CN101975503A - Modified natural gas helium extraction process - Google Patents
Modified natural gas helium extraction process Download PDFInfo
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- CN101975503A CN101975503A CN 201010249718 CN201010249718A CN101975503A CN 101975503 A CN101975503 A CN 101975503A CN 201010249718 CN201010249718 CN 201010249718 CN 201010249718 A CN201010249718 A CN 201010249718A CN 101975503 A CN101975503 A CN 101975503A
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Abstract
The invention relates to a modified natural gas helium extraction process. The process comprises the following steps of: liquefying purified natural gas under a deep cooling condition; distilling and separating at a low temperature to obtain crude helium, wherein the purified natural gas is carbonized by a heat exchanger and enters a rectifying tower to be rectified, and primary crude helium is obtained at the top of the rectifying tower; throttling, exchanging heat and vaporizing liquid at the tower bottom, and then swelling and reheating the liquid to a normal temperature in a swelling machine; and conveying the liquid outwards. Compared with a conventional process, the invention improves the separating pressure and the temperature of the rectifying tower so as to reduce power consumption needed for refrigeration, liquefaction and separation. Meanwhile, along with the decrease of the pressure for conveying outwards natural gas, the invention benefits the improvement of a swelling ratio so as to increase the refrigeration amount, also solves the problem of decreased refrigeration efficiency of the swelling machine of a pre-swelling process because of the with-liquid-property of the swelled swelling machine (the swelling machine of a post-swelling process frees from the with-liquid-property.), accordingly has obvious energy-saving effect and can be popularized and applied.
Description
Technical field
The present invention relates to the chemical separating method and technology, particularly a kind of natural gas of improvement is put forward the technology of helium.
Background technology
From natural gas, extract helium, wide range of industrial applications is separation by deep refrigeration at present, its basic principle is to utilize the helium liquefaction temperature extremely low, the principle that is difficult to liquefy, constantly reduce gas temperature by freezing, with component liquefaction, cryogenic rectifications such as the methane in the natural gas, oxygen, nitrogen, thereby obtain raw helium, raw helium is obtained A level helium (HE concentration is greater than 99.995%) through further making with extra care.The common process step as shown in Figure 1 at present, after the purified treatment such as the natural gas via decarburization after the purification, drying, obtain the natural gas after clean, the dry purification, liquefy by the decompressor expansion after the natural gas process heat exchanger heat exchange after the purification, enter again in the rectifying column and separate, cat head obtains a raw helium, and the liquid at the bottom of the tower is externally carried to normal temperature gasification back through heat exchanger throttling re-heat.Yet, existing technology all has the following disadvantages: 1. the natural gas after purifying is to enter rectifying column more earlier after decompressor expands decompression, advance corresponding the diminishing of stream pressure that rectifying column carries out cryogenic separation this moment, and reduce in order to satisfy the required temperature of separating, must must increase the refrigeration and the work of separation to a certain extent again, just increase energy consumption (mainly being compression power consumption and refrigerating loss) so virtually.2 simultaneously for satisfying the requirement that liquefaction separates, the decompressor band liquid that the back fluid must be to a certain degree that expands., because temperature can not fine adjusting and control before the natural gas after purifying expanded, cold under low temperature dark rank cold and the general cold temperature can not finely be mated, when serious the device natural gas can not be liquefied and ordinary production.3。When outside defeated gas pressure when reducing, the pressure and temp in the rectifying column needs relatively stable, can not increase expansion simultaneously and recently increase refrigerating capacity.
Summary of the invention
At above-mentioned weak point, the object of the present invention is to provide a kind of technology that can rationally utilize low temperature cold and effective natural gas that reduces the tangible improvement of energy consumption for cooling energy-saving effect to carry helium.
In order to achieve the above object, the present invention has adopted following technical scheme: a kind of natural gas of improvement is put forward the technology of helium, be included in the natural gas liquefaction that makes under the deep cooling condition after the purification, the cryogenic rectification separation obtains raw helium, wherein, natural gas after the purification enters rectifying in the rectifying column after liquefying through heat exchanger, and the rectifying column cat head obtains a raw helium; Decompressor expands liquid at the bottom of the tower and re-heat is externally carried behind normal temperature through entering after the heat exchanger throttling heat exchange vaporization again again.
Beneficial effect of the present invention is:
(1) in the existing production technology, natural gas after the purification is to enter rectifying column (being called for short " preceding expansion " technology) earlier after decompressor expands decompression again, production technology of the present invention then is that the natural gas after purifying directly enters rectifying column and carries out cryogenic separation (being called for short " expanding in the back " technology) before the decompression of expanding, " so then expand " advance pressure that rectifying column carries out cryogenic separation " preceding expansion " higher, thereby improved the required temperature of separating, help reducing the refrigeration and the work of separation, simultaneously, the low-pressure tail gas pressure of " expanding in the back " is corresponding also high, then the required merit of pipe network is corresponding just to be reduced with pushing back after the tail gas supercharging, thereby effectively reaches energy-saving effect.
For example, be 2.5Mpa to advance ice chest pressure, going out device pressure is 1.0Mpa, and the pressure that throttling needs is reduced to 0.5Mpa, and then the pressure of preceding expansion rectifying column is 1.5Mpa (condensation temperature of corresponding rectifying tower top is-148 ℃), and expansion ratio is about 2.5/1.5=1.67; The pressure of rectifying column then of then expanding is 2.5Mpa (condensation temperature of corresponding rectifying tower top is-136 ℃), and expansion ratio is about 2.0/1.0=2.
With the existing production technology of HYSYS analog computation and the parameter such as the table 2 of production technology of the present invention, expansion decompressor in back increases refrigerating capacity 15KW as can be seen, the back temperature that expands simultaneously reduces about 5 ℃, and the low-pressure tail gas compression increases the about 82KW of energy efficient because of inlet pressure.
Table 1 has the technological parameter simulation of production technology/production technology of the present invention now and compares
* actual employing reduces the method for advancing rectifying column vaporization branch rate, has further reduced the condensation load of rectifying column, has lowered the low pressure compression power consumption.
(2). operation, operation aspect: operation control is more stable
" preceding expansion " production technology: because the gas field material gas quantity constantly reduces, and Natural gas consumption constantly increases, natural gas supply contradiction becomes increasingly conspicuous, pipe network material pressure fluctuation is bigger, Various Seasonal unstripped gas temperature contrast is also bigger in addition, thereby expands preceding gas flow temperature, pressure transient, causes the cold balancing of device wayward, before expansion process exist to expand before temperature can not fine adjusting and control, the cold under low temperature dark rank cold and the general cold temperature can not finely be mated.Device even can't carry out normal regulating when serious is operated very difficult.
" expanding in the back " production technology: can advance the method for the flow size of decompressor by adjusting, make the preceding temperature that expands adjustable.The operated adjusting function of device is improved.
Because entering the air-flow of decompressor is the air-flow of rectifying column tower bottoms body after the throttling heat exchange, the amount of this air-flow and temperature all can realize stable control through the rectifying column operation, thereby can guarantee the cold balancing of device, make easy and simple to handle, stable.
(3) decompressor operating efficiency refrigerating capacity is big:
Owing to expand to how many no requirement (NR)s that have or not of decompressor outlet band liquid measure in the back, and the general turbo-expander that adopts general decrease in efficiency when after expansion, be with liquid measure to increase, so have the efficient that technology helps improving decompressor now.Because the expansion ratio of " expanding in the back " is higher than " preceding expansion ", corresponding refrigerating capacity increases, referring to table 1 simultaneously.Select for use the highest outer defeated pressure to design during general the design, when defeated pressure reduced outside the reality, the technology after the improvement can expand by increase recently increase refrigerating capacity, and the pressure and temp that common process is stablized rectifying column because of needs then can not.
Description of drawings
Fig. 1 has technological process of production figure now
Fig. 2 process chart of the present invention
The different cryogenic temperatures of Fig. 3 are to the schematic diagram that influences of coefficient of refrigerating performance
The specific embodiment
As shown in Figure 2, the natural gas after the purification enters rectifying in the rectifying column after liquefying through heat exchanger, and the rectifying column cat head obtains a raw helium; Decompressor expands liquid at the bottom of the tower and re-heat is externally carried behind normal temperature through entering after the heat exchanger throttling heat exchange vaporization again again.
One aspect of the present invention mainly is the separating pressure that has improved rectifying column, thereby improved the required temperature of separating, help reducing merit (the needed coefficient of refrigerating performance of refrigeration is seen Fig. 3 under the different temperatures, as can be seen, suitably improves the refrigeration liquefying temperature and can obviously save energy consumption for cooling).On the other hand, help increasing the expansion ratio of decompressor, thereby improve the refrigerating capacity of decompressor, be particularly suitable for going out at present the score of device gas pressure from the low situation of pressure tower.
Claims (1)
1. the natural gas of an improvement is put forward the technology of helium, be included in the natural gas liquefaction that makes under the deep cooling condition after the purification, the cryogenic rectification separation obtains raw helium, it is characterized in that: the natural gas after the purification enters rectifying in the rectifying column after liquefying through heat exchanger, and the rectifying column cat head obtains a raw helium; Decompressor expands liquid at the bottom of the tower and re-heat is externally carried behind normal temperature through entering after the heat exchanger throttling heat exchange vaporization again again.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010249718 CN101975503A (en) | 2010-08-10 | 2010-08-10 | Modified natural gas helium extraction process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010249718 CN101975503A (en) | 2010-08-10 | 2010-08-10 | Modified natural gas helium extraction process |
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| CN101975503A true CN101975503A (en) | 2011-02-16 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102735020A (en) * | 2012-07-23 | 2012-10-17 | 中国石油天然气股份有限公司西南油气田分公司成都天然气化工总厂 | Method for extracting helium from natural gas |
| CN106352657A (en) * | 2016-08-24 | 2017-01-25 | 四川空分设备(集团)有限责任公司 | System and method for extracting helium gas from flashing steam |
| CN111170290A (en) * | 2020-01-07 | 2020-05-19 | 中国科学院高能物理研究所 | Device and process for extracting helium from natural gas |
-
2010
- 2010-08-10 CN CN 201010249718 patent/CN101975503A/en active Pending
Non-Patent Citations (1)
| Title |
|---|
| 《天然气与石油》 20090831 龙增兵，琚宜林，钟志良，蒲远洋 天然气提氦技术探讨与研究 28-31 1 第27卷, 第4期 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102735020A (en) * | 2012-07-23 | 2012-10-17 | 中国石油天然气股份有限公司西南油气田分公司成都天然气化工总厂 | Method for extracting helium from natural gas |
| CN102735020B (en) * | 2012-07-23 | 2013-05-08 | 中国石油天然气股份有限公司西南油气田分公司成都天然气化工总厂 | Method for extracting helium from natural gas |
| CN106352657A (en) * | 2016-08-24 | 2017-01-25 | 四川空分设备(集团)有限责任公司 | System and method for extracting helium gas from flashing steam |
| CN106352657B (en) * | 2016-08-24 | 2019-05-03 | 四川空分设备(集团)有限责任公司 | The system and method for flashed vapour extraction helium |
| CN111170290A (en) * | 2020-01-07 | 2020-05-19 | 中国科学院高能物理研究所 | Device and process for extracting helium from natural gas |
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Application publication date: 20110216 |