JPH03170785A - Extremely low temperature air separation and its apparatus - Google Patents
Extremely low temperature air separation and its apparatusInfo
- Publication number
- JPH03170785A JPH03170785A JP2241040A JP24104090A JPH03170785A JP H03170785 A JPH03170785 A JP H03170785A JP 2241040 A JP2241040 A JP 2241040A JP 24104090 A JP24104090 A JP 24104090A JP H03170785 A JPH03170785 A JP H03170785A
- Authority
- JP
- Japan
- Prior art keywords
- column
- fraction
- nitrogen
- oxygen
- air
- 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.)
- Pending
Links
- 238000000926 separation method Methods 0.000 title claims description 27
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 220
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 109
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 80
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 80
- 239000001301 oxygen Substances 0.000 claims abstract description 80
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 238000001816 cooling Methods 0.000 claims abstract description 16
- 238000004821 distillation Methods 0.000 claims description 62
- 238000000034 method Methods 0.000 claims description 53
- 239000002699 waste material Substances 0.000 claims description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 230000008016 vaporization Effects 0.000 claims description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims 2
- 230000001174 ascending effect Effects 0.000 claims 1
- 230000008878 coupling Effects 0.000 claims 1
- 238000010168 coupling process Methods 0.000 claims 1
- 238000005859 coupling reaction Methods 0.000 claims 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims 1
- 238000010438 heat treatment Methods 0.000 abstract description 6
- 238000009833 condensation Methods 0.000 abstract description 5
- 230000005494 condensation Effects 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 12
- 239000000203 mixture Substances 0.000 description 7
- 229910052786 argon Inorganic materials 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 4
- 239000002826 coolant Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000001944 continuous distillation Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000002609 medium Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000006163 transport media Substances 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
- 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
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
-
- 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
- F25J3/04424—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 without thermally coupled high and low pressure columns, i.e. a so-called split columns
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
-
- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
-
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
【発明の詳細な説明】
発明の技術分野
この発明は、空気分離方法の分野に関し、特に、液化空
気が高圧塔凝縮器に対する熱交換媒体として使用され、
エネルギ.一有効プロセスを提供するような空気から窒
素、酸素、および/またはアルゴンの製造方法およびそ
の装置に関する。TECHNICAL FIELD OF THE INVENTION The present invention relates to the field of air separation processes, in particular where liquefied air is used as a heat exchange medium to a high pressure column condenser;
Energy. The present invention relates to a method and apparatus for producing nitrogen, oxygen, and/or argon from air, providing an effective process.
従来技術
標準の極低温の空気分離方法は、導入空気を濾過して粒
状物質を除去し、その後、その空気を圧縮して分離用の
エネルギーを供給することを含む。Prior art standard cryogenic air separation methods involve filtering incoming air to remove particulate matter and then compressing the air to provide energy for separation.
一般に導入空気流は、その後、冷却され、吸収剤に通さ
れて二酸化炭素および水蒸気のような混入物が除去され
る。得られた気流は、極低温の蒸留に供される。Typically, the incoming air stream is then cooled and passed through an absorbent to remove contaminants such as carbon dioxide and water vapor. The resulting air stream is subjected to cryogenic distillation.
極低温の蒸留もしくは空気分離は、極低温で操作される
一つまたはそれ以上の分離塔に高圧空気を導入し、それ
により酸素、窒素、アルゴン、および希ガスを含む空気
成分が蒸留により分離され得ることを含む。Cryogenic distillation or air separation involves introducing high pressure air into one or more separation columns operated at cryogenic temperatures so that air components, including oxygen, nitrogen, argon, and noble gases, are separated by distillation. Including getting.
蒸気と液体の接触を含む極低温の分離方法は、それぞれ
の成分に対する蒸気圧の差に依存する。Cryogenic separation methods involving contact between vapor and liquid rely on the difference in vapor pressure for each component.
高蒸気圧(より揮発性があるまたはより低い沸点である
ことを意味する)を有する成分は、気相中で濃縮する傾
向を有する。低蒸気圧(揮発性が乏しいまたはより高い
沸点であることを意味する)を有する成分は、液相中で
濃縮する傾向がある。Components with high vapor pressure (meaning more volatile or lower boiling points) have a tendency to concentrate in the gas phase. Components with low vapor pressure (meaning poor volatility or higher boiling point) tend to concentrate in the liquid phase.
液状混合物の加熱で気相の揮発性成分と液相の揮発性に
乏しい成分を濃縮する分離プロセスは、蒸留を定義する
。部分的な凝縮は、蒸気混合物を冷却して揮発性成分を
気相中で濃縮し、同時に揮発性に乏しい成分を液相中で
濃縮する分離プロセスである。A separation process in which the heating of a liquid mixture concentrates the volatile components of the gas phase and the less volatile components of the liquid phase defines distillation. Partial condensation is a separation process in which a vapor mixture is cooled to concentrate volatile components in the gas phase while simultaneously concentrating less volatile components in the liquid phase.
液相における蒸気の向流処理を含む部分的蒸発および凝
縮を連続して組み合わせる方法は、精留とよばれるかま
たはときどき連続蒸留と呼ばれる。The process of sequentially combining partial evaporation and condensation involving countercurrent treatment of vapor in the liquid phase is called rectification or sometimes continuous distillation.
気相および液相の向流接触は、断熱的であり、相間の全
体もしくは微分的接触を含み得る。Countercurrent contact of the gas and liquid phases is adiabatic and may involve total or differential contact between the phases.
精留原理を用いた分離方法を達成し、混合物を分離する
ために使用される装置は、しばしば精留塔、蒸留塔、ま
たは分留塔と呼ばれる。The equipment used to achieve separation methods using the rectification principle and to separate mixtures is often called a rectification column, distillation column, or fractionation column.
本明細書でおよび特許請求の範囲において使用される場
合、「塔」なる語は蒸留もしくは分留の塔もしくは領域
を示す。それは、また液相または気相が流体混合物を分
離するために向流接触されるような接触塔もしくは領域
として記述され得る。As used herein and in the claims, the term "column" refers to a distillation or fractionation column or zone. It may also be described as a contacting column or zone in which liquid or gas phases are brought into countercurrent contact to separate fluid mixtures.
例えば、これは、しばしば穿孔されているおよび波形で
あるこ並びに中心袖に垂直で塔にクロスして延出した垂
直方向に離隔した一連のトレーもしくはプレート上にお
ける気相および液相の接触を含むであろう。トレーもし
くはプレートの代わりに、パッキング要素を使用して塔
を充填してもよい。For example, this may involve contacting the gas and liquid phases on a series of vertically spaced trays or plates that are often perforated and corrugated and extend across the column and perpendicular to the center sleeve. Probably. Instead of trays or plates, packing elements may be used to pack the column.
本明細書で使用される「二重塔」なる語は、低圧塔の下
端と熱交換する上端を有する高圧塔をいう。As used herein, the term "double column" refers to a high pressure column that has an upper end that exchanges heat with a lower end of the lower pressure column.
本明細書で使用される「標準空気分離方法または装置」
なる語は、上述された方法および装置はもちろん当業者
によく知られた他の空気分離方法の記述を意味する。"Standard Air Separation Method or Apparatus" as used herein
is meant to describe the methods and apparatus described above, as well as other air separation methods familiar to those skilled in the art.
本明細書でおよび添付した特許請求の範囲において使用
された「間接熱交換」なる語は、流体相互のなんらかの
物理的接触もしくは混合なしに2つの流体流が熱交換を
起こすことを意味する。As used herein and in the appended claims, the term "indirect heat exchange" means that two fluid streams exchange heat without any physical contact or mixing of the fluids with each other.
従来、窒素、酸素、および/またはアルゴンは、単一塔
プロセスおよび二重塔プロセスを含む2つの基本的なプ
ロセス機構の一つにより製造されている。Traditionally, nitrogen, oxygen, and/or argon are produced by one of two basic process mechanisms, including single column processes and double column processes.
窒素に関して、単一塔プロセスでは、約6〜10バール
の圧力で良質のガス状および液状の窒素を製造する。窒
素の回収は、塔の底部での平衡により制限される。通常
、このプロセスは、最初の原料空気中の窒素の約50〜
60%の割合で窒素を製造できる。Regarding nitrogen, single column processes produce good quality gaseous and liquid nitrogen at pressures of about 6-10 bar. Nitrogen recovery is limited by equilibrium at the bottom of the column. Typically, this process involves about 50% to 50% of the nitrogen in the initial feed air.
Nitrogen can be produced at a rate of 60%.
二重塔プロセスでは、窒素は約1〜4バールの圧力で製
造される。それは単一塔プロセスよりも効果的であり、
約90%またはそれ以上の窒素が最初の原料空気中の窒
素から回収され得る。通常、塔は2つの塔を分離す゜る
凝縮一再沸器を用いて積み重ねられている。このプロセ
スは比較的低圧で窒素を製造するので、さらに窒素の圧
縮がしばしば必要とされ、製造および使用コストを追加
してしまう。In double column processes, nitrogen is produced at a pressure of about 1 to 4 bar. It is more effective than single tower process and
Approximately 90% or more of the nitrogen may be recovered from the nitrogen in the initial feed air. Typically, the columns are stacked with a condenser-reboiler separating the two columns. Because this process produces nitrogen at relatively low pressures, further compression of the nitrogen is often required, adding to manufacturing and usage costs.
従来の二重塔プロセスにおいて、空気は極低温の蒸留も
しくは精留により分離され、高圧塔の頂部で窒素に富む
流れもしくは分画および底部で酸素に富む流れもしくは
分画を製造する。窒素に富む流れは、低圧塔の頂部に送
られこの塔の還流を提供する。底部の酸素富む流れは、
次の分離のために低圧塔に導入される。In a conventional double column process, air is separated by cryogenic distillation or rectification to produce a nitrogen-rich stream or fraction at the top of the high-pressure column and an oxygen-rich stream or fraction at the bottom. The nitrogen-rich stream is sent to the top of the low pressure column to provide reflux for the column. The oxygen-rich flow at the bottom is
It is introduced into a low pressure column for the next separation.
低圧塔において、導入流は極低温蒸留により底部での酸
素富む流れもしくは分画および頂部での窒素に富む流れ
もしくは分画に分離される。頂部流は、その後、窒素生
成物として回収され得る。In the low pressure column, the inlet stream is separated by cryogenic distillation into an oxygen-rich stream or fraction at the bottom and a nitrogen-rich stream or fraction at the top. The top stream can then be recovered as nitrogen product.
二重塔配列において、高圧塔および低圧塔は、凝縮器一
再沸器配列により熱的に結合されている。In a double column arrangement, the high pressure column and the low pressure column are thermally coupled by a condenser-reboiler arrangement.
このように、従来の二重塔プロセスにおいて、高圧塔の
窒素に富む分画は、低圧塔の気化した酸素に富む分画に
対し凝縮される。Thus, in a conventional double column process, the nitrogen-rich fraction of the higher pressure column is condensed against the vaporized oxygen-rich fraction of the lower pressure column.
低圧塔において与えられた圧力に対して、高圧塔に導入
する空気の圧力は、気化した酸素に富む流れの組成、高
圧塔凝縮器と低圧塔再沸器の温度差、およびある程度窒
素において比較的純度が高い凝縮した窒素に富む流れの
組成により規定される。For a given pressure in the low pressure column, the pressure of the air introduced into the high pressure column will depend on the composition of the vaporized oxygen-rich stream, the temperature difference between the high pressure column condenser and low pressure column reboiler, and to some extent the relative Defined by the composition of the highly pure, condensed, nitrogen-rich stream.
他の従来のプロセス機構は、付加的な塔頂凝縮器または
底部再沸器のような付加形態を有する上述した単一もし
くは二重塔プロセスの変形例である。Other conventional process setups are variations of the single or double column processes described above with additions such as additional overhead condensers or bottom reboilers.
発明の概要
この発明の方法は、窒素、酸素、およびアルゴンのエネ
ルギー効率のよい製造に使用され得る。SUMMARY OF THE INVENTION The method of this invention can be used for the energy efficient production of nitrogen, oxygen, and argon.
基本的には、この発明は、高圧および低圧塔間で加熱お
よび冷却媒体として気化されたおよび液化された空気を
使用することにある。従来、窒素が使用されていた。Basically, the invention consists in using vaporized and liquefied air as heating and cooling medium between high pressure and low pressure columns. Traditionally, nitrogen was used.
この発明は窒素に関してとくに詳しく説明されているが
、この発明は酸素、アルゴンの製造に同じく適用できる
ことを理解する必要がある。温度、圧力、および他の操
作条件をどのように最適化して主生成物として酸素およ
び/またはアルゴンの生産を最適化するかは当業者によ
り明らかになるであろう。Although the invention is described in particular detail with respect to nitrogen, it should be understood that the invention is equally applicable to the production of oxygen and argon. It will be clear to those skilled in the art how to optimize the temperature, pressure, and other operating conditions to optimize the production of oxygen and/or argon as the primary products.
加熱および冷却媒体としての空気の使用における特定の
利点は、窒素に富む流れの凝縮より空気の凝縮の方がよ
り少ないエネルギーを必要とすることである。主なエネ
ルギーのコストがガスの圧縮を含むので、与えられる温
度で空気を凝縮するために必要とされる比較的低い圧力
は窒素を凝縮するためよりも高価でない。A particular advantage of using air as a heating and cooling medium is that condensing air requires less energy than condensing a nitrogen-rich stream. The relatively low pressure required to condense air at a given temperature is less expensive than to condense nitrogen, since the primary energy cost involves compression of the gas.
例えば、窒素は−180℃、7バールで凝縮する。これ
に対して、−178℃、6バールのみが空気を凝縮する
ために必要とされる。このように、2℃の温度差および
1バールの圧力差は、この発明の方法において減少され
たエネルギー消費を提供する。For example, nitrogen condenses at -180°C and 7 bar. In contrast, only -178°C and 6 bar are required to condense the air. Thus, a temperature difference of 2° C. and a pressure difference of 1 bar provides a reduced energy consumption in the method of the invention.
窒素が高圧および低圧塔間で加熱および冷却媒体として
使用される従来の方法において、窒素で必要であるよう
に導入空気をより高い導入空気圧力に圧縮する必要があ
る。このように、最初のエネルギー節約は、導入空気の
圧縮に対する減少された必要からきている。In conventional methods where nitrogen is used as a heating and cooling medium between high pressure and low pressure columns, it is necessary to compress the inlet air to a higher inlet air pressure as is required with nitrogen. Thus, the first energy savings come from the reduced need for compression of the introduced air.
この発明の方法は、最初の導入空気に含まれる窒素の9
0%以上程度の高純度窒素の製造を可能にする。それは
約3バール〜約15バールの範囲内の圧力で製造され得
る。高圧および低圧窒素の両方が製造され得る。これは
別々にもしくは一緒に行われ得る。さらに、この方法は
従来の方法に比べてエネルギー効率がよい。The method of this invention requires that 9% of the nitrogen contained in the initially introduced air be
This makes it possible to produce high purity nitrogen of approximately 0% or more. It may be manufactured at a pressure within the range of about 3 bar to about 15 bar. Both high pressure and low pressure nitrogen can be produced. This can be done separately or together. Furthermore, this method is more energy efficient than traditional methods.
この発明の方法によれば、分子篩、アルミナ、シリカゲ
ル等を通すことにより水分並びにCO2およびメタンの
ような不純物を除去するために処理された導入空気は、
圧縮され熱交換器に導入され、流出生成物と熱交換する
。According to the method of this invention, the incoming air is treated to remove moisture and impurities such as CO2 and methane by passing through molecular sieves, alumina, silica gel, etc.
It is compressed and introduced into a heat exchanger to exchange heat with the effluent product.
一つの態様によれば、導入空気は2つの分画に分けられ
、一つの分画は高圧塔の底部に導入され、他の分画は低
圧塔の基底部に位置する凝縮器/再沸器に導入される。According to one embodiment, the introduced air is divided into two fractions, one fraction is introduced at the bottom of the high pressure column and the other fraction is placed in a condenser/reboiler located at the base of the low pressure column. will be introduced in
他の割合を使用することができるが、導入空気を等しい
部分に分けることにより良好な結果が得られた。Although other proportions can be used, good results have been obtained by dividing the introduced air into equal parts.
他の態様によれば、導入空気は3つの分画に分けられる
。導入空気の2つの部分は上述のように高圧塔および低
圧塔の基底部の凝縮器/再沸器に導入される。第3の空
気分画は膨張され、設備の冷却を提供し、その後極低温
分離のために低圧塔に導入される。According to another embodiment, the introduced air is divided into three fractions. Two portions of the incoming air are introduced into the condenser/reboiler at the base of the high pressure column and the low pressure column as described above. The third air fraction is expanded to provide equipment cooling and then introduced into the low pressure column for cryogenic separation.
第1の導入空気分画は、高圧塔内で極低温蒸留により第
1の窒素に富む気体分画および第1の酸素に富む液体分
画に分離される。酸素にざむ液体分画は、高圧塔の基底
部から取り出され、低圧塔に送られる。低圧塔の基底部
の凝縮器/再沸器に送られた第2の導入空気分画は、低
圧塔の底部で酸素に富む液体を用いた熱交換により凝縮
され、それにより酸素に富む液体は気化される。凝縮器
/再沸器においてこのように製造された凝縮され液化さ
れた空気は、その後高圧塔の頂部凝縮器に導入され、そ
こで高圧塔で製造された第1の窒素に富む気体分画を用
いた間接熱交換により気化される。これは窒素を凝縮さ
せる。The first introduced air fraction is separated into a first nitrogen-rich gas fraction and a first oxygen-rich liquid fraction by cryogenic distillation in a high-pressure column. The oxygen-enriched liquid fraction is removed from the base of the high pressure column and sent to the low pressure column. The second inlet air fraction sent to the condenser/reboiler at the base of the LP column is condensed by heat exchange with an oxygen-rich liquid at the bottom of the LP column, whereby the oxygen-rich liquid is vaporized. The condensed and liquefied air thus produced in the condenser/reboiler is then introduced into the top condenser of the high pressure column where it is used with the first nitrogen-rich gas fraction produced in the high pressure column. vaporized by indirect heat exchange. This condenses the nitrogen.
一つの態様によれば、高圧塔において凝縮された窒素に
富む分画の一部は、分離され低圧塔に導入され過剰の還
流を提供する。同特に高圧塔の頂部凝縮器で窒素と接触
する間接熱交換により気化された第2の導入空気分画は
、その後極低温用に低圧塔に導入される。According to one embodiment, a portion of the nitrogen-rich fraction condensed in the higher pressure column is separated and introduced into the lower pressure column to provide excess reflux. The second inlet air fraction, which is vaporized by indirect heat exchange in contact with nitrogen, in particular in the top condenser of the high-pressure column, is then introduced into the low-pressure column for cryogenic use.
低圧塔内で、高圧塔からの第1の酸素に富む分画の一部
と共に第2の導入空気分画は、その後第2の窒素に富む
流れおよび第2の酸素に富む流れに分離される。In the lower pressure column, the second introduced air fraction along with a portion of the first oxygen-rich fraction from the higher pressure column is then separated into a second nitrogen-rich stream and a second oxygen-rich stream. .
他の態様によれば、第2の窒素に富む流れの一部は高圧
窒素生成物として除去され得る。一方、残りの部分は低
圧塔用の還流を提供するために使用される。According to other embodiments, a portion of the second nitrogen-rich stream may be removed as a high pressure nitrogen product. Meanwhile, the remaining portion is used to provide reflux for the lower pressure column.
他の態様によれば、高圧窒素生戊物の一部は膨張され設
備の冷却に提供され、低圧窒素生成物気流に加えられる
。According to another embodiment, a portion of the high pressure nitrogen product is expanded and provided for equipment cooling and added to the low pressure nitrogen product stream.
低圧塔の底部に降下する第2の酸素に富む流れは、入っ
てくる第2の導入空気分画と接触する間接熱交換により
気化され、それにより第2の導入空気分画は凝縮される
。他の態様により、第2の酸素に富む分画は低圧塔に導
入される前に膨張される第3の導入空気分画も含む。The second oxygen-rich stream descending to the bottom of the low pressure column is vaporized by indirect heat exchange in contact with the incoming second inlet air fraction, thereby condensing the second inlet air fraction. According to other embodiments, the second oxygen-rich fraction also includes a third introduced air fraction that is expanded before being introduced into the lower pressure column.
第2の酸素に富む流れの一部は低圧塔の頂部凝縮器に導
入され、そこで上昇する窒素と接触する熱交換により気
化され、それにより窒素は凝縮される。このように気化
された第2の酸素に富む流れは、廃棄物として頂部凝縮
器から除去され、プロセス気流および導入空気を用いた
間接熱交換により過冷却器および熱交換器で暖められる
。A portion of the second oxygen-rich stream is introduced into the top condenser of the low pressure column where it is vaporized by heat exchange in contact with the rising nitrogen, thereby condensing the nitrogen. The second oxygen-rich stream thus vaporized is removed from the top condenser as waste and warmed in the subcooler and heat exchanger by indirect heat exchange with the process air stream and incoming air.
望ましくは、廃棄酸素が膨張され設備の冷却に提供され
ることである。あるいは、約70%の純度を有する廃粂
酸素が、高純度酸素を必要としない用途における生成物
として使用されることである。Desirably, the waste oxygen is expanded and provided for equipment cooling. Alternatively, waste oxygen having a purity of about 70% is used as a product in applications that do not require high purity oxygen.
上述の方法のための装置も提供されている。この装置は
、外界源からの空気を圧縮する空気圧縮手段、空気圧縮
手段により圧縮された空気から二酸化炭素および水蒸気
を除去する精密手段、および精密手段からの圧縮された
空気を極低温に冷却する熱交換手段の組み合わせを含む
。頂部塔または頂部蒸発器/凝縮器を備えた第1の蒸留
塔は、熱交換器からの導入空気の一部の極低温分離のた
めに含まれる。An apparatus for the above method is also provided. This device includes an air compression means for compressing air from an external source, a precision means for removing carbon dioxide and water vapor from the air compressed by the air compression means, and a precision means for cooling the compressed air from the precision means to cryogenic temperatures. Including a combination of heat exchange means. A first distillation column with a top column or top evaporator/condenser is included for cryogenic separation of a portion of the incoming air from the heat exchanger.
頂部塔凝縮器および底部塔再沸器を備えた第2の蒸留塔
は、第1の蒸留塔から得られた酸素富化液体の少なくと
も一部と共に、第2の蒸留塔の底部塔再沸器および第1
の蒸留塔の頂部塔凝縮器による循環の後の冷却され圧縮
された導入空気の少なくとも一部の分留による、第2の
酸素に富む分画および第2の窒素に富む分画への分離の
ために提供される。A second distillation column comprising a top column condenser and a bottom column reboiler, together with at least a portion of the oxygen-enriched liquid obtained from the first distillation column, the bottom column reboiler of the second distillation column. and the first
separation into a second oxygen-rich fraction and a second nitrogen-rich fraction by fractional distillation of at least a portion of the cooled and compressed inlet air after circulation through a top column condenser of a distillation column of provided for.
第2の蒸留塔内で上昇する蒸気との間接熱交換を堤供す
るために第2の蒸留塔の頂部凝縮器への導入のための第
2の蒸留塔の基底部での酸素液体の取り出しのための手
段が設けられている。withdrawal of oxygenated liquid at the base of the second distillation column for introduction into the top condenser of the second distillation column to provide indirect heat exchange with the rising vapor in the second distillation column; There are means for this.
膨張手段は、第2の蒸留塔の頂部凝縮器から取り出され
κ酸素の第2の蒸留塔への導入前の圧縮空気の膨張のた
め、および/または冷却用の窒素生戊物の膨張のために
設けられる。Expansion means are provided for the expansion of compressed air taken from the top condenser of the second distillation column and prior to the introduction of the κ oxygen into the second distillation column and/or for the expansion of the nitrogen production for cooling. established in
発明の詳細な記述
第1図の工程系統図において、不純物のない圧縮された
導入空気が導管20により熱交換器30に導入される。DETAILED DESCRIPTION OF THE INVENTION In the process diagram of FIG. 1, clean, compressed inlet air is introduced by conduit 20 into a heat exchanger 30.
空気は好ましくは約5バール〜約20バールの範囲の圧
力で熱交換器30に導入され、そこで空気の温“度は発
生した廃棄物および生成物を用いた間接熱交換により極
低温に冷却される。Air is preferably introduced into the heat exchanger 30 at a pressure in the range of about 5 bar to about 20 bar, where the temperature of the air is cooled to cryogenic temperatures by indirect heat exchange with generated waste and products. Ru.
次いで、導入空気は2つの分画に分割される。The introduced air is then divided into two fractions.
導入空気を等しい部分に分けるもしくは気流を用いて良
好な結果が得られるが、他の割合が使用され得る二導入
空気の第1の分画はライン22および62により高圧塔
32に送られ、導入空気の残りの第2の分画はライン2
2および60により低圧塔34の再沸器58に送られる
。Good results have been obtained by dividing the inlet air into equal parts or using airflow, but other proportions may be used. The first fraction of the inlet air is sent by lines 22 and 62 to the high pressure column 32 and the inlet air is The remaining second fraction of air is line 2
2 and 60 to reboiler 58 of low pressure column 34.
高圧塔32で圧力は好ましくは約5バール〜20バール
の範囲である。In the high pressure column 32 the pressure preferably ranges from about 5 bar to 20 bar.
第1の導入空気分画は、底部蒸留トレーの下方の36で
示されるような塔32の下部に導入される。ここで、第
1の導入空気分画は・塔32の頂部に上昇する第1の窒
素に富む気体分画と塔32の底部に降下する第1の酸素
に富む液体分画に分離される。A first introduced air fraction is introduced at the bottom of the column 32 as indicated at 36 below the bottom distillation tray. Here, the first introduced air fraction is separated into a first nitrogen-rich gas fraction that rises to the top of column 32 and a first oxygen-rich liquid fraction that descends to the bottom of column 32.
第1の酸素に富む液体の少なくとも一部は、高圧塔の底
部38から回収される。それは約35%〜40%の酸素
を含有する。それは従来技術の方法とほぼ同じ割合であ
る。At least a portion of the first oxygen-rich liquid is recovered from the bottom 38 of the high pressure column. It contains about 35% to 40% oxygen. It is approximately the same proportion as the prior art method.
ライン54により高圧塔32の底部から取り除かれた第
1の酸素に富む液体は過冷却器46に通され、そこでラ
イン48により低圧塔34の上部から出る生成物窒素お
よび低圧塔34の頂部凝縮器/蒸発器から出る廃棄物を
用いた間接熱交換により温度がさらに減少する。The first oxygen-rich liquid removed from the bottom of the high pressure column 32 by line 54 is passed to a subcooler 46 where the product nitrogen exits from the top of the low pressure column 34 by line 48 and to the top condenser of the low pressure column 34. /The temperature is further reduced by indirect heat exchange with the waste leaving the evaporator.
過冷却器46からの冷却された第1の酸素に富む液体は
、その後弁76による膨張の後底部トレー上方の低圧塔
34に導入される。The cooled first oxygen-enriched liquid from subcooler 46 is then introduced into low pressure column 34 above the bottom tray after expansion through valve 76 .
低圧塔34の基底部の凝縮器/再沸器58に入った第2
の導入空気分画は、低圧塔34の底部で酸素に富む液体
を用いた間接熱交換により凝縮される。これは第2の導
入空気分画を凝縮させ、酸素に富む液体を気化させる。A second condenser/reboiler 58 at the base of the low pressure column
The introduced air fraction is condensed at the bottom of the low pressure column 34 by indirect heat exchange with an oxygen-enriched liquid. This condenses the second introduced air fraction and vaporizes the oxygen-rich liquid.
凝縮された第2の導入空気分画は、低圧塔34の凝縮器
/再沸゛器を離れてライン82を経て過冷却器46に入
る。液化された空気は過冷却器46を出てライン84を
経て、弁44により膨張され高圧塔32の凝縮器/再沸
器40に入る。必要であれば、凝縮された第2の導入空
気分画の一部を弁92により膨張された後ライン90を
経て低圧塔34に導入し、高圧および低圧塔間で空気の
バランスを制御することができる。The condensed second inlet air fraction leaves the condenser/reboiler of low pressure column 34 and enters subcooler 46 via line 82. Liquefied air exits subcooler 46 via line 84 and is expanded by valve 44 into condenser/reboiler 40 of high pressure column 32. If necessary, a portion of the condensed second inlet air fraction is expanded by valve 92 and then introduced into the low pressure column 34 via line 90 to control the balance of air between the high and low pressure columns. Can be done.
第1の窒素に富む気体分画は、高圧塔32の頂部に上昇
し、そこで凝縮器/再沸器40に入る。The first nitrogen-rich gas fraction rises to the top of high pressure column 32 where it enters condenser/reboiler 40.
ここで、窒素蒸気は、低圧塔34の凝縮器/再沸器58
から弁44を通り入る凝縮された第2の導大空気分画と
接触する間接熱交換を生じさせる。Here, the nitrogen vapor is transferred to the condenser/reboiler 58 of the low pressure column 34.
indirect heat exchange occurs in contact with the condensed second condensed large air fraction passing through valve 44.
これは液化された空気を気化させ、窒素蒸気を凝縮させ
る。第3図および第4図に示すように、凝縮された窒素
部分の一部もしくは全部は高圧塔32に戻り、必要に応
じて還流を提供する。This vaporizes the liquefied air and condenses the nitrogen vapor. As shown in FIGS. 3 and 4, some or all of the condensed nitrogen portion is returned to high pressure column 32 to provide reflux as needed.
凝縮された第2の導入空気分画を用いた間接熱交換によ
り凝縮されないいずれかの窒素蒸気は、高圧塔32の上
部から例えば第3図に示すようにライン67による除去
により高圧窒素として回収され得る。Any nitrogen vapor that is not condensed by indirect heat exchange with the condensed second introduced air fraction is recovered as high pressure nitrogen from the top of high pressure column 32 by removal, e.g., by line 67 as shown in FIG. obtain.
もし高圧窒素流が小さいか必要でないならば、凝縮され
た窒素の一部は特別な還流のために低圧塔34に送られ
得る。凝縮された窒素のこの部分は、第1図および第3
図に示すようにライン68により高圧塔32の上部から
除去される。凝縮された窒素はその後、過冷却器66に
通され、そこで発生する窒素生成物および廃棄物と接触
する間接熱交換を生じさせる。過冷却器66から、凝縮
された窒素は連続したライン68を通り、弁78による
膨張の後低圧塔34に導入される。If high pressure nitrogen flow is small or not needed, a portion of the condensed nitrogen can be sent to lower pressure column 34 for extra reflux. This portion of the condensed nitrogen is shown in Figures 1 and 3.
It is removed from the top of high pressure column 32 by line 68 as shown. The condensed nitrogen is then passed to a subcooler 66 to create an indirect heat exchange in contact with the nitrogen products and waste generated therein. From the subcooler 66, the condensed nitrogen passes through a continuous line 68 and is introduced into the low pressure column 34 after expansion through a valve 78.
.同時に、高圧塔32の頂部の凝縮器/再沸器40から
ライン56を経て出る気化された空気は、ライン54に
より入る第1の酸素に富む肢体の導入用とほぼ同じレベ
ルで、ライン64による低圧塔34への導入により分離
される。.. At the same time, the vaporized air leaving the condenser/reboiler 40 at the top of the high pressure column 32 via line 56 is at about the same level as for the introduction of the first oxygen-rich limb by line 64, entering by line 54. It is separated by introduction into the low pressure column 34.
塔32の基底部から取り出された第1の酸素に富む肢体
および高圧塔32の頂部の凝縮器/再沸器40からライ
ン56により取り出された気化された空気は、塔34出
で第2の窒素に富む気体分画および第2の酸素に富む分
画にさらに分離される。The first oxygen-rich limb removed from the base of column 32 and the vaporized air removed by line 56 from the condenser/reboiler 40 at the top of high pressure column 32 are transferred to the second oxygen-rich limb at the exit of column 34. It is further separated into a nitrogen-rich gas fraction and a second oxygen-rich fraction.
第2の窒素に富む気′体分画は低圧塔34の頂部に上昇
し、一方、第2の酸素に富む分画は低圧塔34の底部に
下降する。The second nitrogen-rich gaseous fraction rises to the top of the low pressure column 34, while the second oxygen-rich fraction falls to the bottom of the low pressure column 34.
低圧塔34の底部で第2の酸素に富む液体分画の一部は
、ライン74により取り出され、第1の過冷却器46に
通される。ここで、第2の酸素に富む液体は、低圧塔3
4の上部からライン48により除去された窒素ガスおよ
び低圧塔34の頂部凝縮器70からライン52により出
る廃粂物気流を用いた間接熱交換によりさらに冷却され
る。A portion of the second oxygen-rich liquid fraction at the bottom of the low pressure column 34 is removed by line 74 and passed to the first subcooler 46 . Here, the second oxygen-rich liquid is in the lower pressure column 3
Further cooling is provided by indirect heat exchange with nitrogen gas removed from the top of column 4 by line 48 and waste air stream exiting by line 52 from the top condenser 70 of low pressure column 34.
第2の酸素に富む液体は、高圧塔32の頂部からライン
68により除去された窒素ガスおよび頂部凝縮器70か
らライン52により出る廃棄酸素気流を用いた間接熱交
換によりさらに冷却するために、連続するライン74に
より第2の過冷却器66に通される。The second oxygen-rich liquid is continuously cooled for further cooling by indirect heat exchange with nitrogen gas removed from the top of high pressure column 32 by line 68 and waste oxygen stream exiting by line 52 from top condenser 70. A line 74 leads to the second subcooler 66 .
得られた冷却された第2の酸素に富む液体は延出するラ
イン74に通され、そこで液体は弁72による膨張の後
低圧塔34の頂部の頂部凝縮器70に導入され、第2の
酸素に富む流れを冷却する。The resulting cooled second oxygen-enriched liquid is passed to an extending line 74 where the liquid, after expansion by a valve 72, is introduced into a top condenser 70 at the top of the low pressure column 34 where a second oxygen-enriched liquid is passed. Cooling streams rich in
第2の窒素に富む流れの主部は、低圧塔343の上部か
らライン48により窒素生戊物として回収される。ガス
状窒素気流は、系を出る前に過冷却器66および46、
並びに熱交換器30の通過により暖められる。A major portion of the second nitrogen-rich stream is recovered as nitrogen product from the top of the lower pressure column 343 via line 48. The gaseous nitrogen stream passes through subcoolers 66 and 46 before exiting the system;
It is also heated by passing through a heat exchanger 30.
低圧塔34内の第2の窒素に富む流れの残りの部分は、
低圧塔34の頂部蒸発器/凝縮器70で第2の酸素に富
む液体を用いた熱交換により凝縮され、第2の酸素に富
む液体を気化させる。窒素の凝縮は、低圧塔34用の還
流を提供する。気化した酸素に富む液体は、頂部蒸発器
/凝縮器70を出てライン52を経て、続けて過冷却器
46および66並びに熱交換器30の通過により暖めら
れる。The remaining portion of the second nitrogen-rich stream in low pressure column 34 is
It is condensed by heat exchange with the second oxygen-rich liquid in the top evaporator/condenser 70 of the low pressure column 34, vaporizing the second oxygen-rich liquid. Condensation of nitrogen provides reflux for low pressure column 34. The vaporized oxygen-rich liquid exits the top evaporator/condenser 70 via line 52 and is subsequently warmed by passage through subcoolers 46 and 66 and heat exchanger 30.
熱交換器30で暖めた後、廃棄酸素気流はターボエキス
パンダー78に通され、そこで気流は膨張され設備冷却
に提供され得る。After warming in heat exchanger 30, the waste oxygen stream is passed to turboexpander 78 where it can be expanded and provided for equipment cooling.
上述した方法は、高圧および低圧塔間で空気を加熱およ
び冷却媒体として使用するものであることが分かる。従
来の方法において、窒素に富む流れは、低圧塔の底部に
熱を輸送するために使用されている。所定の窒素の回収
、すなわち同じ組戊の酸素に富む流れを有する窒素の回
収のために、より多くのエネルギーが空気を凝縮するた
めよりも窒素に富む流れを凝縮するために必要とされる
ことに留意すべきである。これが意味するものは、熱輸
送媒体として空気を使用する所定の窒素の回収のために
は、高圧塔が従来の技術の方法よりも低い圧力で機能し
得ることである。また、この発明によれば、高圧塔にお
ける同じ圧力1こ対して、低圧塔がより高い圧力で機能
し得る。It will be appreciated that the method described above uses air as a heating and cooling medium between the high pressure and low pressure columns. In conventional methods, a nitrogen-rich stream is used to transport heat to the bottom of the low pressure column. For a given nitrogen recovery, i.e., nitrogen recovery with the same composition of oxygen-rich stream, more energy is required to condense the nitrogen-rich stream than to condense air. should be kept in mind. What this means is that for a given nitrogen recovery using air as the heat transport medium, high pressure columns can operate at lower pressures than prior art methods. Also, according to the invention, the low pressure column can function at a higher pressure for the same pressure in the high pressure column.
以下の第1表は、生成物として窒素生戊物に対する第1
図および上の記述に示されたこの発明の予期される性能
を示す。Table 1 below shows the first
Figure 3 illustrates the expected performance of the invention as illustrated in the figures and above description.
総導入空気流
導入空気圧力
窒素生成物流
窒素圧力
窒素純度
廃棄tV(#素富化)流
i秦物圧力
圧縮空気
塔32
1i132
j!32
酸素富化液体
1縮された第2の
導入空気分言
凝縮された第2の
導入空気分画
M1された第2の
導入空気分画
第1表
ライン20
ライン20
ライン48
ライン18
ライン52
ライン16
ライン22
頂部
底部
ライン38
ライン82
ライン82
ライン84
154Ei2Nm3 /h
10.2パール abs
10514Nm’ /b
5.5バール abs.
18vpm 02
4948NII1’ /h
1,3バール abs .
−l80°C
lO,2パール abs.
−170°C
−160℃
−1[35.G℃
−l[i7.5℃
−187.5℃
− t 7 t ’c
凝縮器/)I沸器40
からの気化された
第2の導入空気分画
窒素排出塔32
Hされた窒素搏出
過冷却器66
塔34
塔34からの
!素富化液体
冷却器66から出る
a素富化液体
l張後の
酸素富化液体
塔34から出る
窒素生成物
塔34から出る
窒素生成物
凝縮器70からの
酸素!I棄気流
ライン56
ライン68
ライン68
ライン74
ライン74
#72
ライン48
ライン48
ライン52
−172.8℃
−170.6°C
−174.4℃
5.5バール abs、
−168.8°C
−174.4°C
−179°C
−177.8℃
5バール
abs .
−178.9℃
第3図および第4図に示される態様に従う場合、21バ
ールabs .の導入空気圧力は、高圧塔32内で約2
0バールabs.の圧力および低圧党34内で約14バ
ールabs .の圧力を生じるであろう。Total introduced air flow Introduced air pressure Nitrogen product stream Nitrogen pressure Nitrogen purity Disposal tV (#subenriching) stream i Qin material pressure Compressed air tower 32 1i132 j! 32 Oxygen Enriched Liquid 1 Condensed Second Inlet Air Fraction Condensed Second Inlet Air Fraction M1 Condensed Second Inlet Air Fraction Table 1 Line 20 Line 20 Line 48 Line 18 Line 52 Line 16 line 22 top bottom line 38 line 82 line 82 line 84 154Ei2Nm3 /h 10.2 pearl abs 10514Nm' /b 5.5 bar abs. 18vpm 02 4948NII1' /h 1,3 bar abs. -l80°C lO, 2 pearl abs. -170°C -160°C -1 [35. G°C -l [i7.5°C -187.5°C - t7t'c Condenser/) Second vaporized inlet air fraction from I boiler 40 Nitrogen discharge column 32 H nitrogen removal Supercooler 66 Tower 34 From tower 34! Nitrogen product exiting from column 34 Nitrogen product exiting column 34 Oxygen from condenser 70! I waste air flow line 56 line 68 line 68 line 74 line 74 #72 line 48 line 48 line 52 -172.8°C -170.6°C -174.4°C 5.5 bar abs, -168.8°C - 174.4°C -179°C -177.8°C 5 bar abs. −178.9° C. When following the embodiment shown in FIGS. 3 and 4, 21 bar abs. The introduced air pressure in the high pressure column 32 is approximately 2
0 bar abs. A pressure of about 14 bar abs. pressure will be generated.
上述したようなこの発明の方法および装置の種々の変形
例は、当業者に明らかであり、特許請求の範囲により規
定される発明の精神および範囲から逸脱しないで依存さ
れ得る。Various modifications of the method and apparatus of the invention as described above will be apparent to those skilled in the art and may be relied upon without departing from the spirit and scope of the invention as defined by the claims.
第1図は低圧窒素が製造されるこの発明の方法および装
置の概略工程系統図、第2図は空気膨張が廃棄物膨張の
代わりに提供されること以外は第1図と同じこの発明の
方法および装置の概略工程系統図、第3図は高圧および
低圧窒素が製造されるこの発明の方法および装置の概斃
工程系統図、第4図は高圧窒素の一部が低圧窒素に膨張
されるような第3図と同じこの発明の方法および装置の
概略工程系統図である。
30・・・熱交換器、32・・・高圧塔、34・・・低
圧塔、40・・・凝縮器/再沸器、46.66・・・過
冷却器、58・・・再沸器、
7
0・・・頂部凝縮器、
7
8・・・ターボ
エキスパンダーFIG. 1 is a schematic process diagram of the method and apparatus of the present invention in which low pressure nitrogen is produced; FIG. 2 is the same method of the invention as in FIG. 1 except that air expansion is provided instead of waste expansion; and a schematic process flow diagram of the apparatus; FIG. 3 is a schematic process flow diagram of the method and apparatus of the present invention in which high-pressure and low-pressure nitrogen is produced; FIG. FIG. 4 is a schematic process flow diagram of the method and apparatus of the present invention, which is the same as FIG. 3; 30... Heat exchanger, 32... High pressure column, 34... Low pressure column, 40... Condenser/reboiler, 46.66... Supercooler, 58... Reboiler , 7 0...Top condenser, 7 8...Turbo expander
Claims (21)
蒸気分画、少なくとも一つの液体分画、並びに少なくと
も一つの生成窒素気流を製造することによる空気の極低
温分離方法であって、 冷却され圧縮された蒸気状態の導入空気流を提供し、 少なくとも一つの該液体分画の間接熱交換接触により該
導入空気気流の少なくとも一部を凝縮して該液体分画を
気化し、該導入空気流を凝縮し、 該蒸気分画の一つとの間接熱交換接触により該凝縮され
た導入空気流の一部を気化する工程を具備する空気の極
低温分離方法。(1) A process for the cryogenic separation of air by rectification in at least one column to produce at least one vapor fraction, at least one liquid fraction, and at least one product nitrogen stream, the method comprising: providing an inlet air stream in a compressed vapor state, condensing at least a portion of the inlet air stream to vaporize the liquid fraction by indirect heat exchange contact of the at least one liquid fraction; and vaporizing a portion of the condensed incoming air stream by indirect heat exchange contact with one of the vapor fractions.
用の導入空気としてさらに該蒸留塔の一つに導入される
請求項1記載の方法。2. The method of claim 1, wherein said vaporized inlet air stream is further introduced into one of said distillation columns as inlet air for cryogenic separation by rectification.
1の酸素富化分画および第1の窒素富化液体分画を生成
し、該第1の酸素富化分画の少なくとも一部が低圧蒸留
塔に導入され、第2の酸素富化分画および第2の窒素富
化分画を生成する窒素の製造方法であって、加熱および
冷却媒体として空気を使用して高圧塔と低圧塔を熱的に
結合する工程を具備する空気の極低温分離方法。(3) performing cryogenic distillation of air in a high-pressure distillation column to produce a first oxygen-enriched fraction and a first nitrogen-enriched liquid fraction; at least a portion of the first oxygen-enriched fraction; is introduced into a low-pressure distillation column to produce a second oxygen-enriched fraction and a second nitrogen-enriched fraction, the method comprising: A method for cryogenic separation of air comprising the step of thermally coupling a column.
れる第1の導入空気分画と該第2の酸素富化分画に関す
る間接熱交換を生じさせる第2の導入空気分画に分離し
、該第2の酸素富化分画の少なくとも一部を気化し、該
第2の導入空気分画の少なくとも一部を凝縮し、 該凝縮された第2の導入空気分画を該第1の窒素富化分
画との間接熱交換関係に通し、該第1の窒素富化分画を
凝縮し、該凝縮された第2の導入空気分画を気化し、 該気化した第2の導入空気分画を極低温分離のために該
低圧塔に導入することをさらに具備する請求項3記載の
方法。(4) a second inlet air fraction that causes indirect heat exchange between the first inlet air fraction and the second oxygen-enriched fraction that are introduced into the high pressure column for cryogenic separation of the inlet air; vaporizing at least a portion of the second oxygen-enriched fraction; condensing at least a portion of the second introduced air fraction; condensing the first nitrogen-enriched fraction and vaporizing the condensed second introduced air fraction through indirect heat exchange with a first nitrogen-enriched fraction; 4. The method of claim 3, further comprising introducing an incoming air fraction of 200 to the low pressure column for cryogenic separation.
圧縮された導入空気を第1の導入空気分画と第2の導入
空気分画に分け、 (B)該第1の導入空気分画を頂部凝縮器を備えた高圧
塔に導入し、 (C)該高圧塔内の該第1の導入空気分画を極低温蒸留
により第1の窒素富化分画と第1の酸素富化分画に分離
し、 (D)該高圧塔から該第1の酸素富化分画の少なくとも
一部を取り出し、 (E)該第1の酸素富化分画の少なくとも一部を、第2
の窒素富化分画と第2の酸素富化分画への極低温分離の
ために底部凝縮器/再沸器および頂部蒸発器/凝縮器を
備えた低圧塔に導入し、 (F)該第2の導入空気分画を該低圧塔の該凝縮器/再
沸器に導入し、 (G)該低圧塔における該第2の酸素富化分画を用いた
間接熱交換により該第2の導入空気分画を凝縮してそれ
により該第2の酸素富化分画の少なくとも一部を気化し
、 (H)該凝縮された第2の導入空気分画の少なくとも一
部を該高圧塔の該頂部凝縮器に導入し、 (I)該高圧塔における該第1の窒素富化分画の少なく
とも一部を用いた間接熱交換により該高圧塔の該頂部凝
縮器内の該第2の凝縮された導入空気分画の少なくとも
一部を気化し、 (J)該第1の酸素富化分画の少なくとも一部をまた第
2の窒素富化分画と第2の酸素富化分画への極低温分離
のために、該高圧塔の該頂部凝縮器における該第1の窒
素富化分画との間接熱交換接触により気化された該第2
の導入空気分画の少なくとも一部を該低圧塔に導入し、 (K)該低圧塔から生成物として該第2の窒素富化分画
の少なくとも一部を除去し、 (L)該低圧塔から該凝縮された第2の酸素富化分画の
少なくとも一部を取り出し、 (M)該取り出された酸素富化分画の少なくとも一部を
該低圧塔の該頂部凝縮器に導入し、 (N)該低圧塔内の該上昇する第2の窒素富化分画の少
なくとも一部を用いた間接熱交換により該頂部凝縮器に
おいて該第2の酸素富化分画の少なくとも一部を気化し
てそれにより該第2の窒素富化分画を凝縮させ、該低圧
塔用の還流を提供し、並びに (O)該頂部凝縮器から廃棄物として該気化された第2
の酸素富化分画の少なくとも一部を取り出すことを具備
する空気から窒素を製造する方法。(5) (A) cooled substantially free of moisture and impurities;
dividing the compressed inlet air into a first inlet air fraction and a second inlet air fraction; (B) introducing the first inlet air fraction into a high pressure column with a top condenser; (C ) separating the first introduced air fraction in the high pressure column into a first nitrogen-enriched fraction and a first oxygen-enriched fraction by cryogenic distillation; (E) removing at least a portion of the first oxygen-enriched fraction from a second oxygen-enriched fraction;
(F) into a low pressure column equipped with a bottom condenser/reboiler and a top evaporator/condenser for cryogenic separation into a nitrogen-enriched fraction and a second oxygen-enriched fraction; (G) introducing a second introduced air fraction into the condenser/reboiler of the low pressure column; condensing an inlet air fraction thereby vaporizing at least a portion of the second oxygen-enriched fraction; (H) transferring at least a portion of the condensed second inlet air fraction to the high pressure column; (I) condensing the second in the top condenser of the high pressure column by indirect heat exchange with at least a portion of the first nitrogen-enriched fraction in the high pressure column; (J) vaporizing at least a portion of the first oxygen-enriched fraction into a second nitrogen-enriched fraction and a second oxygen-enriched fraction; the second nitrogen-enriched fraction vaporized by indirect heat exchange contact with the first nitrogen-enriched fraction in the top condenser of the high pressure column for the cryogenic separation of
(K) removing at least a portion of the second nitrogen-enriched fraction as a product from the low pressure column; (L) removing at least a portion of the second nitrogen-enriched fraction as a product from the low pressure column; (M) introducing at least a portion of the removed oxygen-enriched fraction into the top condenser of the low pressure column; N) vaporizing at least a portion of the second oxygen-enriched fraction in the top condenser by indirect heat exchange with at least a portion of the ascending second nitrogen-enriched fraction in the lower pressure column; (O) thereby condensing the second nitrogen-enriched fraction and providing reflux for the lower pressure column, and (O) discharging the vaporized second fraction as waste from the top condenser.
A method of producing nitrogen from air comprising removing at least a portion of an oxygen-enriched fraction of.
第1の窒素富化分画の少なくとも一部を取り出すことを
さらに具備する請求項5記載の方法。6. The method of claim 5, further comprising: (6) removing at least a portion of the condensed first nitrogen-enriched fraction from the high pressure column as a high pressure nitrogen product.
少なくとも一部を取り出し、および該取り出され凝縮さ
れた第1の窒素富化分画の少なくとも一部を該低圧塔に
導入することをさらに具備する請求項5記載の方法。(7) removing at least a portion of the condensed first nitrogen-enriched fraction from the high pressure column; and transferring at least a portion of the removed and condensed first nitrogen-enriched fraction to the low pressure column. 6. The method of claim 5, further comprising introducing.
らに分け、 該第3の導入空気分画の少なくとも一部を膨張して冷却
し、および 該膨張された導入空気分画の少なくとも一部を該低圧塔
に導入することをさらに具備する請求項5記載の方法。(8) further dividing the compressed inlet air into a third inlet air fraction, expanding and cooling at least a portion of the third inlet air fraction, and 6. The method of claim 5 further comprising introducing at least a portion into the low pressure column.
くとも一部を膨張することをさらに具備する請求項6記
載の方法。7. The method of claim 6, further comprising: (9) expanding at least a portion of the waste oxygen removed from the top condenser.
成物の少なくとも一部を膨張することをさらに具備する
請求項6記載の方法。7. The method of claim 6, further comprising: (10) expanding at least a portion of the high pressure nitrogen product prior to discharging the low pressure nitrogen product.
により該導入空気を冷却し、 該導入空気を圧縮して約2バール〜約20バールの範囲
の高圧塔における圧力を提供することをさらに具備する
請求項5記載の方法。(11) cooling the inlet air by indirect heat exchange in contact with waste and product Kiryu, and compressing the inlet air to provide a pressure in the high pressure column in the range of about 2 bar to about 20 bar; 6. The method of claim 5, comprising:
高圧塔の下半分に導入され、および工程(D)における
該第1の酸素富化分画が該高圧塔の基底部から取り出さ
れる請求項5載の方法。(12) the first introduced air fraction in step (B) is introduced into the lower half of the high pressure column, and the first oxygen enriched fraction in step (D) is introduced from the base of the high pressure column; 6. The method of claim 5, wherein
の下半分に導入され、および 工程(N)の該第2の酸素富化分画が該低圧塔の基底部
から取り出される請求項5記載の方法。(13) the first oxygen-enriched fraction of step (E) is introduced into the bottom half of the low pressure column, and the second oxygen-enriched fraction of step (N) is introduced into the bottom half of the low pressure column; 6. The method of claim 5, taken from.
キスパンダーに通して冷却し、および導入空気との間接
熱交換接触により該ターボエキスパンダーからの該冷却
された廃棄酸素を暖め、それにより導入空気が冷却され
ることをさらに具備する請求項5記載の方法。(14) cooling the waste oxygen obtained in step 0 through a turboexpander and warming the cooled waste oxygen from the turboexpander by indirect heat exchange contact with the inlet air, such that the inlet air 6. The method of claim 5, further comprising cooling.
よる第1の窒素富化分画および第1の酸素富化分画への
極低温分離のための頂部塔凝縮器を備えた第1の蒸留塔
と、 該第2の蒸留塔の該底部塔再沸器および該第1の蒸留塔
の該頂部塔凝縮器をへた循環の後の、該第1の蒸留塔か
ら得られた該第1の酸素富化分画の少なくとも一部と共
に冷却され圧縮された導入空気の少なくとも一部の精密
による、第2の酸素富化分画および第2の窒素富化分画
への分離のための頂部塔凝縮器および底部塔再沸器を備
えた第2の蒸留塔と、液体および蒸気の導入および取り
出しのための該第1のおよび該第2の蒸留塔内の導管手
段と、 液体および蒸気の導入および取り出しのために該第1の
および該第2の蒸留塔間を連通する導管手段と、 冷却され圧縮された導入空気の導入のために該第2の蒸
留塔の該底部塔再沸器と連通する導管手段と、 該第2の蒸留塔における該再沸器からの凝縮された導入
空気の該第1の蒸留塔における該頂部塔凝縮器への輸送
のために、該第2の蒸留塔の該底部塔再沸器と該第1の
蒸留塔の該頂部塔凝縮器とを連通する導管手段と、 該第1の蒸留塔の該頂部塔凝縮器からの気化された空気
の取り出しおよび極低温分離用の該第2の蒸留塔への導
入のために、該第1の蒸留塔の該頂部塔凝縮器と該第2
の蒸留塔とを連通する導管手段と、並びに 該第1の蒸留塔からの該第1の酸素富化分画の少なくと
も一部の取り出しおよび極低温分離用の該第2の蒸留塔
への導入のために、該第1の蒸留塔と該第2の蒸留塔と
を連通する導管手段とを具備する冷却され圧縮された空
気から窒素を製造する装置。(15) a top column condenser for cryogenic separation by rectification of a portion of the cooled compressed inlet air into a first nitrogen-enriched fraction and a first oxygen-enriched fraction; obtained from the first distillation column after circulation through the first distillation column, the bottom column reboiler of the second distillation column and the top column condenser of the first distillation column. separation into a second oxygen-enriched fraction and a second nitrogen-enriched fraction by precision of at least a portion of the cooled and compressed introduced air together with at least a portion of the first oxygen-enriched fraction; a second distillation column with a top column condenser and a bottom column reboiler for and conduit means in the first and second distillation columns for the introduction and withdrawal of liquid and vapor; conduit means communicating between the first and second distillation columns for the introduction and withdrawal of liquid and vapor; and the bottom of the second distillation column for the introduction of cooled and compressed inlet air. conduit means in communication with a column reboiler, for transporting condensed inlet air from the reboiler in the second distillation column to the top column condenser in the first distillation column; conduit means communicating the bottom column reboiler of the second distillation column with the top column condenser of the first distillation column; the top column condenser of the first distillation column and the second distillation column for removal of air and introduction into the second distillation column for cryogenic separation;
conduit means in communication with a distillation column and the removal of at least a portion of the first oxygen-enriched fraction from the first distillation column and introduction into the second distillation column for cryogenic separation; apparatus for producing nitrogen from cooled compressed air, comprising conduit means communicating said first distillation column and said second distillation column.
しおよび該第2の蒸留塔の該頂部塔凝縮器への導入によ
り該第2の蒸留塔内で上昇する蒸気を用いた間接熱交換
を提供するために、該第2の蒸留塔と該第2の蒸留塔の
該頂部塔凝縮器とを連通する導管手段と、 廃棄物としての該第2の酸素富化分画の取り出しのため
に、該第2の蒸留塔の該頂部塔凝縮器と連通する導管手
段と、 該第1の蒸留塔からの該第1の窒素富化分画の取り出し
および該第2の蒸留塔への導入で該第2の蒸留塔用の還
流を提供するために、該第1の蒸留塔と該第2の蒸留塔
とを連通する導管手段とをさらに具備する請求項15記
載の装置。(16) using the vapor rising in the second distillation column by removing the oxygen-enriched fraction from the second distillation column and introducing it into the top column condenser of the second distillation column; conduit means communicating the second distillation column with the top column condenser of the second distillation column to provide indirect heat exchange; conduit means communicating with the top column condenser of the second distillation column for removal of the first nitrogen-enriched fraction from the first distillation column and the second distillation column; 16. The apparatus of claim 15, further comprising conduit means communicating said first distillation column and said second distillation column to provide reflux for said second distillation column upon introduction to said second distillation column.
圧縮手段により圧縮された空気から二酸化炭素、水、お
よび他の不純物を除去する精密手段と、 該精密手段からの圧縮された空気を極低温に冷却する熱
交換手段と、 液体および蒸気の導入および取り出しのために、該第2
の蒸留塔の該頂部塔凝縮器と連通する導管手段と、 冷却され圧縮された導入空気の導入のために、該熱交換
器並びに該第1の蒸留塔および該第2の蒸留塔を連通す
る導管手段とをさらに具備する請求項16記載の装置。(17) compression means for compressing air from an external source; precision means for removing carbon dioxide, water, and other impurities from the air compressed by the air compression means; and precision means for removing the compressed air from the precision means. heat exchange means for cooling to cryogenic temperatures, and said second
conduit means communicating with the top column condenser of the distillation column; and communicating with the heat exchanger and the first distillation column and the second distillation column for the introduction of cooled and compressed inlet air. 17. The apparatus of claim 16, further comprising conduit means.
と該熱交換手段とを連通する導管手段をさらに具備する
請求項15記載の装置。18. The apparatus of claim 15 further comprising conduit means communicating said first distillation column and said heat exchange means for removal of nitrogen product.
ための該導管手段に連通する膨張手段をさらに具備する
請求項18記載の装置。19. The apparatus of claim 18 further comprising expansion means communicating with said conduit means for expanding and cooling at least a portion of the nitrogen product.
備する請求項15記載の装置。20. The apparatus of claim 15, further comprising expansion means for expansion of the oxygen waste.
れ圧縮された空気を膨脹するための膨張手段をさらに具
備する請求項15記載の装置。(21) The apparatus according to claim 15, further comprising expansion means for expanding the cooled and compressed air before it is introduced into the second distillation column and cooled.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/US1989/003926 WO1993013373A1 (en) | 1989-09-12 | 1989-09-12 | Cryogenic air separation process and apparatus |
US89/03926 | 1989-09-12 |
Publications (1)
Publication Number | Publication Date |
---|---|
JPH03170785A true JPH03170785A (en) | 1991-07-24 |
Family
ID=22215224
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP2241040A Pending JPH03170785A (en) | 1989-09-12 | 1990-09-11 | Extremely low temperature air separation and its apparatus |
Country Status (10)
Country | Link |
---|---|
EP (1) | EP0418139B1 (en) |
JP (1) | JPH03170785A (en) |
CN (1) | CN1050260A (en) |
AU (1) | AU643232B2 (en) |
CA (1) | CA2025013A1 (en) |
DE (1) | DE69004647T2 (en) |
ES (1) | ES2046740T3 (en) |
RU (1) | RU2069293C1 (en) |
WO (1) | WO1993013373A1 (en) |
ZA (1) | ZA907188B (en) |
Families Citing this family (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5396269A (en) * | 1991-02-20 | 1995-03-07 | Hitachi, Ltd. | Television telephone |
US5257504A (en) * | 1992-02-18 | 1993-11-02 | Air Products And Chemicals, Inc. | Multiple reboiler, double column, elevated pressure air separation cycles and their integration with gas turbines |
US5251451A (en) * | 1992-08-28 | 1993-10-12 | Air Products And Chemicals, Inc. | Multiple reboiler, double column, air boosted, elevated pressure air separation cycle and its integration with gas turbines |
US5251450A (en) * | 1992-08-28 | 1993-10-12 | Air Products And Chemicals, Inc. | Efficient single column air separation cycle and its integration with gas turbines |
DE19819263C2 (en) * | 1998-04-30 | 2003-08-21 | Linde Ag | Process and device for the production of pressurized nitrogen |
EP2312247A1 (en) * | 2009-10-09 | 2011-04-20 | Linde AG | Method and device for generating liquid nitrogen from low temperature air separation |
EP3159648B1 (en) * | 2015-10-20 | 2018-09-19 | Linde Aktiengesellschaft | Plate heat exchanger capacitor evaporator and method for cryogenic decomposition of air |
WO2020074120A1 (en) * | 2018-10-09 | 2020-04-16 | Linde Aktiengesellschaft | Method for obtaining one or more air products and air separation system |
CN109297260A (en) * | 2018-10-17 | 2019-02-01 | 浙江海天气体有限公司 | A kind of full nitrogen space division waste gas recovering device processed |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AU523019B2 (en) * | 1978-05-25 | 1982-07-08 | Commonwealth Industrial Gases Limited, The | Separation of air |
JPS58198677A (en) * | 1982-05-14 | 1983-11-18 | 株式会社日立製作所 | Method and device for separating air |
US4582518A (en) * | 1984-09-26 | 1986-04-15 | Erickson Donald C | Nitrogen production by low energy distillation |
US4707994A (en) * | 1986-03-10 | 1987-11-24 | Air Products And Chemicals, Inc. | Gas separation process with single distillation column |
GB8800842D0 (en) * | 1988-01-14 | 1988-02-17 | Boc Group Plc | Air separation |
-
1989
- 1989-09-12 WO PCT/US1989/003926 patent/WO1993013373A1/en unknown
-
1990
- 1990-09-10 ZA ZA907188A patent/ZA907188B/en unknown
- 1990-09-10 CA CA002025013A patent/CA2025013A1/en not_active Abandoned
- 1990-09-11 ES ES199090402488T patent/ES2046740T3/en not_active Expired - Lifetime
- 1990-09-11 JP JP2241040A patent/JPH03170785A/en active Pending
- 1990-09-11 EP EP90402488A patent/EP0418139B1/en not_active Expired - Lifetime
- 1990-09-11 CN CN90107623A patent/CN1050260A/en active Pending
- 1990-09-11 DE DE90402488T patent/DE69004647T2/en not_active Expired - Fee Related
- 1990-09-11 RU SU904830924A patent/RU2069293C1/en active
- 1990-09-11 AU AU62375/90A patent/AU643232B2/en not_active Ceased
Also Published As
Publication number | Publication date |
---|---|
DE69004647D1 (en) | 1993-12-23 |
EP0418139B1 (en) | 1993-11-18 |
CN1050260A (en) | 1991-03-27 |
RU2069293C1 (en) | 1996-11-20 |
DE69004647T2 (en) | 1994-03-10 |
ZA907188B (en) | 1991-09-25 |
EP0418139A1 (en) | 1991-03-20 |
WO1993013373A1 (en) | 1993-07-08 |
AU643232B2 (en) | 1993-11-11 |
CA2025013A1 (en) | 1991-03-13 |
AU6237590A (en) | 1991-03-21 |
ES2046740T3 (en) | 1994-02-01 |
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