JPS6237675A - Nitrogen generator - Google Patents
Nitrogen generatorInfo
- Publication number
- JPS6237675A JPS6237675A JP60178273A JP17827385A JPS6237675A JP S6237675 A JPS6237675 A JP S6237675A JP 60178273 A JP60178273 A JP 60178273A JP 17827385 A JP17827385 A JP 17827385A JP S6237675 A JPS6237675 A JP S6237675A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- expansion turbine
- blower
- heat exchanger
- nitrogen
- 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
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims description 54
- 229910052757 nitrogen Inorganic materials 0.000 title claims description 27
- 239000007789 gas Substances 0.000 claims description 28
- 238000001816 cooling Methods 0.000 claims description 9
- 238000005057 refrigeration Methods 0.000 claims description 9
- 238000004887 air purification Methods 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 3
- 238000000034 method Methods 0.000 description 10
- 239000007788 liquid Substances 0.000 description 8
- 239000002912 waste gas Substances 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000010992 reflux Methods 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
- F25J3/044—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 single pressure main column system only
-
- 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
-
- 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
-
- 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
- F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen enriched compared to air, e.g. "crude oxygen"
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
鼠１五旦机朋立託
本発明は、新規寒冷発生装置を有する空気の低温分離に
よる窒素発生装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a nitrogen generation device by low-temperature separation of air having a novel cold generation device.
従来の技術
従来の低温分離による窒素発生装置のフローシートを第
１図に示す。第１図において窒素発生装置は、（ａ）原
料空気圧縮工程、並びに保冷箱に収容された（ｂ）原料
空気精製・冷却工程、（ｃ）精留工程および（ｄ）寒冷
発生工程からなる。BACKGROUND OF THE INVENTION A flow sheet of a conventional nitrogen generator using low-temperature separation is shown in FIG. In FIG. 1, the nitrogen generator consists of (a) a raw air compression process, (b) a raw air purification/cooling process housed in a cold box, (c) a rectification process, and (d) a cold generation process.
（ａ）原料空気圧縮工程
原料空気をエアフィルタ（１）を介し原料空気圧縮機（
２）により所要の圧力（製品窒素の圧力士熱交換器、精
留塔、配管の圧力損失）まで圧縮して保冷箱（３）中の
原料空気精製・冷却工程に供給する。(a) Raw air compression process Raw air is passed through the air filter (1) to the raw air compressor (
2), the compressed air is compressed to the required pressure (pressure loss in the product nitrogen pressure exchanger, rectification tower, and piping) and supplied to the raw air refining/cooling process in the cold storage box (3).
（ｂ）原料空気精製・冷却工程
原料空気は切替弁（４）を介してリバーシング熱交換器
（５）に供給され、製品ガス窒素およびチェックバルブ
ボックス（６）からの戻り廃ガスと熱交換を行ない液化
点（約−１７０℃）に近い温度まで冷却される。この冷
却工程において原料空気中の水分および炭酸ガスは該リ
バーシング熱交換器（５）の流路内に凝結析出して除去
され、ついで原料空気は精留塔（７）下部へ供給される
。(b) Raw air purification/cooling process The raw air is supplied to the reversing heat exchanger (5) via the switching valve (4), where it exchanges heat with the product gas nitrogen and the return waste gas from the check valve box (6). It is cooled to a temperature close to the liquefaction point (approximately -170°C). In this cooling process, moisture and carbon dioxide in the feed air are removed by condensation and precipitation in the flow path of the reversing heat exchanger (5), and then the feed air is supplied to the lower part of the rectification column (7).
（ｃ）精留工程
精留塔（７）に入った空気は、窒素と、酸素３０％程度
の液体空気とに分離され、窒素は精留塔上部より抜き出
され液化器（９）、リバーシング熱交換器（５）を通っ
て、製品窒素として取り出される。一方、液体空気は、
精留塔（７）底部より抜き出され、膨張弁を経て膨張し
、精留塔頂部の窒素温度より低温にて主蒸化器部（８）
に供給される。(c) Rectification process The air that enters the rectifier (7) is separated into nitrogen and liquid air containing about 30% oxygen. The nitrogen is extracted from the top of the rectifier and sent to the liquefier (9), It passes through a singe heat exchanger (5) and is removed as product nitrogen. On the other hand, liquid air
It is extracted from the bottom of the rectification column (7), expanded through an expansion valve, and then transferred to the main evaporator section (8) at a temperature lower than the nitrogen temperature at the top of the rectification column.
is supplied to
精留塔頂部のガス窒素は該主蒸化器部にて熱交換により
、凝縮して精留塔の還流液となり、液体空気は蒸発して
主蒸化器部より出る。主蒸化器部で蒸発した液体空気の
一部は液化器（９）を経てリバーシング熱交換器（５）
で原料空気と熱交換を行ない昇温された後、寒冷発生工
程に送られる。 （ｄ）寒冷発生工程
リバーシング熱交換器（５）で昇温された主蒸化器部（
８）で蒸発したガスは膨張タービン（１０）により大気
圧近くまで断熱膨張し寒冷を発生する。Gaseous nitrogen at the top of the rectification column is condensed through heat exchange in the main evaporator section to become a reflux liquid of the rectification column, and liquid air is evaporated and exits from the main evaporator section. A part of the liquid air evaporated in the main evaporator section passes through the liquefier (9) to the reversing heat exchanger (5).
After exchanging heat with the raw air and raising its temperature, it is sent to the cooling generation process. (d) Cold generation process The main evaporator section heated by the reversing heat exchanger (5) (
The gas evaporated in step 8) is adiabatically expanded to near atmospheric pressure by the expansion turbine (10) and generates cold.
膨張タービン（１０）を出たガスは、主蒸化器部で蒸発
し、リバーシング熱交換器、膨張タービンをバイパスし
膨張弁（１１）で膨張したガスととらにリバーシング
熱交換器（５）を通り、廃ガスとして系外に放出ずろ。The gas leaving the expansion turbine (10) is evaporated in the main evaporator, bypasses the reversing heat exchanger and the expansion turbine, and is combined with the gas expanded in the expansion valve (11) to the reversing heat exchanger (5). ) and be released outside the system as waste gas.
発明が解決しようとする問題点
寒冷発生源である膨張タービンを通るガスは、主蒸化器
部で蒸発した液体空気である。しかしこの主蒸化器は、
例えば製品窒素圧力が８ｋｇ／ｃｒ！２Ｇのときは主蒸
化器部の圧力を約５ ｋｇ／ｃｍ” Ｇ、製品窒素圧力
が６ ｋｇ／ｃｍ” Ｇのときは主蒸化器部の圧力を約
３ 、５ ｋｇ／ｃ１１’ Ｇと下げなければ熱交換が
行なわれない。このような製品窒素圧力の低い場合には
、主蒸化器部の圧力が低下し、膨張タービンの入口圧力
が低下する。このため膨張タービンの膨張比が小さくな
り、膨張タービンのガス流量を増加しないと窒素発生装
置に必要な寒冷の発生が不可能となる。しかし、なから
、膨張タービンに供給可能なガスは、主蒸化器部におい
て液体空気が蒸発して生じたガスに限られるため、必要
な寒冷を得るには製品窒素生産量と精留条件によって決
定されろ空気量以」二に原料空気量を増加して廃ガスｍ
を増加さ什て」転を行なうことが必要となり経済的に好
ましくない。Problem to be Solved by the Invention The gas passing through the expansion turbine, which is the source of refrigeration, is liquid air that has been evaporated in the main evaporator section. However, this main evaporator
For example, the product nitrogen pressure is 8kg/cr! When the pressure is 2G, the pressure in the main evaporator section is approximately 5 kg/cm"G, and when the product nitrogen pressure is 6 kg/cm"G, the pressure in the main evaporator section is approximately 3.5 kg/c11'G. Heat exchange will not take place unless the temperature is lowered. When the product nitrogen pressure is low, the pressure in the main evaporator section decreases, and the inlet pressure of the expansion turbine decreases. Therefore, the expansion ratio of the expansion turbine becomes small, and unless the gas flow rate of the expansion turbine is increased, it becomes impossible to generate the refrigeration necessary for the nitrogen generator. However, the gas that can be supplied to the expansion turbine is limited to the gas produced by evaporation of liquid air in the main evaporator section, so obtaining the necessary refrigeration depends on the product nitrogen production volume and rectification conditions. Second, increase the amount of feed air to reduce the amount of waste gas m.
This is economically undesirable as it would be necessary to increase
また、製品として液体窒素を多くとる窒素製造装置では
必要とする寒冷発生量が多いため、膨張タービンの流量
をふやさなければならず、前記と同様に廃ガス量が不足
する。したがって、製品窒素圧力の低い場合と同様、原
料空気量を増加して廃ガス量の増加をはかる必要があり
不経済であった。In addition, since a nitrogen production apparatus that produces a large amount of liquid nitrogen as a product requires a large amount of cold generation, the flow rate of the expansion turbine must be increased, resulting in an insufficient amount of waste gas as described above. Therefore, as in the case where the product nitrogen pressure is low, it is necessary to increase the amount of raw air to increase the amount of waste gas, which is uneconomical.
問題を解決するための手段
本発明者らは、前記問題点に鑑み、経済的な運転の可能
な窒素製造装置を得るべく種々検討を重ねた結果、本発
明を完成するに至った。Means for Solving the Problems In view of the above-mentioned problems, the inventors of the present invention have conducted various studies in order to obtain a nitrogen production apparatus that can be operated economically, and as a result, they have completed the present invention.
本発明は、原料空気圧縮装置、リバーシング熱交換器を
有する原料空気精製・冷却装置、精留装置および膨張タ
ービンを有する寒冷発生装置を含む窒素発生装置におい
て、該寒冷発生装置の膨張タービンへ供給されるガスの
経路内に、前記膨張タービンにより駆動されかつ該ガス
を加圧するブロワー、および該ブロワ−にて加熱後冷却
された膨張タービン行きガスにより該ブロワ−への供給
ガスを加熱するタービン熱交換器を配置したことを特徴
とずろ窒素発生装置を提供ずろらのである。The present invention provides a nitrogen generation device including a feed air compression device, a feed air purification/cooling device having a reversing heat exchanger, a rectification device, and a refrigeration generation device having an expansion turbine, in which supply is provided to the expansion turbine of the refrigeration generation device. A blower that is driven by the expansion turbine and pressurizes the gas is placed in the path of the gas, and a turbine heat source that heats the gas supplied to the blower by the expansion turbine-bound gas that is heated and cooled by the blower. Zurora's nitrogen generator is characterized by the arrangement of an exchanger.
すなわち、膨張タービンは、ガスを断熱膨張させ、エネ
ルギーを外部にとり出すことによってガスを冷却する。That is, the expansion turbine cools the gas by adiabatically expanding the gas and extracting energy to the outside.
この外部にとり出されたエネルギーは従来、大気を吸い
込み、タービンに直結したブロワ−（１２）にて大気を
加圧することに使われている（ブロワ−を出たガスは、
再び大気に戻される）。これに対し本発明では、先の主
蒸化器部で蒸発したガスをリバーシング熱交換器で昇温
したのち、タービン熱交換器にて常温まで昇温し、これ
を膨張タービンによって外部に取り出されたエネルギー
、すなわち該タービンに直結したブロワ−を用いて加圧
し、ついてタービン熱交換器で冷却した後、膨張タービ
ンにて膨張を行う。Conventionally, this energy extracted externally is used to draw in atmospheric air and pressurize it with a blower (12) directly connected to the turbine (the gas exiting the blower is
(returned to the atmosphere). In contrast, in the present invention, the temperature of the gas evaporated in the main evaporator section is raised in the reversing heat exchanger, then the temperature is raised to room temperature in the turbine heat exchanger, and then taken out to the outside by the expansion turbine. It is pressurized using the generated energy, that is, a blower directly connected to the turbine, and then cooled by a turbine heat exchanger, and then expanded by an expansion turbine.
つぎに本発明を図面にもとづき更に詳しく説明する。第
２図は本発明の窒素製造装置の一具体例を示すフローシ
ートである。第２図において、本発明の装置は、前記従
来装置と同様の（ａ）原料空気圧縮装置、（ｂ）原料空
気精製・冷却装置および（Ｃ）精留装置、ならびにガス
を加圧するブロワ−を有する（ｄ）寒冷装置を含む。Next, the present invention will be explained in more detail based on the drawings. FIG. 2 is a flow sheet showing a specific example of the nitrogen production apparatus of the present invention. In FIG. 2, the apparatus of the present invention includes (a) a raw air compression device, (b) a raw air purification/cooling device, and (C) a rectification device, as well as a blower for pressurizing gas, as in the conventional device. (d) including a refrigeration device.
該寒冷発生装置は、精留塔（７）の主蒸化器（８）で蒸
発１．たガスをリバーシング熱交換器（５）で原料空気
との熱交換により昇温（−９０℃旧後）した後、さらに
タービン熱交換器（１３）により常温付近まで昇温する
。ついで該ガスは膨張タービン（１０）にて駆動される
ブロワ−（１４）にて圧縮されて昇圧したのち、ブロワ
−後方冷却器（１５）にて冷却され、さらに面記タービ
ン熱交換器（１３）にてブロワ−（１４）へ向かうガス
と熱交換して、７ｍ度低下し、膨張タービン（１０）へ
供給される。The refrigeration generating device performs evaporation 1. After the gas is heated by heat exchange with raw air in a reversing heat exchanger (5) (to around -90° C.), the temperature is further raised to around room temperature in a turbine heat exchanger (13). Next, the gas is compressed and pressurized in a blower (14) driven by an expansion turbine (10), cooled in a blower back cooler (15), and further passed through a surface turbine heat exchanger (13). ), it exchanges heat with the gas heading for the blower (14), is cooled by 7 m degrees, and is supplied to the expansion turbine (10).
つぎにかかる加圧されたガスは膨張タービン（１０）に
より大気圧近くまで断熱膨張させろことにより寒冷を発
生する。膨張タービン（１０）から出たガスは前記の従
来装置における寒冷工程と同様、主蒸化器部で蒸発し、
リバーシング熱交換器、膨張タービンをバイパスし膨張
弁（１１）で膨張したガスとともにリバーシング熱交換
器（５）を通って廃ガスとして系外に放出される。The pressurized gas is then adiabatically expanded to near atmospheric pressure by an expansion turbine (10), thereby generating refrigeration. The gas coming out of the expansion turbine (10) is evaporated in the main evaporator section, similar to the cooling process in the conventional device described above,
The gas bypasses the reversing heat exchanger and the expansion turbine, passes through the reversing heat exchanger (5) together with the gas expanded by the expansion valve (11), and is discharged to the outside of the system as waste gas.
発明の効果
本発明によれば、膨張タービンの入口圧力が上昇し、膨
張タービンの膨張比が大きくなるため膨張タービンのガ
ス流量を低減させることができ、ひいては原料空気流量
を精留条件のみにより決定される値まで減少することが
できろ。したがって従来方法で問題となっていた廃ガス
の不足が解消され、余分な空気を圧縮する必要がなくな
り、経済的な運転が可能となった。Effects of the Invention According to the present invention, the inlet pressure of the expansion turbine increases and the expansion ratio of the expansion turbine increases, so the gas flow rate of the expansion turbine can be reduced, and the raw material air flow rate is determined only by the rectification conditions. can be reduced to the value given. Therefore, the lack of waste gas that had been a problem with the conventional method was resolved, and there was no need to compress excess air, making economical operation possible.
第１図は従来の窒素製造装置のフローシート、第２図は
本発明の窒素製造装置の一具体例を示すフローシートで
ある。
図中の主な符号はっぎのとおりである。
２：圧縮機、３：保冷箱、５・リバーシング熱交換器、
７：精留塔、ＩＯ膨張タービン、１２゜１４ニブロワー
。FIG. 1 is a flow sheet of a conventional nitrogen production apparatus, and FIG. 2 is a flow sheet showing a specific example of the nitrogen production apparatus of the present invention. The main symbols in the figure are as shown. 2: Compressor, 3: Cold box, 5. Reversing heat exchanger,
7: Rectification column, IO expansion turbine, 12°14 nib blower.
Claims (1)
る原料空気精製・冷却装置、精留装置および膨張タービ
ンを有する寒冷発生装置を含む窒素発生装置において、
該寒冷発生装置の膨張タービンへ供給されるガスの経路
内に、前記膨張タービンにより駆動されかつ該ガスを加
圧するブロワー、および該ブロワーにて加熱後冷却され
た膨張タービン行きガスにより該ブロワーへの供給ガス
を加熱するタービン熱交換器を配置したことを特徴とす
る窒素発生装置。(1) In a nitrogen generator including a feed air compression device, a feed air purification/cooling device having a reversing heat exchanger, a rectification device and a refrigeration generator having an expansion turbine,
A blower that is driven by the expansion turbine and pressurizes the gas is provided in the path of the gas supplied to the expansion turbine of the cold generation device, and a blower that is heated and cooled by the blower and is directed to the expansion turbine is supplied to the blower. A nitrogen generator characterized by having a turbine heat exchanger arranged to heat supplied gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60178273A JPS6237675A (en) | 1985-08-12 | 1985-08-12 | Nitrogen generator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60178273A JPS6237675A (en) | 1985-08-12 | 1985-08-12 | Nitrogen generator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6237675A true JPS6237675A (en) | 1987-02-18 |
Family
ID=16045588
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60178273A Pending JPS6237675A (en) | 1985-08-12 | 1985-08-12 | Nitrogen generator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6237675A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03137484A (en) * | 1989-08-11 | 1991-06-12 | Boc Group Inc:The | Process of manufacturing nitrogen from air and its device |
| WO2022179748A1 (en) * | 2021-02-25 | 2022-09-01 | Linde Gmbh | Process and plant for providing compressed nitrogen |
-
1985
- 1985-08-12 JP JP60178273A patent/JPS6237675A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03137484A (en) * | 1989-08-11 | 1991-06-12 | Boc Group Inc:The | Process of manufacturing nitrogen from air and its device |
| WO2022179748A1 (en) * | 2021-02-25 | 2022-09-01 | Linde Gmbh | Process and plant for providing compressed nitrogen |
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