treatment again after land, specifically be that Sweet natural gas by the seabed extraction at first enters pretreatment unit, remove silt wherein, water, sour gas, mercury, enter liquefaction unit behind the impurity such as benzene, liquefaction unit is circulated by the propane precooling, the nitrogen expansion refrigeration cycle, natural qi exhaustion heavy hydrocarbon, the liquefaction pipeline is formed.
In propane precooling circulation, the compressed machine of propane is pressurized to about 1.6MPa, takes away the part heat through watercooler propane is all liquefied, and reduces to-36 ℃ through the throttling valve temperature again, is used for precooling Sweet natural gas and nitrogen gas refrigerant.
In the circulation of nitrogen swell refrigeration, being chilled to-33 ℃ in advance by propane in the heat exchange ice chest after, high pressure nitrogen is divided into two strands, one directly enters decompressor and expands, another thigh enters and enters the decompressor expansion heat exchange ice chest further is chilled to-85 ℃ in advance by low-pressure nitrogen after, two strands of low-pressure nitrogens after the expansion backflow and cool off high pressure nitrogen refrigeration agent and Sweet natural gas respectively, be compressed to 8MPa through decompressor supercharging blower and nitrogen compressor successively then, all cool off after every grade of compression by water cooler, after mixing, two strands of high pressure nitrogens after the compression enter the heat exchange ice chest, the circulation of beginning next round by the propane precooling.
In natural qi exhaustion heavy hydrocarbon and liquefaction pipeline, pretreated Sweet natural gas enters the heavy hydrocarbon separating unit be pre-chilled to-30 ℃ by propane in the heat exchange ice chest after.In the heavy hydrocarbon separating unit, Sweet natural gas enters primary separator and carries out gas-liquid separation, separate back liquid and directly enter the rectifying tower middle part, gas enters and enters separator the heat exchange ice chest further is cooled to-65 ℃ by low-pressure nitrogen after and carry out gas-liquid separation, separate back liquid and directly enter the rectifying tower top, gas enters the heat exchange ice chest and further is cooled to-151 ℃ by low-pressure nitrogen and makes it all liquefaction and cold excessively, be cooled to-160 ℃ through the throttling valve throttling again, wherein about 7% liquid gasification, gas-liquid mixture enters the LNG surge tank and carries out gas-liquid separation, separate back liquid and enter the LNG storage tank stores, gas can be used as the low-temperature receiver that the Sweet natural gas method of cooling is dewatered after the buffering abhiseca is discharged, can be used as the resurgent gases on absorption tower in the pretreatment system after the re-heat, enter the use that acts as a fuel or generate electricity of fuel gas pipe network at last.The rectifier bottoms product is depressurized to 1.0MPa through throttling valve, ℃ enters the LPG surge tank through water cooler heat exchange to 35 then and carries out gas-liquid separation, separates back gas and can be used as fuel and use, and liquid enters the LPG storage tank stores, and this LPG product contains more C
5Above component, needing further to handle through land based installation could be as qualified product.
According to the characteristics of this flow process, liquefaction process is divided into four modules such as heat exchange ice chest module, heavy hydrocarbon separation module, hydrodynamic force module and product stock and designs.
This flow process is on the basis of existing nitrogen swell refrigeration circulation technology, adopt the dinitrogen of propane precooling expand design and utilize according to energy expenditure minimum for target to nitrogen high-pressure, nitrogen low pressure, nitrogen expansion in the flow process before before the temperature, Sweet natural gas throttling parameter such as temperature carried out essential, the processing power and the efficient of nitrogen expansion process have been improved, the processing power of this technology can reach 3,000,000 tons/year, liquefied fraction 93% is 0.42kWh/Nm than power consumption
3, be much better than common nitrogen expansion liquefaction process.
Be assurance device safe and reliable operation under the condition of rocking, type selecting and installation to equipment have proposed following requirement: the pressure ratio of required nitrogen compressor is bigger in the flow process, radial compressor is selected in recommendation for use, and compact construction, light weight, floor space little, operate steadily, be applicable to ocean environment; The nitrogen circulation amount is bigger in the flow process, and decompressor is recommended to select turbo-expander for use, and size is little, working stability, and is better to the adaptability of marine operating mode; Plate-fin heat exchanger compact construction, stable performance are a kind of interchanger that present liquefied natural gas (LNG) plant is generally used.Separator should be installed on the axis of hull, rocks influence to separating effect to reduce hull.
The invention has the beneficial effects as follows: adopt the dinitrogen expansion design of propane precooling, the heavy hydrocarbon separating unit has utilized the cold in the liquefaction process to realize that heavy hydrocarbon separates, the modular design and the process flow operation Parameter Optimization of liquefaction process fully, has reduced the load of pretreatment unit.Wherein, water cooler can utilize seawater to carry out refrigeration cycle.The modular design of liquefaction process can make facility compact, is convenient to install.Major cycle is nitrogen cycle in the liquefaction unit, and nitrogen can be produced by nitrogen gas generator, do not need to store, and the safe distance between each system can suitably shorten, and floor space is reduced; And nitrogen is in gas phase all the time in the circulation, is subjected to the influence of ship motion hardly, and nitrogen expansion cycles flow process is safer with the flow process of using the flammable coolant technology; Because the flow process valve member is few, equipment is few, and be the unitary system cryogen, reduced the start time of a lot of utility appliance, do not need operations such as refrigeration agent proportioning, control is simple and drive, stop rapid.Propane precooling circulation can effectively utilize the propane latent heat of vaporization, reduces the energy consumption of flow process.Solve little, the inefficient defective of marine the suitability relatively poor and conventional nitrogen expansion process processing power of existing liquefaction technology preferably.This flow process is insensitive to conditions such as the composition of Sweet natural gas, temperature, pressure, all meets the requirements than technical indicators such as power consumption, liquefied fractions.
Description of drawings
Fig. 1 is a liquefaction process schema of the present invention.
Fig. 2 is the heat exchange ice chest module diagram of liquefaction process.
Fig. 3 is the heavy hydrocarbon separation module synoptic diagram of liquefaction process.
Fig. 4 is the hydrodynamic force module synoptic diagram of liquefaction process.
Fig. 5 is the product stock module diagram of liquefaction process.
Among the figure, the 1-first heat exchange ice chest, the 2-second heat exchange ice chest, 3-the 3rd heat exchange ice chest, 4-the 4th heat exchange ice chest, the 5-LNG throttling valve, 6-LNG surge tank, 7-LNG storage tank, 8-propane one stage compressor, 9-first water cooler, 10-propane two stage compressor, 11-second water cooler, 12-propane throttling valve, 13-high temperature nitrogen circulation decompressor supercharging blower, 14-cryogenic nitrogen circulation decompressor supercharging blower, 15-the 3rd water cooler, 16-the 4th water cooler, the 17-high temperature nitrogen stage compressor that circulates, the 18-cryogenic nitrogen stage compressor that circulates, 19-the 5th water cooler, 20-the 6th water cooler, 21-high temperature nitrogen circulation compound expansion machine, 22-cryogenic nitrogen circulation compound expansion machine, 23-the 7th water cooler, 24-the 8th water cooler, 25-nitrogen mixing tank, 26-nitrogen splitter, 27-high temperature nitrogen circulation decompressor, 28-cryogenic nitrogen circulation decompressor, 29-first separator, 30-second separator, 31-rectifying tower, the 32-mixer for natural gas in use, 33-heavy hydrocarbon throttling valve, 34-the 9th water cooler, 35-LPG surge tank, the 36-LPG storage tank, 51～59-natural gas stream, the logistics of 60～61-propane, 62～70-nitrogen 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 5.0MPa, temperature is 34.5 ℃, and liquefaction flow path is made up of propane precooling circulation, dinitrogen inflatable refrigeration cycle, natural qi exhaustion heavy hydrocarbon, liquefaction pipeline.
In propane precooling circulation, propane is compressed to 1.6MPa by propane compressor 8,10, all pass through water cooler 9,11 after every grade of compression and be cooled to 35 ℃, propane all liquefies, be depressurized to 0.13MPa through propane throttling valve 12 again, temperature is reduced to-36 ℃, and this moment, propane was gas-liquid two-phase, entered heat exchange ice chest 1 precooling Sweet natural gas and nitrogen gas refrigerant.
In the circulation of nitrogen swell refrigeration, high pressure nitrogen is divided into two strands by nitrogen splitter 26 after heat exchange ice chest 1 is chilled to-33 ℃ in advance, one is directly through 27 expansions of nitrogen expansion machine and to decompressor supercharging blower 13 output shaft works, pressure is reduced to 1.1MPa, temperature is reduced to-122.0 ℃, enter heat exchange ice chest 3,2,1 then successively, be used for cooled natural gas and another strand nitrogen, be compressed to 8.0MPa through decompressor supercharging blower 13 and nitrogen compressor 17,21 successively after the re-heat, all pass through water cooler 15,19,23 after every grade of compression and be cooled to 35 ℃; Another strand nitrogen enters heat exchange ice chest 2 and is chilled to-65 ℃ in advance, enter heat exchange ice chest 3 and be cooled to-85 ℃, again through 28 expansions of nitrogen expansion machine and to decompressor supercharging blower 14 output shaft works, pressure is reduced to 1.4MPa, temperature is reduced to-156 ℃, return heat exchange ice chest 4,3,2,1 temperature successively and rise to 30 ℃, be compressed to 8.0MPa through decompressor supercharging blower 14, nitrogen compressor 18,22 successively then, all pass through water cooler 16,20,24 after every grade of compression and be cooled to 35 ℃, two strands of highly compressed nitrogen enter 1 precooling of heat exchange ice chest after gas mixture 25 mixes.
At natural qi exhaustion heavy hydrocarbon, in the liquefaction pipeline, pretreated natural gas via heat exchange ice chest 1 is pre-chilled to-30 ℃, enter separator 29 then and carry out flash trapping stage, isolated liquid phase is as the middle part charging of rectifying tower 31, isolated gas phase enters heat exchange ice chest 2 and is cooled to-65 ℃, enter separator 30 then and carry out the secondary separation, isolated liquid phase is as its top feed of rectifying tower 31, rectifying tower 31 bottoms are depressurized to 1.0MPa through throttling valve 33, ℃ enter LPG surge tank 35 through water cooler 34 heat exchange to 35 then, isolated gas can be used as fuel and uses, and isolated liquid phase enters LPG storage tank 36, and this LPG product contains more C
5Above component, needing further to handle through land based installation could be as qualified product; Separator 30 isolated gas phases and the top products of rectifying tower 31 enter heat exchange ice chest 3,4 successively and are cooled to-151 ℃ and make it all liquefaction and cold excessively after mixing tank 32 mixes, be cooled to-160 ℃ through throttling valve 5 throttlings again, wherein about 7% liquid gasification, gas-liquid mixture enters LNG surge tank 6, isolated liquid phase enters LNG storage tank 7 and stores, isolated gas phase can be used as the low-temperature receiver that the Sweet natural gas method of cooling is dewatered after abhiseca is discharged, can be used as the resurgent gases on absorption tower in the pretreatment system after the re-heat, enter the use that acts as a fuel or generate electricity of fuel gas pipe network at last.
Fig. 2 is the heat exchange ice chest module diagram of liquefaction process, wherein 51～52,53～54,55～56 be respectively Sweet natural gas as the liquefaction process of thermal source in the heat exchange ice chest, 60～61 is as the process of low-temperature receiver precooling Sweet natural gas and nitrogen gas refrigerant in the heat exchange ice chest after the propane refrigerant throttling, 62～64 for the nitrogen gas refrigerant after the compression as thermal source in the heat exchange ice chest by the process of precooling, 65～66 and 68～69 are the process of the nitrogen gas refrigerant after expanding as low-temperature receiver cooled natural gas and high pressure nitrogen refrigeration agent.This module is made up of four heat exchange ice chests (being encapsulated in an attemperator the inside), two throttling valve and a splitter.
Fig. 3 is the heavy hydrocarbon separation module synoptic diagram of liquefaction process, the 52nd, from the Sweet natural gas of heat exchange ice chest module after 1 precooling of heat exchange ice chest, the 54th, from heat exchange ice chest module through heat exchange ice chest 2 cooled Sweet natural gases, 53 remove the heat exchange ice chest 2 of heat exchange ice chest module, 55 go the heat exchange ice chest 3,58 of heat exchange ice chest module to remove the water cooler 34 of product stock module.This module is made up of two separators, a mixing tank and a rectifying tower.
Fig. 4 is the hydrodynamic force module synoptic diagram of liquefaction process, and wherein 63～68,64～65 is the nitrogen expansion process, and 69～70,66～67 is the nitrogen pressure compression process, and 61～60 is the propane compression process.This module is made up of two decompressors, three compressors, two decompressor supercharging blowers and eight water coolers.
Fig. 5 is the product stock module diagram of liquefaction process, and 56 is the LNG flash steam from the throttling valve 5,58 of heat exchange ice chest module from the throttling valve 33,57 of heavy hydrocarbon separation module, and 59 is the LPG flash steam.This module is made up of two storage tanks, two separators and a water cooler.
Claims (4)
1. process for compact natural gas liquefying and floating production, it is characterized in that by heat exchange ice chest module, the heavy hydrocarbon separation module, four modules of hydrodynamic force module and product stock design, Sweet natural gas by the seabed extraction at first enters pretreatment unit, remove silt wherein, water, sour gas, mercury, enter liquefaction unit behind the impurity such as benzene, liquefaction flow path propane precooling circulation, the circulation of dinitrogen gas swell refrigeration, natural qi exhaustion heavy hydrocarbon, the liquefaction pipeline is formed, it is applicable to the natural gas liquefaction production under the marine floating condition, have and prevent that hull from rocking the performance to the liquefaction process influence, compact construction, it is convenient to start.
2. process for compact natural gas liquefying and floating production according to claim 1 is characterized in that, the refrigeration agent that the precooling circulation is adopted is a propane.
3. process for compact natural gas liquefying and floating production according to claim 1 is characterized in that, what major cycle was adopted is dinitrogen expansion flow process.
4. process for compact natural gas liquefying and floating production according to claim 1 is characterized in that, the used water coolant of water cooler is a seawater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010140435 CN101787314B (en) | 2010-04-01 | 2010-04-01 | Process for compact natural gas liquefying and floating production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010140435 CN101787314B (en) | 2010-04-01 | 2010-04-01 | Process for compact natural gas liquefying and floating production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101787314A true CN101787314A (en) | 2010-07-28 |
| CN101787314B CN101787314B (en) | 2013-04-17 |
Family
ID=42530696
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010140435 Active CN101787314B (en) | 2010-04-01 | 2010-04-01 | Process for compact natural gas liquefying and floating production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101787314B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN103865601A (en) * | 2014-03-13 | 2014-06-18 | 中国石油大学(华东) | Heavy hydrocarbon recovery method of propane precooling and deethanizer top reflux |
| CN104061758A (en) * | 2014-07-01 | 2014-09-24 | 天津市振津工程设计咨询有限公司 | Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation |
| CN104087357A (en) * | 2014-07-16 | 2014-10-08 | 北京安珂罗工程技术有限公司 | Method and system for removing heavy hydrocarbons in natural gas liquefaction process |
| 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 |
| CN105121271A (en) * | 2013-04-12 | 2015-12-02 | 埃克赛勒瑞特液化解决方案公司 | Systems and methods for floating dockside liquefaction of natural gas |
| CN108106325A (en) * | 2018-01-08 | 2018-06-01 | 中国寰球工程有限公司 | Suitable for marine natural gas liquefaction system |
| CN109781449A (en) * | 2019-03-05 | 2019-05-21 | 合肥万豪能源设备有限责任公司 | A kind of natural gas liquefaction device list sled block and whole test device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN101338964A (en) * | 2008-08-14 | 2009-01-07 | 苏州制氧机有限责任公司 | Natural gas liquefaction device and liquefaction flow path |
-
2010
- 2010-04-01 CN CN 201010140435 patent/CN101787314B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN101338964A (en) * | 2008-08-14 | 2009-01-07 | 苏州制氧机有限责任公司 | Natural gas liquefaction device and liquefaction flow path |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101948706B (en) * | 2010-08-18 | 2013-02-27 | 中国海洋石油总公司 | Mixed refrigerant and nitrogen expansion combinational refrigeration type natural gas liquefying method |
| 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 |
| CN105121271A (en) * | 2013-04-12 | 2015-12-02 | 埃克赛勒瑞特液化解决方案公司 | Systems and methods for floating dockside liquefaction of natural gas |
| CN105121271B (en) * | 2013-04-12 | 2018-08-10 | 埃克赛勒瑞特液化解决方案公司 | The liquefied system and method for relocatable code rostral for natural gas |
| US9903647B2 (en) | 2013-04-12 | 2018-02-27 | Excelerate Liquefaction Solutions, Llc | Systems and methods for floating dockside liquefaction of natural gas |
| CN103865601A (en) * | 2014-03-13 | 2014-06-18 | 中国石油大学(华东) | Heavy hydrocarbon recovery method of propane precooling and deethanizer top reflux |
| CN103865601B (en) * | 2014-03-13 | 2015-07-08 | 中国石油大学(华东) | Heavy hydrocarbon recovery method of propane precooling and deethanizer top reflux |
| CN104061758A (en) * | 2014-07-01 | 2014-09-24 | 天津市振津工程设计咨询有限公司 | Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation |
| CN104087357A (en) * | 2014-07-16 | 2014-10-08 | 北京安珂罗工程技术有限公司 | Method and system for removing heavy hydrocarbons in natural gas liquefaction process |
| CN104087357B (en) * | 2014-07-16 | 2018-02-27 | 北京安珂罗工程技术有限公司 | A kind of method and system that heavy hydrocarbon is removed from gas deliquescence process |
| 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 |
| CN108106325A (en) * | 2018-01-08 | 2018-06-01 | 中国寰球工程有限公司 | Suitable for marine natural gas liquefaction system |
| CN108106325B (en) * | 2018-01-08 | 2024-01-19 | 中国寰球工程有限公司 | Natural gas liquefaction system suitable for sea |
| CN109781449A (en) * | 2019-03-05 | 2019-05-21 | 合肥万豪能源设备有限责任公司 | A kind of natural gas liquefaction device list sled block and whole test device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101787314B (en) | 2013-04-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101787314B (en) | Process for compact natural gas liquefying and floating production | |
| Tan et al. | A new boil-off gas re-liquefaction system for LNG carriers based on dual mixed refrigerant cycle | |
| US9003828B2 (en) | Method and system for production of liquid natural gas | |
| CN102093921A (en) | Offshore natural gas liquefying method and device | |
| US20110067439A1 (en) | Method and system for production of liquid natural gas | |
| Bukowski et al. | Natural gas liquefaction technology for floating LNG facilities | |
| CN103865601B (en) | Heavy hydrocarbon recovery method of propane precooling and deethanizer top reflux | |
| CN104833175A (en) | FLNG/FLPG oil gas pretreatment and liquefaction method | |
| CN101406763B (en) | Reliquefaction method for evaporation gas of liquor goods on ship | |
| CN103363778B (en) | Minitype skid-mounted single-level mixed refrigerant natural gas liquefaction system and method thereof | |
| CN106440656B (en) | Carbon dioxide precooling two-stage nitrogen expansion natural gas liquefaction system | |
| CN101915494A (en) | Re-liquefaction method of shipped liquid cargo of ethylene/ethane evaporation gas | |
| CN104930815A (en) | Marine natural gas liquefaction and NGL recycling system and application | |
| CN105737515A (en) | Natural gas liquefaction system and method based on plate heat exchanger and modular mixed refrigerant | |
| CN101392980B (en) | Re-liquefying method for shipping liquefaction ethylene/ethane vaporized gas | |
| CN107620863B (en) | The re-liquefied system of one kind liquefaction hydro carbons BOG peculiar to vessel and technique | |
| CN204739842U (en) | Preliminary treatment of FLNG oil gas and liquefying plant | |
| CN104807287A (en) | Small natural gas liquefaction and refrigeration system and small natural gas liquefaction and refrigeration method | |
| WO2015140197A2 (en) | A method for liquefaction of a pre-processed natural gas | |
| Li et al. | Thermodynamic Analysis‐Based Improvement for the Boil‐off Gas Reliquefaction Process of Liquefied Ethylene Vessels | |
| CN202030720U (en) | Offshore natural gas liquefaction device | |
| CN203310202U (en) | Dual-mixed-refrigerant liquefying system applied to base load type natural gas liquefaction factory | |
| KR20110121134A (en) | Method and apparatus for liquefying natural gas | |
| CN103868322A (en) | Pre-cooling type heavy hydrocarbon recycling system and technology for offshore natural gas extraction | |
| CN102304403B (en) | Method and device for liquefying natural gas by using propylene precooling mixed cryogen |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent for invention or patent application | ||
| CB02 | Change of applicant information |
Address after: 266580 Changjiang Road West, Qingdao Development Zone, Shandong, China, 66 Applicant after: China Petroleum University (East China) Address before: 257061 North Dongying Road, Dongying, Shandong, No. two, No. 271 Applicant before: China Petroleum University (East China) |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: CNOOC RESEARCH INSTITUTE CHINA UNIVERSITY OF PETRO Effective date: 20140918 Owner name: CHINA MARINE PETROLEUM GENERAL CO. Free format text: FORMER OWNER: CHINA UNIVERSITY OF PETROLEUM AST CHINA Effective date: 20140918 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| C53 | Correction of patent for invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Xie Bin Inventor after: Wang Qing Inventor after: Li Yuxing Inventor after: Wang Wuchang Inventor after: Yu Xisui Inventor after: Zhu Jianlu Inventor after: Tang Jianfeng Inventor after: Lin Riyi Inventor after: Liu Yonghao Inventor after: Wang Weiwei Inventor before: Li Yuxing Inventor before: Wang Wuchang Inventor before: Zhu Jianlu Inventor before: Tang Jianfeng Inventor before: Lin Riyi Inventor before: Liu Yonghao Inventor before: Wang Weiwei |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 266580 QINGDAO, SHANDONG PROVINCE TO: 100010 DONGCHENG, BEIJING Free format text: CORRECT: INVENTOR; FROM: LI YUXING WANG WUCHANG ZHU JIANLU TANG JIANFENG LIN RIYI LIU YONGHAO WANG WEIWEI TO: XIE BIN LI YUXING WANG WUCHANG YU XISUI ZHU JIANLU TANG JIANFENG LIN RIYI LIU YONGHAO WANG WEIWEI WANG QING |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20140918 Address after: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Patentee after: China National Offshore Oil Corporation Patentee after: CNOOC Research Institute Patentee after: China Petroleum University (East China) Address before: 266580 Changjiang Road West, Qingdao Development Zone, Shandong, China, 66 Patentee before: China Petroleum University (East China) |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Co-patentee after: CNOOC research institute limited liability company Patentee after: China Offshore Oil Group Co., Ltd. Co-patentee after: China Petroleum University (East China) Address before: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Co-patentee before: CNOOC Research Institute Patentee before: China National Offshore Oil Corporation Co-patentee before: China Petroleum University (East China) |
|
| CP01 | Change in the name or title of a patent holder | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20210803 Address after: 100010 No. 25 North Main Street, Dongcheng District, Beijing, Chaoyangmen Patentee after: CHINA NATIONAL OFFSHORE OIL Corp. Patentee after: CNOOC RESEARCH INSTITUTE Co.,Ltd. Address before: 100010 No. 25 North Main Street, Dongcheng District, Beijing, Chaoyangmen Patentee before: CHINA NATIONAL OFFSHORE OIL Corp. Patentee before: CNOOC RESEARCH INSTITUTE Co.,Ltd. Patentee before: China University of Petroleum (East China) |