JPS5825953B2 - Exhaust air system - Google Patents
Exhaust air systemInfo
- Publication number
- JPS5825953B2 JPS5825953B2 JP50092924A JP9292475A JPS5825953B2 JP S5825953 B2 JPS5825953 B2 JP S5825953B2 JP 50092924 A JP50092924 A JP 50092924A JP 9292475 A JP9292475 A JP 9292475A JP S5825953 B2 JPS5825953 B2 JP S5825953B2
- Authority
- JP
- Japan
- Prior art keywords
- air
- flow path
- natural gas
- liquefied natural
- solidification
- 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
Links
- 239000007788 liquid Substances 0.000 claims description 26
- 239000003949 liquefied natural gas Substances 0.000 claims description 25
- 238000000034 method Methods 0.000 claims description 17
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 238000007711 solidification Methods 0.000 claims description 11
- 230000008023 solidification Effects 0.000 claims description 11
- 238000003860 storage Methods 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000007906 compression Methods 0.000 claims description 6
- 238000005057 refrigeration Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 9
- 239000007789 gas Substances 0.000 description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 238000001514 detection method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000013611 frozen food Nutrition 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000002699 waste material 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
- F25J1/0224—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration loop
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
-
- 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
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/40—Separating high boiling, i.e. less volatile components from air, e.g. CO2, hydrocarbons
-
- 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
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
-
- 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
- F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
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)
Description
【発明の詳細な説明】
本発明は液化天然ガスの寒冷を利用して液体空気を製造
する方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for producing liquid air by utilizing the refrigeration of liquefied natural gas.
近年液化天然ガスが都市ガス、火力発電等に大量に用い
られる様になったが、使用に際しては海水等によって再
気化しているためその寒冷は殆ど利用されずに無駄にさ
れている。In recent years, liquefied natural gas has come to be used in large quantities for city gas, thermal power generation, etc., but when it is used, it is re-vaporized by seawater etc., so the cold water is hardly used and is wasted.
液体空気は冷凍食品、冷凍倉庫、冷凍輸送、低温破砕お
よび粉砕、冷凍土木工事等に大量使用が見込まれ、また
病院、大集会場、工場等の空調用、更に将来実現が予想
されている各種の大規模な新産業分野に於ける寒冷供給
源として大量需要が見込まれている。Liquid air is expected to be used in large quantities for frozen foods, frozen warehouses, frozen transportation, cryogenic crushing and pulverization, frozen civil engineering work, etc., as well as for air conditioning in hospitals, large gathering halls, factories, etc., and various other applications that are expected to be realized in the future. Large-scale demand is expected as a source of refrigeration for large-scale new industrial fields.
最も普遍的且つ大量に存在する空気によって寒冷を貯溜
し得ること、放出しても無害安全であることも液体空気
を利用して上記用途に大量需要が見込まれる理由であり
、従って安価な液体空気が製造され供給されればその需
要は急激に伸びると予想される。The fact that air can store cold air, which is the most universal and abundant, and that it is harmless and safe even when released, is another reason why liquid air is expected to be used in large quantities for the above applications. Once manufactured and supplied, demand is expected to increase rapidly.
しかし従来液化天然ガスの寒冷を利用した液体空気製造
装置は実際稼動している例が無い。However, there are no examples of conventional liquid air production equipment that utilizes the refrigeration of liquefied natural gas actually operating.
本発明の目的は上記の要求に従い、液化天然ガスの寒冷
を利用して安価な液体空気を製造する方法に関し、その
製造工程を精製工程、低温圧縮工程および液化工程の３
工程より構成し、該工程のいづれに於ても液化天然ガス
の寒冷を利用することにより極めて効率よく且つ経済的
に液体空気を得るプロセスを提供することにある。In accordance with the above-mentioned requirements, the object of the present invention is to provide a method for producing inexpensive liquid air by utilizing the refrigeration of liquefied natural gas, and to process the production process into three steps: a purification process, a low-temperature compression process, and a liquefaction process.
The object of the present invention is to provide a process for obtaining liquid air extremely efficiently and economically by utilizing the refrigeration of liquefied natural gas in each of the steps.
更に本発明の目的は周期的に切替え使用する対で成る２
個以上の熱交換器群によって原料空気より易凝縮性成分
を凝縮固化分離する方法に関し、上記熱交換器に於て原
料空気と向流して液化天然ガスを流すことにより空気流
路に上記易凝縮性成分を凝縮固化せしめて該成分を分離
し、更に固化分離した該易凝縮性成分を真空排気するこ
とにより効果的に除去し装置外に排出する方法を提供す
ることにある。Furthermore, it is an object of the present invention to provide two
Regarding a method of condensing and solidifying easily condensable components from feed air using a group of two or more heat exchangers, the easily condensable components are caused to flow into the air flow path by flowing liquefied natural gas countercurrently to the feed air in the heat exchanger. It is an object of the present invention to provide a method for condensing and solidifying a highly condensable component, separating the component, and then evacuation of the solidified and separated easily condensable component to effectively remove it and discharge it to the outside of the apparatus.
空気中に含まれる易凝縮性成分は通常型として水分およ
び炭酸ガスであり上記方法はこの両成分を同時に除去す
る場合、あるいは炭酸ガスのみを単独除去する場合、い
づれの場合に於ても適用し得る。The easily condensable components contained in the air are usually water and carbon dioxide gas, and the above method can be applied to both cases where both of these components are removed at the same time, or when only carbon dioxide gas is removed individually. obtain.
また原料ガスが空気に限らずエチレン等の石油分解ガス
あるいはコークス炉ガス等の場合も含有する易凝縮性成
分の除去方法として用いることが出来る。Furthermore, the present invention can be used as a method for removing easily condensable components when the raw material gas is not only air but also petroleum cracked gas such as ethylene or coke oven gas.
以下本発明を図に従って詳細説明する。The present invention will be explained in detail below with reference to the drawings.
管１より導入された原料空気は水分離器２に入って向流
する零度に近い零度以上の一定温度の気化天然ガスに冷
却されてその温度に於ける飽和蒸気圧以上の水分を凝縮
分離して導出する。The raw material air introduced from the pipe 1 enters the water separator 2, where it is cooled by vaporized natural gas at a constant temperature close to zero or above zero, which flows counter-currently, and condenses and separates moisture above the saturated vapor pressure at that temperature. and derive it.
該水分離器によって外気温、湿度の変化による原料空気
中の含有水分は常に一定の蒸気正分の水分のみを含んで
管３より三方切替弁４を経て切り替え使用する対で成る
易凝縮性成分除去熱交換器の一方５ａに導入され向流す
る液化天然ガスに冷却されて約−１５７℃になって導出
する。The moisture content in the raw material air due to changes in outside temperature and humidity is always controlled by the water separator by using a pair of easily condensable components that are switched from the pipe 3 through the three-way switching valve 4, containing only the moisture equivalent to a certain amount of steam. It is introduced into one side 5a of the removal heat exchanger, cooled by the liquefied natural gas flowing countercurrently, and discharged at about -157°C.
この際該易凝縮性成分除去熱交換器５ａの空気流路６ａ
には原料空気中の易凝縮成分即ち主として水分および炭
酸ガスが凝縮固化する。At this time, the air flow path 6a of the easily condensable component removal heat exchanger 5a
In this case, easily condensable components in the feed air, namely mainly water and carbon dioxide gas, condense and solidify.
易凝縮性成分除去熱交換器５ａがこの様に易凝縮成分の
凝縮固化周期にある時効で成る他方の該熱交換器５ｂは
凝縮成分の蒸発除去即ち再生周期にある。The easily condensable component removal heat exchanger 5a is thus aged in the condensation and solidification period of the easily condensable components, while the other heat exchanger 5b is in the evaporation removal or regeneration period of the condensed components.
前周期で該熱交換器５ｂの空気流路６ｂ内に易凝縮成分
の凝縮固化が行われるが、この周期の終りに三方切替弁
４，７．９および１０を切り替えることにより該空気流
路６ｂは凝縮固化周期より蒸発除去周期に切り替えられ
る。In the previous cycle, easily condensable components are condensed and solidified in the air passage 6b of the heat exchanger 5b, and at the end of this cycle, by switching the three-way switching valves 4, 7.9, and 10, the air passage 6b is is switched from the condensation solidification cycle to the evaporation removal cycle.
また同時に液化天然ガス流路の三方切替弁３６゜３９を
切り替えて管３５よりの液化天然ガスを管３７ｂから管
３７ａを経て流路３８ａへ流し、流路３８ｂへの液化天
然ガスは遮断する。At the same time, the three-way switching valves 36 and 39 of the liquefied natural gas flow path are switched to allow the liquefied natural gas from the pipe 35 to flow from the pipe 37b to the flow path 38a via the pipe 37a, and the liquefied natural gas to the flow path 38b is cut off.
蒸発除去周期に入った流路６ｂは加熱器１１、ブロワ−
１２、管１３、加熱器１４、管１５と循環流路を形成し
、該循環流路には弁１６を介して真空ポンプ１７を接続
する。The flow path 6b that has entered the evaporation removal cycle is connected to the heater 11 and the blower.
12, a pipe 13, a heater 14, and a pipe 15 to form a circulation flow path, and a vacuum pump 17 is connected to the circulation flow path via a valve 16.
加熱器１１，１４、循環ブロワ−１２を作動させて、循
環流路内の残溜空気を加温しつつ循環し、流路６ｂ内に
凝縮固化している易凝縮性成分、主として水および炭酸
ガスを該循環空気中に蒸発同伴させ、同時に弁１６を開
は真空ポンプ１７を作動させて循環系統内の空気および
これに含まれる蒸発品凝縮性成分を系外に排出する。The heaters 11, 14 and the circulation blower 12 are operated to heat and circulate the residual air in the circulation channel to remove easily condensable components, mainly water and carbonic acid, which have condensed and solidified in the channel 6b. The gas is evaporated and entrained in the circulating air, and at the same time, the valve 16 is opened and the vacuum pump 17 is operated to discharge the air within the circulation system and the evaporated condensable components contained therein to the outside of the system.
この排出は固化している易凝縮性成分の蒸発に相当する
熱を供給しつつ、また圧力も蒸発を促進する様に徐々に
低下させるので固化成分は短時間に完全に系外に排出す
ることが出来る。This discharge supplies heat equivalent to the evaporation of the solidified easily condensable components, and the pressure is gradually lowered to promote evaporation, so that the solidified components can be completely discharged from the system in a short period of time. I can do it.
上記系統中の加熱器１１，１４は定温加熱器、スチーム
加熱器、電熱器等を適宜使用する。As the heaters 11 and 14 in the above-mentioned system, a constant temperature heater, a steam heater, an electric heater, etc. are appropriately used.
場合によっては配管部分を長くすることにより行う。In some cases, this can be done by lengthening the piping section.
循環ブロワ−１２はスクリュ一式、ターボ式、ルーツ式
等を適宜使用する。As the circulation blower 12, a screw set, a turbo type, a roots type, etc. are appropriately used.
真空ポンプは油回転式が適当である。An oil rotary type vacuum pump is suitable.
これらの容量は熱交換器５ａ 、 ｓｂの容量および切
替時間に応じて決定する。These capacities are determined depending on the capacity and switching time of the heat exchangers 5a and sb.
循環系統中の空気および易凝縮性成分が排出され真空度
が充分高くなった時、熱交換器５ｂは予冷に入る。When air and easily condensable components in the circulation system are exhausted and the degree of vacuum becomes sufficiently high, the heat exchanger 5b enters precooling.
即ち三方切替弁３６，３９を両側開として熱交換器５ａ
の流路３８ａに液化天然ガスを流したまＮ熱交換器５ｂ
の流路３８ｂにも短時間液化天然ガスを導入して該熱交
換器５ｂを冷却する。That is, with the three-way switching valves 36 and 39 open on both sides, the heat exchanger 5a
The liquefied natural gas is passed through the flow path 38a of the N heat exchanger 5b.
Liquefied natural gas is also introduced into the flow path 38b for a short time to cool the heat exchanger 5b.
この冷却に要する液化天然ガスは少量で良い。即ち蒸発
除去周期に於ける易凝縮性成分の蒸発は真空下で行って
いるためこの時の流路６ｂの温度上昇は少なくて良い、
従って熱履歴の巾が小さいためである。Only a small amount of liquefied natural gas is required for this cooling. That is, since the easily condensable components are evaporated in a vacuum during the evaporation removal cycle, the temperature rise in the flow path 6b at this time may be small.
This is because the width of the thermal history is therefore small.
熱交換器５ｂの温度が所定温度迄低下した時、三方切替
弁４，７，９および１０を切り替えまた両側開の三方切
替弁３６．３９の片側を閉じて流路３８ａの液化天然ガ
スを遮断し液化天然ガスの流れを流路３８ｂのみとする
。When the temperature of the heat exchanger 5b drops to a predetermined temperature, the three-way switching valves 4, 7, 9, and 10 are switched, and one side of the three-way switching valves 36 and 39, which are open on both sides, is closed to shut off the liquefied natural gas in the flow path 38a. The liquefied natural gas flows only through the flow path 38b.
これにより流路６ａは凝縮固化周期から蒸発除去周期へ
、流路６ｂは蒸発除去周期から凝縮固化周期に切り替わ
る。As a result, the flow path 6a switches from the condensation and solidification period to the evaporation removal period, and the flow path 6b switches from the evaporation and removal period to the condensation and solidification period.
以上易凝縮性成分除去工程は凝縮固化、切り替、蒸発、
真空排気、予冷のサイクルが対で成る熱交換器に於て周
期をずらせて繰り返えことにより連続的に行われる。The above easily condensable component removal process includes condensation solidification, switching, evaporation,
The vacuum evacuation and precooling cycles are repeated in a pair of heat exchangers with different cycles, thereby performing the cycle continuously.
易凝縮性成分除去熱交換器５ａを導出した約１５７℃の
低温精製空気は三方切替弁７、管８を経、管１８を経て
来る液体空気貯槽２４よりの低温蒸発空気と合流して約
−１５８℃で低温圧縮機１９に導入される。The low-temperature purified air of approximately 157° C. led out of the easily condensable component removal heat exchanger 5a passes through the three-way switching valve 7, the pipe 8, and joins with the low-temperature evaporated air from the liquid air storage tank 24 coming through the pipe 18, resulting in approximately - It is introduced into the low temperature compressor 19 at 158°C.
低温圧縮機１９に於て上記空気は圧縮され約２０気圧に
なる。The air is compressed in the low-temperature compressor 19 to approximately 20 atmospheres.
該低温圧縮機を駆動する電動機２０の所要動力は通常の
場合の約半分で良い。The required power of the electric motor 20 for driving the low-temperature compressor may be about half that of a normal case.
低温圧縮機１９を出た加圧空気は液化器２１に導入され
て向流する液化天然ガスによって約−１５７℃迄冷却液
化されて次いで適冷器２２に導入されて液体空気貯槽２
４よりの蒸発空気に冷却されて約−１６３℃になって該
適冷器２２を導出し、膨張弁２３によって２０気圧から
約１．２気圧に降圧して約−１９３℃になり液体空気貯
槽２４に導入される。The pressurized air coming out of the low-temperature compressor 19 is introduced into the liquefier 21 where it is cooled and liquefied to approximately -157°C by liquefied natural gas flowing countercurrently, and then introduced into the appropriate cooler 22 where it is stored in the liquid air storage tank 2.
The temperature is cooled by the evaporative air from 4 to about -163°C, and the appropriate cooler 22 is taken out, and the pressure is lowered from 20 atm to about 1.2 atm by the expansion valve 23, and the temperature reaches about -193°C, and the liquid air storage tank is discharged. It will be introduced on 24th.
該液体空気貯槽２４に貯えられた液体空気は管２７より
弁２８を経て取り出され使用に供される。The liquid air stored in the liquid air storage tank 24 is taken out from the pipe 27 through the valve 28 and is made available for use.
膨張弁２３および液体空気貯槽２４に於て発生した蒸発
空気は管２５より弁２６を介して更に１気圧に降圧、僅
かに降温しで一１９１℃になり適冷器２２に導入される
。The evaporated air generated in the expansion valve 23 and the liquid air storage tank 24 is further lowered in pressure to 1 atm through a pipe 25 and a valve 26, and the temperature is slightly lowered to -191° C., and then introduced into the appropriate cooler 22.
該蒸発空気は適冷器２２に於て向流する液体空気を適冷
して自身は昇温しで約−１６０℃どなり適冷器２２を導
出し管１８を経て管８よりの精製空気と合流し低温圧縮
機１９に導入される。The evaporated air cools the liquid air flowing countercurrently in the suitable cooler 22, and its temperature rises to about -160°C, which is led out of the suitable cooler 22 and passes through the pipe 18 to the purified air from the pipe 8. They are combined and introduced into the low-temperature compressor 19.
一方寒冷供給源である液化天然ガスは次の如く供給され
る。On the other hand, liquefied natural gas, which is a cold supply source, is supplied as follows.
即ち管３０より導入された液化天然ガスはポンプ３１に
より１．２気圧で圧送され管３２を経て２分しその１部
は弁３３を経て液化器２１に導入され向流する圧縮空気
を液化し、自身は気化して管３４より導出する。That is, the liquefied natural gas introduced from the pipe 30 is pumped at 1.2 atmospheres by the pump 31, divided into two parts through the pipe 32, and one part is introduced into the liquefier 21 through the valve 33, where it liquefies the compressed air flowing in the opposite direction. , itself is vaporized and led out from the tube 34.
２分した他部は管３５より三方切替弁３６を経て切り替
え使用する易凝縮性成分除去熱交換器の一方に導入して
向流する原料空気を冷却し自身は昇温気化して零度附近
の一定温度で導出し三方切替弁３９管、４０を経た後、
水分離器２に入って原料空気を一定温度に冷却すること
によって含有水分を凝縮させて導出し、管３４よりの気
化天然ガスと合流して管４１より糸外へ導出して使用に
供される。The other part of the two halves is introduced from the pipe 35 through the three-way switching valve 36 into one side of the heat exchanger for removing easily condensable components, which cools the raw material air flowing in the opposite direction, and the air itself is heated and vaporized to a temperature near zero. After being led out at a constant temperature and passing through a three-way switching valve 39 pipes and 40,
The raw material air enters the water separator 2 and is cooled to a constant temperature to condense the moisture contained therein and lead it out, join with the vaporized natural gas coming from the pipe 34, and lead it out of the thread through the pipe 41 for use. .
同局凝縮性成分除去熱交換器５ａ 、５ｂの出口または
水分離器２の出口に於ける液化天然ガスの温度が一定に
なる様に管３５より導入される液化天然ガスの量を調節
する装置をとりつける。A device is provided for adjusting the amount of liquefied natural gas introduced through the pipe 35 so that the temperature of the liquefied natural gas at the outlet of the condensable component removal heat exchangers 5a and 5b or the outlet of the water separator 2 is constant. Attach.
即ち熱交換器５ａ 、５ｂの出口または水分離器２の出
口に検出端を設けこれにより作動する流量調節弁を管３
５に設けることにより（図示せず）天候の変化による空
気中の水分の含有量の変化を水分離器２に於て吸収し熱
交換器５ａ、５ｂに於ける凝縮水分量を一定にする。That is, a detection end is provided at the outlet of the heat exchangers 5a, 5b or the outlet of the water separator 2, and a flow rate regulating valve operated by the detection end is connected to the pipe 3.
5 (not shown), the water separator 2 absorbs changes in the moisture content in the air due to changes in weather, and makes the amount of condensed moisture constant in the heat exchangers 5a and 5b.
本発明は以上の如く構成され実施されるがこれによる特
徴効果は次の通りである。The present invention is constructed and implemented as described above, and its characteristic effects are as follows.
第１に液体空気を製造するに際し原料空気の不純物除去
工程、液化工程共成化天然ガスの寒冷を有効に利用して
冷却を行うので極めて経済的である。First, when producing liquid air, cooling is performed by effectively utilizing the cooling of the co-produced natural gas in the process of removing impurities from the raw air and the process of liquefaction, so it is extremely economical.
第２に圧縮工程を低温精製工程の後にしたことにより低
温圧縮を行い、これによって圧縮に要する動力を通常の
場合に比較してはマ半減させた。Second, by placing the compression step after the low-temperature refining step, low-temperature compression was performed, thereby reducing the power required for compression by half compared to a normal case.
第３に空気中に含まれる水分、炭酸ガス等の不純物の除
去を液化天然ガスの寒冷を利用し且つ真空ポンプを使用
して簡単に一工程で除去しているため他の方法に比較し
て装置全体が簡単になり運転も容易で経済的である。Third, impurities such as moisture and carbon dioxide contained in the air can be easily removed in one step by using the cold of liquefied natural gas and by using a vacuum pump, making it easier to remove than other methods. The entire device is simple, easy to operate, and economical.
第４に上記易凝縮性成分除去方法は空気分離装置の不純
物除去工程に用いられているリパーシング熱交換器によ
る方法と異なり再生ガスを必要としないため原料空気を
１００℃製品液体空気とすることが出来無駄がない。Fourth, unlike the method using a reparsing heat exchanger used in the impurity removal process of an air separation device, the above method for removing easily condensable components does not require regeneration gas, so it is possible to convert the feed air into 100°C product liquid air. There is no waste.
且つ使用する熱交換器も２流路で良くまた容量が小さく
て済む。Moreover, the heat exchanger used only needs to have two channels and has a small capacity.
第５に膨張弁および液体空気貯槽に於て発生した蒸発空
気を全量再液化するので常に大気と同一組成の液体空気
が得られる等の特徴効果がある。Fifth, since the entire amount of evaporated air generated in the expansion valve and liquid air storage tank is reliquefied, there are characteristic effects such as always obtaining liquid air having the same composition as the atmosphere.
図は本発明方法を説明する系統図である。
１．３，８，１３，１５，１８，２５，２７゜３０．３
２，３４，３５，３７ａ、３７ｂ、４０及び４１は管、
２は水分離器、４，７，９，１０゜３６及び３９は三方
切替弁、５ａ、５ｂは易凝縮性成分除去熱交換器、６ａ
、６ｂは空気流路、１１゜１４は加熱器、１２は循環
ブロワ−１１６、２６゜２８及び３３は弁、１７は真空
ポンプ、１９は低温圧縮機、２０は電動機、２１は液化
器、２２は適冷器、２３は膨張弁、２４は液体空気貯槽
、３１はポンプ、３８ａ、３８ｂは流路である。The figure is a system diagram explaining the method of the present invention. 1.3, 8, 13, 15, 18, 25, 27°30.3
2, 34, 35, 37a, 37b, 40 and 41 are pipes,
2 is a water separator, 4, 7, 9, 10° 36 and 39 are three-way switching valves, 5a and 5b are easily condensable component removal heat exchangers, 6a
, 6b is an air flow path, 11° 14 is a heater, 12 is a circulation blower 116, 26° 28 and 33 are valves, 17 is a vacuum pump, 19 is a low temperature compressor, 20 is an electric motor, 21 is a liquefier, 22 23 is an expansion valve, 24 is a liquid air storage tank, 31 is a pump, and 38a and 38b are channels.
Claims (1)
方法において、空気を冷却して空気中に含有する易凝縮
性成分を固化流路に凝縮固化させる固化分離周期と、易
凝縮性成分固化流路に、加熱器、循環ブロワ−を介して
循環流路を接続し、該流路の空気を加熱しつつ循環する
ことにより固化成分を蒸発同伴して導出し、且つこれを
循環流路に接続した真空ポンプにより糸外に排出する蒸
発除去周期との両周期を、対を成す熱交換器によって交
互にくり返す精製工程によって低温精製空気を得、次い
で低温圧縮工程、液化工程を経て液体空気を得ると共に
上記精製工程、液化工程に液化天然ガスを供給して冷却
する様にしたことを特徴とする液体空気の製造方法。 ２ 液化天然ガスの寒冷を利用して液体空気を製造する
方法において、空気を冷却して空気中に含有する易凝縮
性成分を固化流路に凝縮固化させる固化分離周期と、易
凝縮性成分固化流路に、加熱器、循環ブロワ−を介して
循環流路を接続し、該流路の空気を加熱しつつ循環する
ことにより固化成分を蒸発同伴して導出し、且つこれを
循環流路に接続した真空ポンプにより系外に排出する蒸
発除去周期との両周期を、対を成す熱交換器によって交
互にくり返す精製工程によって低温精製空気を得た後、
これを後記する液体空気貯槽よりの蒸発空気と合流した
上、低温圧縮工程により１５〜３５気圧に圧縮し、次い
で液化器に導入して液化し更に液体空気貯槽よりの蒸発
空気により適冷した後、膨張弁を介して液体空気貯槽に
導入する液化工程により、液体空気を得るようにすると
共に上記精製工程、液化工程に液化天然ガスを供給して
冷却するようにしたことを特徴とする液体空気の製造方
法。[Claims] 1. A method for producing liquid air using the cooling of liquefied natural gas, which includes a solidification separation cycle in which air is cooled and easily condensable components contained in the air are condensed and solidified in a solidification channel. , a circulation flow path is connected to the easily condensable component solidification flow path via a heater and a circulation blower, and the air in the flow path is heated and circulated to evaporate and entrain the solidified component, and Low-temperature purified air is obtained through a purification process in which both cycles of evaporation and removal, in which the air is discharged to the outside of the thread by a vacuum pump connected to a circulation channel, are repeated alternately using a pair of heat exchangers, followed by a low-temperature compression process, A method for producing liquid air, characterized in that liquid air is obtained through a liquefaction step, and liquefied natural gas is supplied to the purification and liquefaction steps for cooling. 2. In a method for producing liquid air using the refrigeration of liquefied natural gas, there is a solidification separation cycle in which air is cooled and easily condensable components contained in the air are condensed and solidified in a solidification channel, and a solidification cycle in which easily condensable components are solidified. A circulation flow path is connected to the flow path via a heater and a circulation blower, and by heating and circulating the air in the flow path, the solidified components are evaporated and entrained, and this is introduced into the circulation flow path. After obtaining low-temperature purified air through a purification process in which both the evaporation removal cycle and the evaporation removal cycle in which air is discharged outside the system by a connected vacuum pump are alternately repeated using a pair of heat exchangers,
This is combined with evaporated air from the liquid air storage tank (described later), compressed to 15 to 35 atmospheres in a low-temperature compression process, then introduced into a liquefier to liquefy, and further cooled appropriately with evaporated air from the liquid air storage tank. Liquid air is obtained by a liquefaction process that is introduced into a liquid air storage tank through an expansion valve, and is also cooled by supplying liquefied natural gas to the purification process and liquefaction process. manufacturing method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP50092924A JPS5825953B2 (en) | 1975-07-30 | 1975-07-30 | Exhaust air system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP50092924A JPS5825953B2 (en) | 1975-07-30 | 1975-07-30 | Exhaust air system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5216479A JPS5216479A (en) | 1977-02-07 |
| JPS5825953B2 true JPS5825953B2 (en) | 1983-05-31 |
Family
ID=14068025
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP50092924A Expired JPS5825953B2 (en) | 1975-07-30 | 1975-07-30 | Exhaust air system |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5825953B2 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS55146372A (en) * | 1979-05-02 | 1980-11-14 | Nippon Oxygen Co Ltd | Method of liquefying air by liquefied natural gas |
| JPS5634083A (en) * | 1979-08-23 | 1981-04-06 | Nippon Oxygen Co Ltd | Method of liquefying air by low temperature of liquefied natural gas |
| US7165422B2 (en) * | 2004-11-08 | 2007-01-23 | Mmr Technologies, Inc. | Small-scale gas liquefier |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3364686A (en) * | 1963-08-17 | 1968-01-23 | Linde Ag | Process and installation for the removal of easily condensable components from gas mixtures |
| JPS4945054A (en) * | 1972-08-03 | 1974-04-27 | ||
| JPS5056392A (en) * | 1973-09-19 | 1975-05-17 |
-
1975
- 1975-07-30 JP JP50092924A patent/JPS5825953B2/en not_active Expired
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3364686A (en) * | 1963-08-17 | 1968-01-23 | Linde Ag | Process and installation for the removal of easily condensable components from gas mixtures |
| JPS4945054A (en) * | 1972-08-03 | 1974-04-27 | ||
| JPS5056392A (en) * | 1973-09-19 | 1975-05-17 |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5216479A (en) | 1977-02-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US3894856A (en) | Liquefaction of natural gas with product used as adsorber | |
| US2496380A (en) | Gas purifying method and apparatus | |
| US4699642A (en) | Purification of carbon dioxide for use in brewing | |
| US3608323A (en) | Natural gas liquefaction process | |
| US4367082A (en) | Air separating system | |
| JPS5939671B2 (en) | Air separation method and device | |
| CN101981399B (en) | Distillation method and apparatus | |
| US1989190A (en) | Apparatus for separating low boiling gas mixtures | |
| BR112020021060A2 (en) | air separation unit, and, air separation method. | |
| US2619810A (en) | Low-pressure process of and apparatus for separating gas mixtures | |
| US20080289362A1 (en) | Process and apparatus for low-temperature air fractionation | |
| US4192662A (en) | Process for liquefying and rectifying air | |
| US4732597A (en) | Low energy consumption method for separating gaseous mixtures and in particular for medium purity oxygen production | |
| JP4276520B2 (en) | Operation method of air separation device | |
| TWI628401B (en) | Verfahren und vorrichtung zur sauerstoffgewinnung durch tieftemperaturzerlegung von luft mit variablem energieverbrauch | |
| US2918801A (en) | Process and apparatus for separating gas mixtures | |
| US3233418A (en) | Apparatus for liquefying helium | |
| CN104185767B (en) | For the method and apparatus producing two strands of partial air flow purified | |
| KR19990014225A (en) | Separation method of air by cryogenic rectification | |
| CN103109145B (en) | For compressing the method and apparatus with cooling-air | |
| US3057167A (en) | Process and apparatus for separating helium from helium-air mixtures | |
| JPS5825953B2 (en) | Exhaust air system | |
| US1810312A (en) | Pro ess of separating gases | |
| US2213338A (en) | Method and apparatus for fractionating gaseous mixtures | |
| JPH10170144A (en) | Device and method for cleaning raw air of air liquefaction and separation device |