JPS643467Y2 - - Google Patents
Info
- Publication number
- JPS643467Y2 JPS643467Y2 JP1982061536U JP6153682U JPS643467Y2 JP S643467 Y2 JPS643467 Y2 JP S643467Y2 JP 1982061536 U JP1982061536 U JP 1982061536U JP 6153682 U JP6153682 U JP 6153682U JP S643467 Y2 JPS643467 Y2 JP S643467Y2
- Authority
- JP
- Japan
- Prior art keywords
- adsorber
- brake
- blower
- gas
- heater
- 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
- 239000007789 gas Substances 0.000 claims description 22
- 239000002912 waste gas Substances 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 5
- 230000001172 regenerating effect Effects 0.000 claims description 4
- 230000008929 regeneration Effects 0.000 description 10
- 238000011069 regeneration method Methods 0.000 description 10
- 238000000034 method Methods 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
- 239000003463 adsorbent Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000013016 damping Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【考案の詳細な説明】
本考案は原料空気の精製に吸着器を使用する型
式の空気分離装置に於て、膨張タービン制動ブロ
ワーの圧縮熱を利用して吸着器の再生用エネルギ
ーの節減を図つた吸着器再生用ガスの供給装置に
関するものである。[Detailed description of the invention] This invention aims to save energy for regenerating the adsorber by using the compression heat of the expansion turbine damping blower in an air separation device that uses an adsorber to purify feed air. This invention relates to a gas supply device for regenerating an ivy adsorber.
空気を液化精溜することにより窒素および酸素
等を製造する装置に於ける原料空気中の水分およ
び炭酸ガスを除去する方式は大別してリバーシン
グ熱交換器等の非加熱再生式熱交換器により冷却
と精製を同時に行う方式とゼオライト等の吸着剤
により吸着精製を行う方式とがある。 Methods for removing moisture and carbon dioxide from the raw air in equipment that produces nitrogen, oxygen, etc. by liquefying and rectifying air can be broadly divided into cooling methods using non-heating regenerative heat exchangers such as reversing heat exchangers. There are two methods: one in which purification is carried out at the same time, and the other in which adsorption and purification is carried out using an adsorbent such as zeolite.
このうち吸着剤を用いた方式の空気液化分離装
置に於ては、吸着器の再生は通常該分離装置の廃
ガスを電熱器又は蒸気式加熱器で300℃迄加熱し
て供給することにより行つている。この場合、上
記廃ガスの温度は約４℃であるのでこの廃ガスを
300℃迄加熱するために多量のエネルギーを要し
ていた。 In air liquefaction separation equipment that uses adsorbents, regeneration of the adsorber is usually carried out by heating the waste gas from the separation equipment to 300°C with an electric heater or steam heater. It's on. In this case, the temperature of the above waste gas is about 4℃, so this waste gas is
It required a large amount of energy to heat up to 300℃.
本考案は、この種装置において膨張タービン制
動ブロワーには廃ガスを供給して制動を行わせて
いるが、この際加圧昇温した廃ガスは従来そのま
ま廃棄していた点に着目し、この圧縮熱を利用す
ることにより吸着器を再生するための所要エネル
ギーの節減を図り、同時にその再生用ガスの供給
系統に三方弁、保圧弁及び循環経路を設けて継続
運転を可能ならしめたものである。 The present invention focuses on the fact that in this type of equipment, waste gas is supplied to the expansion turbine braking blower to perform braking, but the waste gas, which has been pressurized and heated at this time, was conventionally disposed of as is. By utilizing the heat of compression, the energy required to regenerate the adsorber is reduced, and at the same time, a three-way valve, pressure holding valve, and circulation path are installed in the regeneration gas supply system to enable continuous operation. be.
図は本考案による吸着器再生用ガスの供給装置
の一実施例を示す図である。図に於て切替使用さ
れ対で成る原料空気中の水分および炭酸ガス除去
用吸着器１，１′は吸着剤として通常ゼオライト
が充填されており、管２より導入された圧縮原料
空気は吸着器入口弁３を経て吸着過程にある一方
の吸着器１に入り、水分および炭酸ガスを吸着剤
に吸着されて精製空気となり空気出口逆止弁４，
４′の一方の弁４を通り、管５を経て次工程の熱
交換器６に導入される。熱交換器６において分離
低温ガスとの熱交換により液化温度附近迄冷却さ
れた精製原料空気は精溜塔に導入され、液化精溜
されて製品ガスおよび廃ガスとに分離される。 The figure shows an embodiment of the adsorber regeneration gas supply device according to the present invention. In the figure, adsorbers 1 and 1', which are used alternately and are used to remove moisture and carbon dioxide from the feed air, are usually filled with zeolite as an adsorbent, and the compressed feed air introduced from the pipe 2 is It enters one of the adsorbers 1 which is in the adsorption process via the inlet valve 3, and the water and carbon dioxide are adsorbed by the adsorbent to become purified air.Air outlet check valve 4,
It passes through one valve 4 of 4' and is introduced into a heat exchanger 6 for the next step via a pipe 5. The purified feed air cooled to near the liquefaction temperature by heat exchange with the separated low-temperature gas in the heat exchanger 6 is introduced into the rectification tower, where it is liquefied and rectified and separated into product gas and waste gas.
精溜塔で分離され導出された廃ガスは前記熱交
換器６に入り原料空気と熱交換し昇温後導出して
一部分岐するが大部分は膨張タービン７に入りほ
ぼ常圧まで降圧、降温して寒冷を発生した後管８
より再び熱交換器６に入り、前記分岐した一部と
合流し、原料空気と熱交換してこれを冷却し自身
は昇温して約４℃で該熱交換器６を導出後、その
大部分は管９、管１０より制動ブロワー１１に入
る。制動ブロワー１１は膨張タービン７で発生し
た動力を吸収し該膨張タービン７の回転数を規定
値に保持するが、従来は、制動により加圧、昇温
した廃ガスは該制動ブロワー１１を排出後そのま
ま廃棄されていた。 The waste gas separated and led out in the rectification column enters the heat exchanger 6, where it exchanges heat with the raw material air, and after raising its temperature, is drawn out and partially branched out, but most of it enters the expansion turbine 7, where the pressure is lowered to almost normal pressure and the temperature is lowered. After the cold generation occurs, the tube 8
It enters the heat exchanger 6 again, merges with the branched part, exchanges heat with the raw material air, cools it, and heats itself up to about 4°C. After leading out the heat exchanger 6, its large The part enters the brake blower 11 through pipes 9 and 10. The brake blower 11 absorbs the power generated by the expansion turbine 7 and maintains the rotation speed of the expansion turbine 7 at a specified value. Conventionally, the exhaust gas, which has been pressurized and heated by braking, is discharged from the brake blower 11. It was just discarded.
本考案はこの従来廃棄していた制動加圧により
昇温した制動タービン排出ガスを、制動用ブロワ
ー１１の出口配管１２、三方弁１３を介して加熱
器１４に導入して約300℃に加熱した後、加熱器
１４の出口配管１５を経、再生加熱ガス入口逆止
弁１６，１６′の一方の弁１６′を経て、加熱再生
過程にある吸着器１′に導入する。吸着器１′に導
入された吸着器再生用加熱ガスは該器１′内を流
れ、前周期で吸着した水分および炭酸ガスを同伴
して管１７′を経、廃ガス出口弁１８′より大気に
放出される。吸着器１には同様に管１７を経て廃
ガス出口弁１８が設けられている。また管１７，
１７′には夫々吸着器切換時、吸着器内ガスを大
気に放出するための圧力放出弁１９，１９′を設
けられている。吸着器再生用加熱ガスを所望量流
して吸着器１′の加熱脱着過程が終了すると、次
いで非加熱の廃ガスによる冷却過程に入る。即ち
冷却過程は管９よりの４℃の廃ガスを制動タービ
ン１１を経ずに管２０を経、直接三方弁１３を経
て加熱源を切つた加熱器１４を経、開状態にある
切換弁１６′を経て吸着器１′に導入する。この冷
却用廃ガスの流量が多く必要で、制動ブロワー１
１に行く量が少ない場合は制動ガス量としては不
足するので管１２を分岐した管２１により制動ブ
ロワー出口ガスをリサイクルさせる。 In the present invention, the brake turbine exhaust gas heated by the brake pressurization, which was conventionally discarded, is introduced into the heater 14 through the outlet pipe 12 of the brake blower 11 and the three-way valve 13, and heated to approximately 300°C. Thereafter, the gas is introduced into the adsorber 1' which is in the process of heating and regeneration through the outlet pipe 15 of the heater 14 and one of the regenerated heated gas inlet check valves 16, 16'. The heated gas for adsorber regeneration introduced into the adsorber 1' flows through the adsorber 1', carries with it the moisture and carbon dioxide adsorbed in the previous cycle, passes through the pipe 17', and is discharged into the atmosphere from the waste gas outlet valve 18'. is released. The adsorber 1 is likewise provided with a waste gas outlet valve 18 via a line 17 . Also tube 17,
17' are provided with pressure release valves 19 and 19', respectively, for releasing the gas in the adsorber to the atmosphere when the adsorber is switched. When the heating desorption process of the adsorber 1' is completed by flowing the desired amount of heated gas for adsorber regeneration, a cooling process using unheated waste gas begins. That is, in the cooling process, the 4°C waste gas from the pipe 9 is passed through the pipe 20 without passing through the brake turbine 11, directly through the three-way valve 13, the heater 14 with the heating source turned off, and then the switching valve 16 which is in the open state. ' into the adsorber 1'. A large flow rate of this cooling waste gas is required, and the brake blower 1
If the amount going to 1 is small, the amount of brake gas is insufficient, so the brake blower outlet gas is recycled through a pipe 21 branched from the pipe 12.
なお制動ブロワー１１の出口配管１２は管２２
を分岐し、これは保圧弁２３を経て管２４により
大気へ解放されている。また加熱器１４の出口配
管１５の吸着器１又は１′の入口部には各入口部
を結ぶ管２５およびバランス弁２６が設けられて
おり切換時両吸着器の圧を均圧させる。そして両
吸着器の圧をバランスする均圧工程時は、再生用
ガスの流れが停止するがこの場合管１２の圧を圧
力検出制御器P.I.Cにより検出して保圧弁２３を
作動させ、制動ブロワーの吸入圧力を一定値に保
持する。制動ブロワーの吐出圧力はブロワー内に
設けられている絞り弁で一定に調節される。 Note that the outlet pipe 12 of the brake blower 11 is a pipe 22.
is branched off, and is released to the atmosphere via a pipe 24 via a pressure holding valve 23. Further, a pipe 25 connecting each inlet and a balance valve 26 are provided at the inlet of the adsorber 1 or 1' of the outlet pipe 15 of the heater 14 to equalize the pressures of both adsorbers at the time of switching. During the pressure equalization process to balance the pressures of both adsorbers, the flow of regeneration gas is stopped, but in this case, the pressure in the pipe 12 is detected by the pressure detection controller PIC, the pressure holding valve 23 is activated, and the brake blower is activated. Maintain suction pressure at a constant value. The discharge pressure of the brake blower is regulated at a constant level by a throttle valve provided within the blower.
いま原料空気1350m3／ｈの装置に本考案を適用
した場合膨張タービン７に導入される廃ガス量は
1000m3／ｈであり、該タービン入口に於ける条件
は入口温度−154℃、圧力４Kg／cm2Ｇである。ま
た該膨張タービン出口に於ては温度−183℃、圧
力0.3Kg／cm2Ｇである。一方この膨張タービン７
で発生した動力を吸収し、タービンの回転数を規
定値に合せるのに必要な制動ブロワー１１の条件
は入口温度４℃、入口圧力0.2Kg／cm2Ｇ、出口圧
力1.22Kg／cm2Ｇの場合、必要な廃ガス量は1040
m3／ｈ、出口温度は60℃である。従つて該制動タ
ービン出口よりの廃ガスを吸着器再生用ガスとし
て用いることによりこれを300℃迄加熱するに要
するエネルギーは
（300−60）0.3＝72.0Kcal／m3
であり、従来は88.8Kcal／m3必要であるから
16.8Kcal／m3のエネルギーが節減出来る。 If the present invention is applied to a device with feed air of 1350 m 3 /h, the amount of waste gas introduced into the expansion turbine 7 will be
1000 m 3 /h, and the conditions at the turbine inlet are an inlet temperature of -154°C and a pressure of 4 kg/cm 2 G. At the outlet of the expansion turbine, the temperature is -183°C and the pressure is 0.3 kg/cm 2 G. On the other hand, this expansion turbine 7
The conditions for the brake blower 11 necessary to absorb the power generated by the engine and adjust the rotational speed of the turbine to the specified value are: inlet temperature 4℃, inlet pressure 0.2Kg/cm 2 G, outlet pressure 1.22Kg/cm 2 G. In this case, the amount of waste gas required is 1040
m 3 /h, outlet temperature 60°C. Therefore, the energy required to heat the waste gas from the brake turbine outlet to 300°C by using it as adsorber regeneration gas is (300-60)0.3=72.0Kcal/m 3 , compared to the conventional energy of 88.8Kcal. /m 3 is required
Energy savings of 16.8Kcal/ m3 can be achieved.
本考案はこの様に従来方式の吸着器再生用ガス
の加熱系統に改良を加えて、膨張タービン制動ブ
ロワーによる圧縮熱を利用して吸着器の加熱再生
用ガスの加熱エネルギーの節減を図つたものであ
り、更に加熱器入口に三方弁を設けて吸着器冷却
時は制動ブロワーを経ない廃ガスを用いる様に
し、また制動ブロワー出口には圧力調節弁を設け
ることにより、吸着器切換時均圧の状態でも制動
ブロワー入口圧力を常に一定圧力に保持される様
にするとともに、制動ブロワーの制動ガスを確保
するため該制動ブロワーの出口ガスを該制動ブロ
ワーに循環させる経路を設けることにより、安定
継続運転を可能ならしめたものである。そして特
に、この循環経路を設けることで、制動ブロワー
の出口ガスは冷却工程時不足分循環吸入し、制動
ブロワーの負荷を一定に保ち圧力変動をなくすこ
とができる。この結果例えば原料空気1350m3／ｈ
で窒素ガス160m3／ｈ液化窒素65m3／ｈを製造す
る装置の場合約10kw動力費節減が可能になつた。 In this way, the present invention improves the conventional adsorber regeneration gas heating system and uses the compression heat from the expansion turbine brake blower to save heating energy for the adsorber regeneration gas. Furthermore, by installing a three-way valve at the heater inlet to use waste gas that does not pass through the brake blower when cooling the adsorber, and by installing a pressure control valve at the brake blower outlet, the pressure can be equalized when switching the adsorber. Even under these conditions, the inlet pressure of the brake blower is always maintained at a constant pressure, and a path is provided to circulate the outlet gas of the brake blower to the brake blower in order to secure the brake gas for the brake blower, thereby ensuring continued stability. This made it possible to drive. Particularly, by providing this circulation path, the outlet gas of the brake blower can be circulated and sucked in the amount that is insufficient during the cooling process, thereby making it possible to keep the load on the brake blower constant and eliminate pressure fluctuations. As a result, for example, raw air 1350m 3 /h
In the case of a device that produces 160 m 3 /h of nitrogen gas and 65 m 3 /h of liquefied nitrogen, it has become possible to save approximately 10 kW in power costs.
図は本考案による一実施例のフローシート図で
ある。
１及び１′は吸着器、７は膨張タービン、１１
は制動ブロワー、１２，１５は出口配管、１３は
三方弁、１４は加熱器、２３は保圧弁である。
The figure is a flow sheet diagram of an embodiment of the present invention. 1 and 1' are adsorbers, 7 is an expansion turbine, 11
1 is a brake blower, 12 and 15 are outlet pipes, 13 is a three-way valve, 14 is a heater, and 23 is a pressure holding valve.
Claims (1)
ン制動にブロワーを使用する型式の空気分離装置
に於て、廃ガス出口配管を二分して一方を制動ブ
ロワー１１入口へ連結するとともに他方を三方弁
１３を介して加熱器１４に連結し、前記制動ブロ
ワー１１の出口配管１２を三分してその一つを前
記三方弁１３を介して加熱器１４に連結し、かつ
加熱器１４の出口配管１５を前記吸着器１または
吸着器１′に連結し、前記三分した他の一つを保
圧弁２３を介して大気へ開放し、さらに他の一つ
を前記制動ブロワー１１に循環せしめたことを特
徴とする空気分離装置の吸着器再生用ガス供給装
置。 In an air separation device that uses an adsorber to purify raw air and a blower to brake the expansion turbine, the waste gas outlet pipe is divided into two, one of which is connected to the inlet of the brake blower 11, and the other connected to a three-way valve. The outlet pipe 12 of the brake blower 11 is divided into three parts, one of which is connected to the heater 14 via the three-way valve 13, and the outlet pipe 15 of the heater 14 is connected to the heater 14 through the three-way valve 13. is connected to the adsorber 1 or adsorber 1', the other one of the three parts is opened to the atmosphere via the pressure holding valve 23, and the other one is circulated to the brake blower 11. Features: A gas supply device for regenerating the adsorber of an air separation device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6153682U JPS58165584U (en) | 1982-04-27 | 1982-04-27 | Gas supply device for regenerating the adsorber of air separation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6153682U JPS58165584U (en) | 1982-04-27 | 1982-04-27 | Gas supply device for regenerating the adsorber of air separation equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58165584U JPS58165584U (en) | 1983-11-04 |
| JPS643467Y2 true JPS643467Y2 (en) | 1989-01-30 |
Family
ID=30071727
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6153682U Granted JPS58165584U (en) | 1982-04-27 | 1982-04-27 | Gas supply device for regenerating the adsorber of air separation equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58165584U (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0792327B2 (en) * | 1987-03-11 | 1995-10-09 | 株式会社日立製作所 | Gas separation apparatus and method for controlling the amount of raw material gas thereof |
| JP6925950B2 (en) * | 2017-12-15 | 2021-08-25 | 三菱重工機械システム株式会社 | Bottle cleaning system and bottle filling system |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5527034A (en) * | 1978-08-16 | 1980-02-26 | Hitachi Ltd | Pressure swing adsorption system used with heat regeneration method |
-
1982
- 1982-04-27 JP JP6153682U patent/JPS58165584U/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5527034A (en) * | 1978-08-16 | 1980-02-26 | Hitachi Ltd | Pressure swing adsorption system used with heat regeneration method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58165584U (en) | 1983-11-04 |
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