JPH0413630B2 - - Google Patents
Info
- Publication number
- JPH0413630B2 JPH0413630B2 JP63204965A JP20496588A JPH0413630B2 JP H0413630 B2 JPH0413630 B2 JP H0413630B2 JP 63204965 A JP63204965 A JP 63204965A JP 20496588 A JP20496588 A JP 20496588A JP H0413630 B2 JPH0413630 B2 JP H0413630B2
- Authority
- JP
- Japan
- Prior art keywords
- pressure
- raw material
- column
- nitrogen
- liquid
- 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.)
- Expired - Lifetime
Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 105
- 229910052757 nitrogen Inorganic materials 0.000 description 46
- 239000007788 liquid Substances 0.000 description 30
- 239000002994 raw material Substances 0.000 description 29
- 238000001179 sorption measurement Methods 0.000 description 17
- 239000003949 liquefied natural gas Substances 0.000 description 15
- 238000004519 manufacturing process Methods 0.000 description 14
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 13
- 229910001873 dinitrogen Inorganic materials 0.000 description 13
- 230000006835 compression Effects 0.000 description 9
- 238000007906 compression Methods 0.000 description 9
- 238000010992 reflux Methods 0.000 description 9
- 238000000926 separation method Methods 0.000 description 9
- 239000003507 refrigerant Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 241001125929 Trisopterus luscus Species 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- F25J3/0426—The cryogenic component does not participate in the fractionation
- F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
- F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Drying Of Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は原料空気から液体窒素および液体酸素
を製造するための空気分離装置に関するものであ
る。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to an air separation apparatus for producing liquid nitrogen and liquid oxygen from raw air.
従来の空気分離装置の構成と作用を第２図によ
つて説明する。
The structure and operation of a conventional air separation device will be explained with reference to FIG.
原料空気濾過器１で濾過された原料空気は、原
料圧縮機２により吸着塔３での吸着操作を行なう
のに必要な圧力（通常は５Kg／cm2ｇ、以下、この
例で説明する）まで加圧され、吸着塔３で水分お
よび炭酸ガス等の不要成分を除去された後、コー
ルドボツクスＣに入る。４は予冷器、５は再生ガ
ス加熱器である。 The raw air filtered by the raw air filter 1 is compressed by the raw material compressor 2 to the pressure required for adsorption operation in the adsorption tower 3 (usually 5 kg/cm 2 g, which will be explained below using this example). After being pressurized and removing unnecessary components such as water and carbon dioxide in the adsorption tower 3, it enters a cold box C. 4 is a precooler, and 5 is a regeneration gas heater.
コールドボツクスＣは、主熱交換器６、精留塔
７、循環窒素熱交換器８、フラツシユボトル（減
圧器）９から成つている。また、精留塔７は、原
料空気圧力（５Kg／cm2ｇ）で操作される高圧塔７
１と、これよりも低圧（通常は0.2〜0.5Kg／cm2
ｇ）で操作される低圧塔７２とから成つている。 Cold box C consists of a main heat exchanger 6, a rectification column 7, a circulating nitrogen heat exchanger 8, and a flash bottle (pressure reducer) 9. In addition, the rectification column 7 is a high pressure column 7 operated at feed air pressure (5 kg/cm 2 g).
1 and lower pressure (usually 0.2 to 0.5Kg/cm 2
g) and a low pressure column 72 operated in
吸着塔３から出た原料空気は、主熱交換器６に
より沸点近くまで冷却された後、精留塔７の高圧
塔７１に入り、同塔内を上昇する間に還流液体窒
素との接触により次第に窒素濃度を高め、頂部で
は高純度窒素ガスとなる。この窒素ガスは低圧塔
底部の液体酸素との熱交換により凝縮して液体窒
素となり、その一部は低圧塔還流液として低圧塔
頂部に、また一部は高圧塔還流液として高圧塔頂
部にそれぞれ供給され、残りは製品液体窒素とし
て液体窒素タンク１０に抜き出される。 The feed air coming out of the adsorption tower 3 is cooled to near its boiling point by the main heat exchanger 6, then enters the high pressure tower 71 of the rectification tower 7, and while rising in the tower, it is reduced by contact with refluxing liquid nitrogen. The nitrogen concentration gradually increases and becomes high purity nitrogen gas at the top. This nitrogen gas condenses into liquid nitrogen through heat exchange with liquid oxygen at the bottom of the low-pressure column, and part of it is sent to the top of the low-pressure column as a reflux liquid in the low-pressure column, and part of it is sent to the top of the high-pressure column as a reflux liquid in the high-pressure column. The remainder is extracted into the liquid nitrogen tank 10 as product liquid nitrogen.
上記高圧塔還流液は、高圧塔７１内を下つてい
く間に空気と接触して酸素濃度を高めつつ塔底か
ら酸素35〜40％を含む液体空気となつて抜き出さ
れ、低圧塔中間部に供給される。 The above-mentioned high pressure column reflux liquid comes into contact with air while descending in the high pressure column 71, increasing the oxygen concentration, and is extracted from the bottom of the column as liquid air containing 35 to 40% oxygen, and is extracted from the middle of the low pressure column. is supplied to
この液体空気は、低圧塔７２内を下降する間に
酸素濃度を増し、同塔底部から高純度液体酸素が
液体酸素タンク１１に抽出され、同塔頂部から高
純度窒素が抜き出される。また、低圧塔上部から
は低純度窒素ガスが抜き出され主熱交換器６によ
り加熱された後、再生ガスとして吸着塔３に入
る。 This liquid air increases its oxygen concentration while descending within the low-pressure column 72, and high-purity liquid oxygen is extracted from the bottom of the column into the liquid oxygen tank 11, and high-purity nitrogen is extracted from the top of the column. Furthermore, low-purity nitrogen gas is extracted from the upper part of the low-pressure column, heated by the main heat exchanger 6, and then enters the adsorption column 3 as regeneration gas.
上記高純度低圧窒素ガスは、一部が主熱交換器
６により、残りが循環窒素熱交換器８によりそれ
ぞれ加熱された後、循環窒素予冷器１２を経て循
環窒素圧縮機１３により加圧される。この加圧さ
れた窒素ガスは、液化天然ガス熱交換器（以下、
LNG熱交換器という）１４で冷却されて液化し、
循環窒素熱交換器８の低温部に入る。同熱交換器
８を出た液体窒素は、フラツシユボトル９により
高圧塔７１の圧力まで減圧され、一部はガス化し
て熱交換器８経由で循環窒素圧縮機１３に戻り、
残りは高圧塔頂部に還流液として供給される。 A portion of the high-purity low-pressure nitrogen gas is heated by the main heat exchanger 6 and the rest by the circulating nitrogen heat exchanger 8, and then passes through the circulating nitrogen precooler 12 and is pressurized by the circulating nitrogen compressor 13. . This pressurized nitrogen gas is transferred to a liquefied natural gas heat exchanger (hereinafter referred to as
LNG is cooled and liquefied in the LNG heat exchanger (14),
It enters the low temperature section of the circulating nitrogen heat exchanger 8. The liquid nitrogen exiting the heat exchanger 8 is reduced in pressure to the pressure of the high pressure column 71 by the flash bottle 9, and a portion is gasified and returned to the circulating nitrogen compressor 13 via the heat exchanger 8.
The remainder is fed to the top of the high pressure column as a reflux liquid.
上記LNG熱交換器１４には、高圧低温（通常
は40Kg／cm2ｇ、−150℃）の液化天然ガス（以下、
LNGという）が寒冷源として供給され、この
LNGにより上記循環窒素圧縮機１３から出た高
圧窒素、および循環窒素予冷器１２に寒冷を与え
る循環冷媒（通常はフロン）が冷却される。 The LNG heat exchanger 14 is equipped with high-pressure, low-temperature (usually 40 kg/cm 2 g, -150°C) liquefied natural gas (hereinafter referred to as
LNG) is supplied as a cooling source, and this
The high-pressure nitrogen discharged from the circulating nitrogen compressor 13 and the circulating refrigerant (usually fluorocarbon) that cools the circulating nitrogen precooler 12 are cooled by the LNG.
また、循環窒素圧縮機１３は、低圧塔頂部から
出た低圧（0.2Kg／cm2ｇ）の窒素ガスを高圧塔７
１の操作圧力（５Kg／cm2ｇ）まで加圧する低圧段
圧縮機１３ａと、この低圧段圧縮機１３ａから出
た窒素ガスを液化させるのに必要な圧力でかつ
LNG圧力（40Kg／cm2ｇ）よりも高い圧力（通常
は60Kg／cm2ｇ）に加圧する高圧段圧縮機１３ｂと
によつて構成される。 In addition, the circulating nitrogen compressor 13 supplies low pressure (0.2 kg/cm 2 g) nitrogen gas from the top of the low pressure column to the high pressure column 7.
The low-pressure stage compressor 13a pressurizes to the operating pressure of 1 (5 kg/cm 2 g), and the nitrogen gas discharged from this low-pressure stage compressor 13a is compressed at the pressure necessary to liquefy the nitrogen gas.
It is constituted by a high-pressure stage compressor 13b that pressurizes to a higher pressure (usually 60 Kg/cm 2 g) than the LNG pressure (40 Kg/cm 2 g).
なお、１５は冷媒ポンプ、１６はLNG加温器
である。 Note that 15 is a refrigerant pump, and 16 is an LNG warmer.
このような空気分離装置において、液体窒素の
生産量は、一般的には、液体酸素生産量の１〜
1.5倍であるが、近年、液体窒素の需要の伸びに
伴い、液体窒素の生産量を液体酸素の３倍以上ま
で増加させる必要性が生じている。
In such air separation equipment, the production amount of liquid nitrogen is generally 1 to 1 times the production amount of liquid oxygen.
However, in recent years, with the growth in demand for liquid nitrogen, it has become necessary to increase the production volume of liquid nitrogen to more than three times that of liquid oxygen.
ところが、従来装置によると、液体窒素の生産
量の増加によつて圧縮機の総動力が増加するとい
う問題が生じていた。 However, with the conventional apparatus, a problem has arisen in that the total power of the compressor increases as the production amount of liquid nitrogen increases.
すなわち、圧縮機の動力は、流量と圧縮比とに
よつて決定される。このうち、圧縮比は、原料圧
縮機２については、常圧から５Kg／cm2ｇまで、循
環圧縮機１３では高圧塔圧力（５Kg／cm2ｇ）また
は低圧塔圧力（0.2Kg／cm2ｇ）から60Kg／cm2ｇま
でと、循環圧縮機側で格段に大きい。一方、液体
窒素の生産量が液体酸素生産量の1.2倍末満では、
循環窒素圧縮機１３の流量（以下、循環窒素流量
という）は原料圧縮機２の流量（以下、原料流量
という）に対して同等かそれ以下であるが、液体
窒素生産量が液体酸素生産量の1.2倍以上になる
と、逆に循環窒素流量が原料流量よりも多くな
る。 That is, the power of the compressor is determined by the flow rate and compression ratio. Among these, the compression ratio is from normal pressure to 5Kg/cm 2 g for the raw material compressor 2, and from high pressure column pressure (5Kg/cm 2 g) or low pressure column pressure (0.2Kg/cm 2 g) for the circulation compressor 13. ) to 60Kg/cm 2 g, which is much larger on the circulation compressor side. On the other hand, when the production amount of liquid nitrogen is less than 1.2 times the production amount of liquid oxygen,
The flow rate of the circulating nitrogen compressor 13 (hereinafter referred to as the circulating nitrogen flow rate) is equal to or lower than the flow rate of the raw material compressor 2 (hereinafter referred to as the raw material flow rate), but the liquid nitrogen production volume is lower than the liquid oxygen production volume. When it becomes 1.2 times or more, the circulating nitrogen flow rate becomes larger than the raw material flow rate.
従つて、従来装置によると、圧縮比の高い循環
圧縮機１３の流量が増加することにより、圧縮機
総動力が増加して動力コストを押上げ、これによ
り製品製造原価が高騰することとなつていた。 Therefore, according to the conventional device, as the flow rate of the circulation compressor 13 with a high compression ratio increases, the total power of the compressor increases, pushing up the power cost, which causes a rise in product manufacturing costs. Ta.
そこで本発明は、循環窒素流量が原料流量より
も多い場合に、圧縮機総動力を節減することがで
きる空気分離装置を提供するものである。 Therefore, the present invention provides an air separation device that can reduce the total compressor power when the circulating nitrogen flow rate is greater than the raw material flow rate.
本発明は、原料空気中から水分等の不要部分を
吸着除去する吸着塔を備えた原料供給ラインと、
この原料供給ラインから供給される原料空気を液
体空気と窒素とに分離する高圧塔および上記液体
空気を液体酸素と窒素とに分離する低圧塔から成
る精留塔と、この精留塔の高圧塔から出た高圧窒
素を加圧しかつ液化天然ガスを寒冷源とする冷媒
との熱交換により冷却し液化させて上記高圧塔に
還流液として送り込む高圧液体窒素還流ライン
と、精留塔の低圧塔頂部から出た低圧窒素を加圧
して低圧塔底部に送り込み液体酸素との熱交換に
よつて液化させる低圧窒素液化ラインとを具備
し、上記原料供給ラインに、上記吸着塔の入口側
において原料空気を吸着塔での吸着操作に必要な
圧力まで加圧する一次原料圧縮機と、吸着塔から
出た原料空気をさらに精留塔の高圧塔での精留操
作を行ないうる限度内において加圧して高圧塔に
送り込む二次原料圧縮機とが設けられてなるもの
である。
The present invention provides a raw material supply line equipped with an adsorption tower that adsorbs and removes unnecessary parts such as moisture from raw material air;
A rectification column consisting of a high-pressure column that separates the raw material air supplied from this raw material supply line into liquid air and nitrogen, and a low-pressure column that separates the liquid air into liquid oxygen and nitrogen, and a high-pressure column of this rectification column. A high-pressure liquid nitrogen reflux line that pressurizes the high-pressure nitrogen released from the liquefied natural gas and cools it through heat exchange with a refrigerant that uses liquefied natural gas as a cooling source, liquefies it and sends it to the high-pressure column as a reflux liquid, and a low-pressure column top of the rectification column. and a low-pressure nitrogen liquefaction line that pressurizes the low-pressure nitrogen coming out of the tower and sends it to the bottom of the low-pressure tower where it is liquefied by heat exchange with liquid oxygen. A primary raw material compressor pressurizes the raw material air to the pressure required for adsorption operation in the adsorption tower, and a high-pressure tower that further pressurizes the raw material air coming out of the adsorption tower within the limit that allows rectification operation in the high-pressure tower of the rectification tower. A secondary raw material compressor is provided.
このように、流量の少ない原料供給側での圧縮
比を高くし、大流量の循環窒素の圧縮比を低くす
ることにより、圧縮機総動力を小さく抑えること
ができる。
In this way, by increasing the compression ratio on the raw material supply side where the flow rate is low and by lowering the compression ratio for the circulating nitrogen where the flow rate is large, the total power of the compressor can be kept low.
本発明の実施例を第１図によつて説明する。 An embodiment of the present invention will be explained with reference to FIG.
第１図において、従来装置を示す第２図と同一
部分には同一符号を付して示している。 In FIG. 1, the same parts as in FIG. 2, which shows a conventional device, are designated by the same reference numerals.
従来装置との相違点のみを説明すると、この実
施例装置においては、原料濾過器１を出た原料空
気を、一次原料圧縮機２１により、従来装置の原
料圧縮機２と同様、吸着塔３での吸着操作を行な
うのに必要な圧力（５Kg／cm2ｇ）まで加圧すると
ともに、吸着塔３から出た原料空気を、二次圧縮
機２２により、精留塔７の高圧塔７１で精留操作
を行ないうる限度圧力内でさらに加圧（たとえば
10Kg／cm2ｇ、以下、この例で説明する）するよう
にしている。従つて、この装置の場合、高圧塔７
１の操作圧力はこの二次原料圧縮機２２の吐出圧
と同じ10Kg／cm2ｇとなる。 To explain only the differences from the conventional device, in this embodiment device, the raw material air coming out of the raw material filter 1 is passed through the adsorption tower 3 by the primary raw material compressor 21, similar to the raw material compressor 2 of the conventional device. At the same time, the raw air coming out of the adsorption tower 3 is rectified in the high pressure column 71 of the rectification column 7 using the secondary compressor 22. Further pressurization (for example,
10Kg/cm 2 g (explained below using this example). Therefore, in the case of this device, the high pressure column 7
The operating pressure of No. 1 is 10 kg/cm 2 g, which is the same as the discharge pressure of this secondary raw material compressor 22.
２３，２４は二次原料圧縮機２２の入口および
出口で原料空気を予冷する原料予冷器で、LNG
熱交換器１４で冷却された冷媒が寒冷として与え
られる。 23 and 24 are raw material precoolers that pre-cool the raw material air at the inlet and outlet of the secondary raw material compressor 22;
The refrigerant cooled by the heat exchanger 14 is provided as cold air.
精留塔７においては、高圧塔７１での分離操作
によつて高圧窒素ガスが高圧塔上部から、また低
圧塔での分離操作によつて低圧窒素ガスが低圧塔
頂部からそれぞれ抜き出される。 In the rectification column 7, high-pressure nitrogen gas is extracted from the upper part of the high-pressure column through a separation operation in the high-pressure column 71, and low-pressure nitrogen gas is extracted from the top of the low-pressure column through a separation operation in the low-pressure column.
このうち、低圧窒素ガスは、低圧段圧縮機２５
により加圧された後、第１および第２熱交換器２
６，２７を経て低圧塔底部に入り、ここで液体酸
素との熱交換作用によつて液化した後、一部が低
圧塔還流液として低圧塔頂部に送られ、残りが製
品液体窒素として液体窒素タンク１０に抜き出さ
れる。ここで、低圧段圧縮機２５では低圧塔頂部
から出た0.2Kg／cm2ｇの低圧窒素ガスを、上記低
圧塔底部での熱交換によつて液化させるのに必要
な圧力（たとえば５Kg／cm2ｇ）まで加圧する。 Among these, the low pressure nitrogen gas is supplied to the low pressure stage compressor 25.
After being pressurized by the first and second heat exchangers 2
6, 27 and enters the bottom of the low-pressure column, where it is liquefied by heat exchange with liquid oxygen. A portion of the liquid is sent to the top of the low-pressure column as the reflux liquid of the low-pressure column, and the rest is liquid nitrogen as product liquid nitrogen. It is extracted into the tank 10. Here, in the low pressure stage compressor 25, the pressure (for example, 5 kg/cm 2 Pressurize to 2 g).
一方、高圧塔上部から出た高圧窒素ガスは、高
圧段圧縮機２８により加圧され、次いでLNG熱
交換器１４により冷却され液化した後、第２熱交
換器２７を経てフラツシユボトル９で減圧され、
高圧塔上部に高圧塔還流液として送られる。ここ
で、高圧段圧縮機２８では、高圧塔上部から出た
10Kg／cm2ｇの窒素ガスを、LNG熱交換器１４で
液化させるのに必要な圧力でかつLNG圧力より
も高い圧力（従来同様、通常60Kg／cm2ｇ）まで加
圧する。 On the other hand, the high-pressure nitrogen gas discharged from the upper part of the high-pressure column is pressurized by the high-pressure stage compressor 28, then cooled and liquefied by the LNG heat exchanger 14, and then passed through the second heat exchanger 27 and depressurized by the flash bottle 9. is,
It is sent to the upper part of the high pressure column as high pressure column reflux liquid. Here, in the high pressure stage compressor 28, the
10 kg/cm 2 g of nitrogen gas is pressurized to a pressure necessary for liquefying it in the LNG heat exchanger 14 and higher than the LNG pressure (usually 60 kg/cm 2 g as in the conventional case).
このように、流量の少ない原料空気を、従来装
置においては原料圧縮機２によつて高圧塔７１上
部の窒素を低圧塔７２底部の液体酸素で凝縮させ
るために必要な圧力で、かつ吸着塔３での吸着操
作に必要な圧力である５Kg／cm2ｇまでしか加圧し
なかつたのに対し、この装置においては一次およ
び二次両圧縮機２１，２２によつて常圧から高圧
塔７１での分離操作を行ないうる限度圧力（約30
Kg／cm2ｇ）内の圧力である10Kg／cm2ｇまで加圧
し、その分、流量の多い循環窒素の圧縮比、すな
わち高圧段圧縮機２８の圧縮比を小さくしたか
ら、圧縮機総動力を低減することができる。 In this way, in the conventional apparatus, feed air having a small flow rate is compressed by the feed compressor 2 at the pressure necessary to condense the nitrogen at the top of the high pressure column 71 with the liquid oxygen at the bottom of the low pressure column 72, and at the pressure necessary for condensing the feed air at the bottom of the low pressure column 72. In contrast, in this device, both the primary and secondary compressors 21 and 22 are used to increase the pressure from normal pressure to the high pressure column 71, which is the pressure required for adsorption operation in the high pressure column 71. The maximum pressure that can be used for separation operations (approximately 30
Kg/cm 2 g), and the compression ratio of circulating nitrogen with a large flow rate , that is, the compression ratio of the high-pressure stage compressor 28, was reduced by that amount, so the total compressor power was reduced. can be reduced.
この点を詳述すると、液体窒素の生産量がたと
えば液体酸素生産量の３倍になつた場合には、高
圧段圧縮機２８の窒素流量は原料空気流量の役
1.8倍となる。この条件で従来装置と本装置の圧
縮機総動力を比較すると、等温圧縮機の場合、そ
の動力Ｗは、
Ｗ＝aFln（Pout／Pin）
ａは係数、Ｆは流量、Poutは吐出圧（絶対
圧）、Pinは吸込圧（絶対圧）である。 To explain this point in detail, if the production amount of liquid nitrogen becomes three times the production amount of liquid oxygen, the nitrogen flow rate of the high-pressure stage compressor 28 will play a role of the feed air flow rate.
It becomes 1.8 times. Comparing the total compressor power of the conventional device and this device under these conditions, in the case of an isothermal compressor, the power W is W=aFln(Pout/Pin) where a is the coefficient, F is the flow rate, and Pout is the discharge pressure (absolute pressure), Pin is the suction pressure (absolute pressure).
よつて、従来装置の場合、原料圧縮機２の動力
W11は、
W11＝aFln（６／１）
また、高圧段圧縮機１３ｂの動力W12は、
W12＝ａ×1.8Fln（61／６）
となる。 Therefore, in the case of the conventional device, the power of the raw material compressor 2
W 11 is W 11 =aFln (6/1), and the power W 12 of the high-pressure stage compressor 13b is W 12 =a×1.8Fln (61/6).
一方、本装置の場合、一次原料圧縮機２１の動
力W21は、
W21＝aFln（６／１）＋aFln（11／６）
また、高圧段圧縮機２８の動力W22は、
W22＝ａ×1.8Fln（61／11）
ここで、低圧段圧縮機２５の動力は、従来装置
の低圧段圧縮機１３ａの動力と同じであるため、
総動力の差は、
△Ｗ＝W11＋W12−W22−W22
＝ａ（1.8−１）Fln（11／６）
となる。すなわち、本装置によると、従来装置に
比べて
△Ｗ＝a0.8Fln（11／６）
分の動力を低減することができる。 On the other hand, in the case of this device, the power W 21 of the primary raw material compressor 21 is W 21 = aFln (6/1) + aFln (11/6), and the power W 22 of the high-pressure stage compressor 28 is W 22 = a ×1.8Fln (61/11) Here, since the power of the low-pressure stage compressor 25 is the same as the power of the low-pressure stage compressor 13a of the conventional device,
The difference in total power is △W=W 11 +W 12 −W 22 −W 22 =a(1.8-1)Fln(11/6). That is, according to this device, the power can be reduced by ΔW=a0.8Fln (11/6) compared to the conventional device.
ところで、原料空気の圧力は、高圧塔７１での
分離操作を行ないうる限度圧力内で上記した10
Kg／cm2ｇ以上に上げてもよい。ただし、この限度
圧力内においても、圧力が高くなるほど精留条件
が悪くなるため、これを補うために高圧塔段数を
増加させる等の対策が必要となる。 By the way, the pressure of the raw material air is within the limit pressure for performing the separation operation in the high pressure column 71, and is within the above-mentioned 10.
It may be increased to Kg/cm 2 g or more. However, even within this limit pressure, the higher the pressure, the worse the rectification conditions become, so measures such as increasing the number of high-pressure column plates are required to compensate for this.
上記のように本発明によるときは、原料空気
を、吸着塔の入口側で吸着塔での吸着操作に必要
な圧力まで加圧し、さらに吸着塔出口側で精留塔
の高圧塔での精留操作を行ないうる限度圧力内で
加圧することにより、従来装置と比較して、原料
空気の圧力を高め、液体窒素生産量の増加によつ
て循環窒素流量が原料空気流量よりも多くなる場
合に、大流量の循環窒素の圧縮比を小さく、少流
量の原料空気の圧縮比を大きくする構成としたか
ら、圧縮機総動力を低減することができる。この
ため、製造コスト中に大きな割合を占める動力コ
ストを安くでき、製品製造原価の低廉化を実現し
うるものである。
As described above, according to the present invention, the feed air is pressurized at the inlet side of the adsorption tower to the pressure necessary for adsorption operation in the adsorption tower, and then at the outlet side of the adsorption tower, it is subjected to rectification in the high pressure column of the rectification tower. By pressurizing within the limit pressure that can be operated, the pressure of the feed air is increased compared to conventional equipment, and when the circulating nitrogen flow rate becomes higher than the feed air flow rate due to an increase in liquid nitrogen production, Since the compression ratio of circulating nitrogen with a large flow rate is small and the compression ratio of raw material air with a small flow rate is large, the total power of the compressor can be reduced. Therefore, the power cost, which accounts for a large proportion of the manufacturing cost, can be reduced, and the manufacturing cost of the product can be reduced.
第１図は本発明の実施例にかかる空気分離装置
のフローシート、第２図は従来装置のフローシー
トである。
２１…一次原料圧縮機、３…吸着塔、２２…二
次原料圧縮機、７…精留塔、７１…精留塔の高圧
塔、７２…同低圧塔、２５…低圧窒素液化ライン
の低圧段圧縮機、２８…高圧液体窒素液化ライン
の高圧段圧縮機、１４…液化天然ガス熱交換器。
FIG. 1 is a flow sheet of an air separation device according to an embodiment of the present invention, and FIG. 2 is a flow sheet of a conventional device. 21...Primary raw material compressor, 3...Adsorption tower, 22...Secondary raw material compressor, 7...Rectification column, 71...High pressure column of the rectification column, 72...Low pressure column of the same, 25...Low pressure stage of the low pressure nitrogen liquefaction line Compressor, 28... High pressure stage compressor of high pressure liquid nitrogen liquefaction line, 14... Liquefied natural gas heat exchanger.
Claims (1)
する吸着塔を備えた原料供給ラインと、この原料
供給ラインから供給される原料空気を液体空気と
窒素ガスとに分離する高圧塔および上記液体空気
を液体酸素と窒素ガスとに分離する低圧塔から成
る精留塔と、この精留塔の高圧塔から出た高圧窒
素を加圧しかつ液化天然ガスを寒冷源とする冷媒
との熱交換により冷却し液化させて上記高圧塔に
還流液として送り込む高圧液体窒素還流ライン
と、精留塔の低圧塔頂部から出た低圧窒素を加圧
して低圧塔底部に送り込み液体酸素との熱交換に
よつて液化させる低圧窒素液化ラインとを具備
し、上記原料供給ラインに、上記吸着塔の入口側
において原料空気を吸着塔での吸着操作に必要な
圧力まで加圧する一次原料圧縮機と、吸着塔から
出た原料空気をさらに精留塔の高圧塔での精留操
作を行ないうる限度内において加圧して高圧塔に
送り込む二次原料圧縮機とが設けられてなること
を特徴とする空気分離装置。1. A raw material supply line equipped with an adsorption tower that adsorbs and removes unnecessary components such as moisture from raw material air, a high-pressure column that separates the raw material air supplied from this raw material supply line into liquid air and nitrogen gas, and the liquid air. A rectification column consists of a low-pressure column that separates gas into liquid oxygen and nitrogen gas, and the high-pressure nitrogen coming out of the high-pressure column of this rectification column is pressurized and cooled by heat exchange with a refrigerant that uses liquefied natural gas as a cooling source. A high-pressure liquid nitrogen reflux line is used to liquefy the nitrogen and send it as a reflux liquid to the high-pressure column, and a high-pressure liquid nitrogen reflux line is used to pressurize the low-pressure nitrogen that comes out from the top of the low-pressure column of the rectification column and send it to the bottom of the low-pressure column where it is liquefied by heat exchange with liquid oxygen. The raw material supply line is equipped with a primary raw material compressor that pressurizes the raw material air to the pressure required for adsorption operation in the adsorption tower at the inlet side of the adsorption tower, and a An air separation device characterized in that it is provided with a secondary raw material compressor that further pressurizes the raw material air within the limit that allows the rectification operation in the high pressure column of the rectification column and sends it to the high pressure column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63204965A JPH0252980A (en) | 1988-08-18 | 1988-08-18 | Air separating device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63204965A JPH0252980A (en) | 1988-08-18 | 1988-08-18 | Air separating device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0252980A JPH0252980A (en) | 1990-02-22 |
| JPH0413630B2 true JPH0413630B2 (en) | 1992-03-10 |
Family
ID=16499231
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63204965A Granted JPH0252980A (en) | 1988-08-18 | 1988-08-18 | Air separating device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0252980A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3466437B2 (en) * | 1997-09-24 | 2003-11-10 | ジャパン・エア・ガシズ株式会社 | Air separation equipment |
| CA2457075A1 (en) | 2001-08-15 | 2003-02-27 | Shell Internationale Research Maatschappij B.V. | Tertiary oil recovery combined with gas conversion process |
| US7712331B2 (en) * | 2006-06-30 | 2010-05-11 | Air Products And Chemicals, Inc. | System to increase capacity of LNG-based liquefier in air separation process |
| US10578356B2 (en) * | 2017-08-25 | 2020-03-03 | Praxair Technology, Inc. | Annular divided wall column for an air separation unit having a ring shaped support grid |
| CN109855389B (en) * | 2019-01-04 | 2020-11-13 | 曹建喜 | Method for producing liquid oxygen and liquid nitrogen by using LNG cold energy and single-tower rectification process |
-
1988
- 1988-08-18 JP JP63204965A patent/JPH0252980A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0252980A (en) | 1990-02-22 |
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