CN203625262U - Device for recycling ethane from liquefied natural gas - Google Patents
Device for recycling ethane from liquefied natural gas Download PDFInfo
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- CN203625262U CN203625262U CN201320724938.9U CN201320724938U CN203625262U CN 203625262 U CN203625262 U CN 203625262U CN 201320724938 U CN201320724938 U CN 201320724938U CN 203625262 U CN203625262 U CN 203625262U
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Abstract
The utility model discloses a device for recycling ethane from liquefied natural gas, belonging to the techno field of a technique for recycling the ethane from LNG (Liquefied Natural Gas). An LNG pump is connected with a first distributor; the first distributor is connected with a plate-fin heat exchanger and a demethanizing column; the demethanizing column is connected with a reflux pump and a dethanizing column; the plate-fin heat exchanger is connected with a reflux tank, a first circulator, the demethanizing column and the dethanizing column; the first circulator is connected with the demethanizing column; the reflux tank is connected with the reflux pump; the reflux pump is connected with a second distributor; the second distributor is connected with a second circulator; the second circulator is connected with the dethanizing column, and the dethanizing column is connected with a balancer. The device disclosed by the utility model is simple in structure, and the mass balance and energy balance of the device are realized through heat exchange between material flows of the plate-fin heat exchanger. The separation of methane in the LNG is realized through the demethanizing column, and the separation of ethane in the LNG is realized through the dethanizing column. The purity of the finally recycled ethane is as high as 94%, and the obtained liquefied natural gas also satisfies the national liquefied natural gas standards.
Description
Technical field
The utility model relates to one and from natural gas liquids, reclaims ethane device, belongs to LNG(natural gas liquids) recovery ethane Technology field.
Background technology
Along with China's Petrochemical Market continues swift and violent development, also more and more higher to the requirement of petrochemical industry basic material, raw material sources become the key of restriction Ethylene Industry development.At present, China's ethylene raw is mainly from petroleum naphtha, and petroleum naphtha is all from oil, oil price is high in recent years, not only improved production cost of ethylene, and raw materials cost also accounts for 60%～80% of production cost of ethylene, compressed the profit margin of ethene.Therefore, searching ethylene raw is just very necessary.
Summary of the invention
In order to overcome the deficiencies in the prior art, the utility model provides a kind of ethane device that reclaims from natural gas liquids.
The purpose of this utility model is to adopt LNG as raw materials recovery ethane, and a kind of method that reclaims ethane is provided.From LNG, reclaim ethane, propane, butane as ethylene raw, not only yield of ethene is high, and can save a large amount of preciousnesses and oil fuel in short supply, and can effectively alleviate the imbalance between supply and demand of market oil product.
A kind of device that reclaims ethane from natural gas liquids, LNG pump connects the first divider, the first divider web plate fin heat exchanger, demethanizing tower, demethanizing tower connects reflux pump, deethanizing column, fin heat exchanger connects return tank, the first circulator, demethanizing tower, deethanizing column, the first circulator connects demethanizing tower, and return tank connects reflux pump, and reflux pump connects the second divider; The second divider connects the second circulator; The second circulator connects deethanizing column, ethane tower connection balancer.
Static organ output liquefied gas; LNG enters LNG pump; The second divider output ethane; Fin heat exchanger output methane.
From natural gas liquids, reclaim a method for ethane, at least comprise LNG pump, divider, demethanizing tower, deethanizing column, ice chest, return tank, reflux pump composition; By after LNG supercharging, a part is as cryogen, and another part enters demethanizing tower, deviates from medium methane after rectifying, and at the bottom of tower, liquid enters deethanizing column, and after rectifying, overhead ethane is qualified rear outer defeated as product, and at the bottom of tower, liquid is liquefied gas.
Contain following steps;
LNG(temperature-162 ℃, pressure 0.12MPa) after the supercharging of LNG pump, be pressurized to 4.5MPa, then be divided into two bursts of logistics through the first divider, wherein the second logistics accounts for 61% of total flux; The 3rd logistics accounts for 39% of total flux; The second logistics enters the top of demethanizing tower 6 by pipeline; By the pressure-controlling of demethanizing tower, at 3.6～3.62MPa, to guarantee that most of methane deviates from, at the bottom of demethanizer, methane content is controlled at 1% left and right; Reboiler temperature is controlled at 50.6 ℃, and rectifying at this temperature, and the 6th logistics (50.6 ℃ of temperature, pressure 3.62MPa) out at the bottom of demethanizer, continues transported to deethanizing column by pipeline; Deethanizing column pressure-controlling is at 2.97～3.0MPa, and for guaranteeing that most of ethane deviates from, at the bottom of deethanizing column tower, ethane content is controlled at 1% left and right; In deethanizing column tower, reboiler Temperature Setting is at 92.1 ℃, at this temperature, in tower, carry out secondary rectifying, liquefied gas (92.11 ℃ of temperature out at the bottom of deethanizing column tower, pressure 3.0MPa) through static organ test: at 37.8 ℃, the saturation vapour pressure of deethanizing column liquefied gas is 1023kPa, and the vapour pressure of the refinery's liquefied petroleum gas (LPG) that meets defined in GB11174-89 at 37.8 ℃ is not more than 1380kPa; Deethanizer overhead the 7th logistics (12.56 ℃ of temperature, pressure 2.97MPa) ethane content out reaches 94%, and recovering effect is good;
Another gang of LNG the 3rd logistics (temperature-159.9 ℃ that branch away from the first divider, pressure 4.5MPa), heated through plate-fin heat exchanger, the 14 logistics (temperature-55 ℃, pressure 4.49MPa) enter the first circulator circulation, the 14 logistics enters demethanizing tower;
Demethanizer column overhead methane out the 5th thing (temperature-84.36 ℃, pressure 3.6MPa), methane content is 0.99%, the basic satisfied requirement of controlling; Heated through plate-fin heat exchanger again, it is outer defeated as fuel gas that logistics methane (7.4 ℃ of temperature, pressure 3.59MPa) is transported to downstream;
Deethanizing column ethane out, the 7th logistics (12.6 ℃ of temperature, pressure 2.97MPa) be cooled through plate-fin heat exchanger, the 8th thing (temperature-18 ℃, pressure 2.96MPa) enter return tank, after in return tank tank, buffering separates, the tenth logistics is pressurized to 3.2MPa through reflux pump, enters the second divider and carries out secondary distribution; Distribute rear portion ethane to enter the second circulator and play circulation, again be driven into deethanizing column and carry out secondary rectifying, the object of setting up this circulation is to carry out rectifying repeatedly by constantly allowing the ethane that contains other composition constantly enter deethanizing column, finally improves ethane purity; Another part ethane is outer defeated as product, and analog calculation moderate purity can reach 94% left and right.
The utility model is simple in structure, by analyzing the each component in LNG, has proposed a kind of processing method and process unit that reclaims ethane from LNG.The method can be by utilizing the low temperature of LNG itself, and mass balance and the energy balance of this device are provided by the heat exchange between the each logistics of plate-fin heat exchanger.Realize the separation of methane in LNG by demethanizing tower; Can realize the separation of ethane in LNG by deethanizing column.The final ethane purity to 94% reclaiming; Liquefied gas out also meets the standard of China's liquefied gas.This device is applicable to the LNG peak regulation station of each department, and the methane of producing and liquefied gas can meet the daily gas requirement of downstream user, and the ethane of producing can meet the demand to ethene in national economy production.All devices, pipeline and valve process pipeline can be realized the installation of sledge dressization, digital management, real time remote control simultaneously; In addition, the required thermal load of demethanizing tower is that 50 ℃ of left and right, the required thermal load of deethanizing column are 90 ℃ of left and right, can adopt Boiler Steam or heat-conducting oil heating nearby, easily handled easily.
Accompanying drawing explanation
When considered in conjunction with the accompanying drawings, by the detailed description with reference to below, can more completely understand better the utility model and easily learn wherein many advantages of following, but accompanying drawing described herein is used to provide further understanding of the present utility model, form a part of the present utility model, schematic description and description of the present utility model is used for explaining the utility model, does not form to improper restriction of the present utility model, wherein:
Fig. 1 is enforcement structural representation of the present utility model.
Below in conjunction with drawings and Examples, the utility model is further illustrated.
Embodiment
Obviously the many modifications and variations that, those skilled in the art do based on aim of the present utility model belong to protection domain of the present utility model.
Embodiment 1: as shown in Figure 1, a kind of device that reclaims ethane with LNG, LNG pump 2 connects the first divider 3, the first divider 3 web plate fin heat exchangers 4, demethanizing tower 6, demethanizing tower 6 connects reflux pump 13, deethanizing column 7, and fin heat exchanger 4 connects return tank 14, the first circulator 5, demethanizing tower 6, deethanizing column 7, the first circulators 5 and connects demethanizing tower 6, return tank 14 connects reflux pump 13, and reflux pump 13 connects the second divider 12; The second divider 12 connects the second circulator 10; The second circulator 10 connects deethanizing column 7, ethane tower 7 connection balancers 8.
Static organ 8 is exported liquefied gas 9; LNG1 enters LNG pump 2; The second divider 12 is exported ethane 11; Fin heat exchanger 4 is exported methane 15.
Embodiment 2: as shown in Figure 1, a kind of method that reclaims ethane from natural gas liquids, contains following steps;
At least comprise LNG pump, divider, demethanizing tower, deethanizing column, ice chest, return tank, reflux pump composition; By after LNG supercharging, a part is as cryogen, another part enters demethanizing tower, after rectifying, deviate from medium methane, at the bottom of tower, liquid enters deethanizing column, and after rectifying, overhead ethane is qualified rear outer defeated as product, at the bottom of tower, liquid is liquefied gas, meets the quality index of China's refinery's liquefied petroleum gas (LPG).
Be divided into two bursts of logistics through the first divider 3, wherein the second logistics 22 accounts for 61% of total flux; The 3rd logistics 23 accounts for 39% of total flux; The second logistics 22 enters the top of demethanizing tower 6 by pipeline; By the pressure-controlling of demethanizing tower 6, at 3.6～3.62MPa, to guarantee that most of methane deviates from, at the bottom of demethanizing tower 6 towers, methane content is controlled at 1% left and right; Reboiler temperature is controlled at 50.6 ℃, and rectifying at this temperature, 50.6 ℃ of the 6th logistics 26(temperature out at the bottom of demethanizing tower 6 towers, pressure 3.62MPa), continue transported to deethanizing column 7 by pipeline; Deethanizing column 7 pressure-controlling are at 2.97～3.0MPa, and for guaranteeing that most of ethane deviates from, at the bottom of deethanizing column 7 towers, ethane content is controlled at 1% left and right; In deethanizing column 7 towers, reboiler Temperature Setting is at 92.1 ℃, at this temperature, in tower, carry out secondary rectifying, liquefied gas (92.11 ℃ of temperature out at the bottom of deethanizing column 7 towers, pressure 3.0MPa) through static organ test: at 37.8 ℃, the saturation vapour pressure of deethanizing column liquefied gas is 1023kPa, and the vapour pressure of the refinery's liquefied petroleum gas (LPG) that meets defined in GB11174-89 at 37.8 ℃ is not more than 1380kPa; 12.56 ℃ of deethanizing column 7 tower tops the 7th logistics 27(temperature out, pressure 2.97MPa) ethane content reaches 94%, and recovering effect is good;
Another gang of LNG the 3rd logistics 23(temperature-159.9 ℃ that branch away from the first divider 3, pressure 4.5MPa), heated through plate-fin heat exchanger, the 14 logistics 24(temperature-55 ℃, pressure 4.49MPa) enter the first circulator 5 and circulate, the 14 logistics 34 enters demethanizing tower 6;
Demethanizing tower 6 tower tops methane the 5th logistics 25(temperature-84.36 ℃ out, pressure 3.6MPa), methane content is 0.99%, the basic satisfied requirement of controlling; Heated through plate-fin heat exchanger 4 again, it is outer defeated as fuel gas that logistics methane (7.4 ℃ of temperature, pressure 3.59MPa) is transported to downstream;
Table-1 is LNG composition table.
Table-1
As mentioned above, embodiment of the present utility model is explained, but as long as not departing from fact inventive point of the present utility model and effect can have a lot of distortion, this will be readily apparent to persons skilled in the art.Therefore, within such variation is also all included in protection domain of the present utility model.
Claims (1)
1. one kind is reclaimed the device of ethane from natural gas liquids, it is characterized in that LNG pump connects the first divider, the first divider web plate fin heat exchanger, demethanizing tower, demethanizing tower connects reflux pump, deethanizing column, fin heat exchanger connects return tank, the first circulator, demethanizing tower, deethanizing column, the first circulator connects demethanizing tower, and return tank connects reflux pump, and reflux pump connects the second divider; The second divider connects the second circulator; The second circulator connects deethanizing column, ethane tower connection balancer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320724938.9U CN203625262U (en) | 2013-11-15 | 2013-11-15 | Device for recycling ethane from liquefied natural gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320724938.9U CN203625262U (en) | 2013-11-15 | 2013-11-15 | Device for recycling ethane from liquefied natural gas |
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| CN203625262U true CN203625262U (en) | 2014-06-04 |
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| CN201320724938.9U Expired - Fee Related CN203625262U (en) | 2013-11-15 | 2013-11-15 | Device for recycling ethane from liquefied natural gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104140349A (en) * | 2014-07-16 | 2014-11-12 | 西安石油大学 | Novel light hydrocarbon separation system and method for LNG |
| CN104628505A (en) * | 2013-11-15 | 2015-05-20 | 中国石油天然气股份有限公司 | Method and device for recovering ethane from liquefied natural gas (LNG) |
| CN110118468A (en) * | 2019-05-10 | 2019-08-13 | 西南石油大学 | A kind of band is suitable for the ethane recovery methods of rich gas from SAPMAC method |
-
2013
- 2013-11-15 CN CN201320724938.9U patent/CN203625262U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104628505A (en) * | 2013-11-15 | 2015-05-20 | 中国石油天然气股份有限公司 | Method and device for recovering ethane from liquefied natural gas (LNG) |
| CN104628505B (en) * | 2013-11-15 | 2016-09-07 | 中国石油天然气股份有限公司 | A kind of method and device reclaiming ethane from liquefied natural gas |
| CN104140349A (en) * | 2014-07-16 | 2014-11-12 | 西安石油大学 | Novel light hydrocarbon separation system and method for LNG |
| CN104140349B (en) * | 2014-07-16 | 2015-12-02 | 西安石油大学 | A kind of lighter hydrocarbons tripping device of natural gas liquids and method |
| CN110118468A (en) * | 2019-05-10 | 2019-08-13 | 西南石油大学 | A kind of band is suitable for the ethane recovery methods of rich gas from SAPMAC method |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140604 Termination date: 20211115 |
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| CF01 | Termination of patent right due to non-payment of annual fee |