JPH0210356B2 - - Google Patents
Info
- Publication number
- JPH0210356B2 JPH0210356B2 JP15751184A JP15751184A JPH0210356B2 JP H0210356 B2 JPH0210356 B2 JP H0210356B2 JP 15751184 A JP15751184 A JP 15751184A JP 15751184 A JP15751184 A JP 15751184A JP H0210356 B2 JPH0210356 B2 JP H0210356B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- temperature
- expansion turbine
- pressure expansion
- low
- 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 101
- 238000005057 refrigeration Methods 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 38
- 229910001873 dinitrogen Inorganic materials 0.000 description 20
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 238000000034 method Methods 0.000 description 7
- 239000007788 liquid Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000001816 cooling Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000001681 protective effect Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
〔発明の利用分野〕
本発明は、空気分離装置等で分離した窒素、酸
素等の沸点が極めて低いガスを寒冷発生源として
高圧膨張タービンと低圧膨張タービンを用いた、
いわゆる２段膨張タービンを使用して液化するガ
ス液化装置に関するものである。[Detailed Description of the Invention] [Field of Application of the Invention] The present invention uses a high-pressure expansion turbine and a low-pressure expansion turbine using gases with extremely low boiling points such as nitrogen and oxygen separated by an air separation device etc. as a cold generation source.
The present invention relates to a gas liquefaction device that liquefies gas using a so-called two-stage expansion turbine.
酸素、窒素等の沸点の極めて低いガスを効率良
く液化する方法として、例えば特公昭49−40547
号公報に示されるように、高圧膨張タービンと低
圧膨張タービンを組合せた２段膨張式のタービン
を使用した方法が知られている。
For example, as a method for efficiently liquefying gases with extremely low boiling points such as oxygen and nitrogen,
As shown in the above publication, a method using a two-stage expansion turbine that is a combination of a high-pressure expansion turbine and a low-pressure expansion turbine is known.
ガス液化装置においては、高圧の状態で液化さ
れた製品液化ガスを貯蔵タンクその他に供給する
場合、低圧の状態に減圧する必要があり、この
時、製品液化ガスが十分に過冷却されていない
と、減圧された時液の一部がフラツシユしてガス
が発生する。 In gas liquefaction equipment, when supplying product liquefied gas under high pressure to a storage tank or other equipment, it is necessary to reduce the pressure to a low pressure state. When the pressure is reduced, part of the liquid flashes and gas is generated.
このフラツシユロスを少なくするためには、高
圧の製品液化ガスを減圧後の飽和温度まで過冷却
してやる必要があり、そのため、低圧膨張タービ
ンのガスの出口温度を、液化ガスの減圧後の飽和
温度以下に下げる必要がある。しかしながら、低
圧膨張タービンの出口温度を下げ過ぎると、ガス
の一部が液化し、ミストが発生する。膨張タービ
ンは、一般に数万回転という高速回転で運転され
ており、ガス中に液ミストが発生すると、摩耗や
アンバランスを起してタービンを破壊する恐れが
ある。このための保護装置として特公昭49−
40547号公報に示されているように、低圧膨張タ
ービンの出口ガス温度を制御する方法がこれまで
採用されている。 In order to reduce this flash loss, it is necessary to supercool the high-pressure product liquefied gas to the saturation temperature after depressurization. Therefore, the gas outlet temperature of the low-pressure expansion turbine must be lowered below the saturation temperature of the liquefied gas after depressurization. need to be lowered. However, if the outlet temperature of the low-pressure expansion turbine is lowered too much, part of the gas will liquefy and mist will be generated. Expansion turbines are generally operated at high speeds of several tens of thousands of revolutions, and if liquid mist is generated in the gas, it may cause wear or imbalance, which may destroy the turbine. As a protective device for this purpose,
As shown in Japanese Patent No. 40547, a method of controlling the outlet gas temperature of a low pressure expansion turbine has been adopted so far.
一方、寒冷を発生する膨張タービンは、熱力学
の原理からガスの温度、圧力が高い方が理論断熱
熱落差が多いため、熱交換器が許容できる範囲内
で膨張タービンの入口ガス温度を高めた方がガス
液化装置の効率が向上する。 On the other hand, in an expansion turbine that generates cold air, based on the principle of thermodynamics, the higher the gas temperature and pressure, the greater the theoretical adiabatic heat drop. This will improve the efficiency of the gas liquefaction equipment.
従来技術による高圧膨張タービンと低圧膨張タ
ービンを用いたガス液化装置の一例を液体窒素発
生装置で第２図により説明する。 An example of a gas liquefaction device using a high-pressure expansion turbine and a low-pressure expansion turbine according to the prior art will be described with reference to FIG. 2 as a liquid nitrogen generator.
第２図において、１は窒素ガスを昇圧する循環
圧縮機、２は予冷器、３はフロン等を冷媒とする
冷却器、４は熱交換器、５は液化器、６は高圧膨
張タービン、７は低圧膨張タービン、８は液化ガ
ス出口弁、９は熱交換器４で冷却された窒素ガス
の一部を寒冷発生用の高圧膨張タービン６に導く
導管、１０は残部を液化用ガスとして液化器５に
導く導管、１１は液化器５を通して高圧膨張ター
ビン６の出口と低圧膨張タービン７の入口とを連
結した導管である。 In Fig. 2, 1 is a circulation compressor that boosts the pressure of nitrogen gas, 2 is a precooler, 3 is a cooler using Freon or the like as a refrigerant, 4 is a heat exchanger, 5 is a liquefier, 6 is a high-pressure expansion turbine, and 7 8 is a low-pressure expansion turbine; 8 is a liquefied gas outlet valve; 9 is a conduit that guides a portion of the nitrogen gas cooled by the heat exchanger 4 to the high-pressure expansion turbine 6 for cold generation; and 10 is a liquefier that uses the remainder as liquefaction gas. A conduit 11 leading to the liquefier 5 is a conduit connecting the outlet of the high pressure expansion turbine 6 and the inlet of the low pressure expansion turbine 7 through the liquefier 5 .
ガス窒素を循環圧縮機１で約35Kg／cm2Ｇに昇圧
した後、予冷器２および冷却器３で冷却し、更に
熱交換器４で低温戻りガス窒素で約−100℃まで
冷却した後２分流し、その一方の高圧窒素ガスを
導管９より高圧膨張タービン６に導入し、圧力約
５Kg／cm2Ｇまで膨張させて約−160℃の寒冷を発
生させ、この窒素ガスを導管１１を介して液化器
５で約−150℃まで温度回復させた後、低圧膨張
タービン７に導入して約−190℃の寒冷を発生さ
せる。低圧膨張タービン７で圧力約0.3Kg／cm2Ｇ
となつた低圧、低温度の窒素ガスは液化器５に導
かれ、熱交換器４の出口で分流され導管１０より
液化器５に導かれた他方の高圧液化用の窒素ガス
を液化させると同時に過冷却し、更に熱交換器４
で高圧窒素ガスを冷却して温度回復した後、予冷
器２を経て循環圧縮機１に戻される。一方、液化
器５で液化された高圧液化用窒素ガスは、液化器
５の後流で製品の飽和温度まで過冷却され、導管
１２より液化ガス出口弁８を通つて製品液体窒素
として貯蔵タンクに溜められたり、空気分離装な
どの精留塔の寒冷源として使用される。低圧膨張
タービン７の出口ガス温度の調節は、出口温度検
出器を設け、温度調節装置１３により液化ガス出
口弁８を介して調節する方法が従来より行なわれ
ている。また、減量運転時または液化用ガスの調
整が間に合わないような場合は、前述の特公昭49
−40547号公報の方法なども併用されている。 After the gas nitrogen is pressurized to about 35 kg/cm 2 G by the circulating compressor 1, it is cooled by the precooler 2 and the cooler 3, and further cooled to about -100°C by the low-temperature return gas nitrogen in the heat exchanger 4. One of the high-pressure nitrogen gases is introduced into the high-pressure expansion turbine 6 through the conduit 9 and expanded to a pressure of approximately 5 kg/cm 2 G to generate cooling of approximately -160°C. After the temperature is recovered to about -150°C in the liquefier 5, it is introduced into the low pressure expansion turbine 7 and cooled to about -190°C. Pressure approximately 0.3Kg/cm 2 G at low pressure expansion turbine 7
The resulting low-pressure, low-temperature nitrogen gas is led to the liquefier 5, where it is divided at the outlet of the heat exchanger 4 and simultaneously liquefies the other high-pressure liquefied nitrogen gas, which is led to the liquefier 5 through the conduit 10. Supercooling and further heat exchanger 4
After the high-pressure nitrogen gas is cooled to recover its temperature, it is returned to the circulation compressor 1 via the precooler 2. On the other hand, the high-pressure liquefied nitrogen gas liquefied in the liquefier 5 is supercooled to the saturation temperature of the product in the wake of the liquefier 5, and is passed from the conduit 12 through the liquefied gas outlet valve 8 to the storage tank as product liquid nitrogen. It is stored and used as a cooling source for rectification towers such as air separation equipment. Conventionally, the outlet gas temperature of the low-pressure expansion turbine 7 is controlled by providing an outlet temperature detector and adjusting the temperature via the liquefied gas outlet valve 8 using the temperature control device 13. In addition, when reducing the amount of water or when the liquefaction gas cannot be adjusted in time, the above-mentioned
-40547 publication method etc. are also used together.
しかしながら、第２図に示す従来の調節方法で
は、液化器５で温度回復される低圧膨張タービン
７の入口温度は、高温流体である高圧の液化用ガ
スの流量によつて変化する。換言すれば、低圧膨
張タービン７の出口ガス温度で液化用ガス量を制
御する方法では、設計点以外の減量運転などでは
液化器５の伝熱面積の関係を変えることができな
いため、液化器５より製品として取出される液体
窒素の温度は、低圧膨張タービン７の出口温度優
先制御により、液化用ガス量の変動により大きく
変化し、また。高圧膨張タービン６の入口温度に
も影響を与えるなどの欠点があつた。 However, in the conventional adjustment method shown in FIG. 2, the inlet temperature of the low-pressure expansion turbine 7, whose temperature is recovered by the liquefier 5, changes depending on the flow rate of the high-pressure liquefaction gas, which is a high-temperature fluid. In other words, in the method of controlling the amount of liquefied gas by the outlet gas temperature of the low-pressure expansion turbine 7, the relationship between the heat transfer areas of the liquefier 5 cannot be changed by a reduction operation other than the design point. The temperature of liquid nitrogen taken out as a product changes greatly due to fluctuations in the amount of liquefied gas due to the outlet temperature priority control of the low-pressure expansion turbine 7. There were drawbacks such as affecting the inlet temperature of the high pressure expansion turbine 6.
液体窒素の温度が上昇するとフラツシユロスが
増加し、余分な窒素ガスを捨てることになり、効
率が低下する。一方、特公昭49−40547号公報の
高圧膨張タービン６の入口ガスをバイパスする方
法は、低圧膨張タービン７の保護としては有効で
あるが、エネルギーの損失となり、同様に液化装
置の効率が大幅に低下する。 As the temperature of liquid nitrogen increases, flash loss increases and excess nitrogen gas must be discarded, reducing efficiency. On the other hand, the method of bypassing the inlet gas of the high-pressure expansion turbine 6 disclosed in Japanese Patent Publication No. 49-40547 is effective in protecting the low-pressure expansion turbine 7, but it results in a loss of energy and similarly significantly reduces the efficiency of the liquefaction device. descend.
本発明は、かかる従来技術の欠点をなくするた
め、低圧膨張タービンの出口ガス温度を、高圧膨
張タービンの入口温度や液化ガスの最終冷却温度
に影響を与えることなく、装置の最適運転条件に
合せて運転できるガス液化装置を提供することに
ある。
In order to eliminate the drawbacks of the prior art, the present invention adjusts the outlet gas temperature of the low-pressure expansion turbine to the optimum operating conditions of the device without affecting the inlet temperature of the high-pressure expansion turbine or the final cooling temperature of the liquefied gas. The object of the present invention is to provide a gas liquefaction device that can be operated with ease.
本発明の要点は、高圧膨張タービン出口と低圧
膨張タービン入口とを連結する導管の途中に、低
圧膨張タービンの出口ガス温度を調節するための
タービン熱交換器を設け、温度調節するための高
温流体に液化用ガスを２分してその一方をタービ
ン熱交換器に通し、低圧膨張タービンの出口ガス
温度によりタービン熱交換器に導かれる液化用ガ
スと液化器を通る液化用ガス量をそれぞれ調節弁
により自動的に調整するようにしたもので、更に
液化器出口の製品液化ガスの温度を検出し、液化
ガス温度で高圧膨張タービンの入口温度を最適温
度に自動調整するようにしたものである。
The gist of the present invention is to provide a turbine heat exchanger for adjusting the outlet gas temperature of the low-pressure expansion turbine in the middle of a conduit connecting the high-pressure expansion turbine outlet and the low-pressure expansion turbine inlet, and to provide a high-temperature fluid for temperature adjustment. The liquefied gas is divided into two parts, one of which is passed through a turbine heat exchanger, and the amount of liquefied gas guided to the turbine heat exchanger and the amount of liquefied gas passed through the liquefier are controlled by control valves, respectively, depending on the outlet gas temperature of the low-pressure expansion turbine. Furthermore, the temperature of the product liquefied gas at the outlet of the liquefier is detected, and the inlet temperature of the high-pressure expansion turbine is automatically adjusted to the optimum temperature based on the liquefied gas temperature.
以下、本発明の一実施例を窒素ガス液化装置に
ついて第１図により詳細に説明する。
EMBODIMENT OF THE INVENTION Hereinafter, one embodiment of the present invention will be described in detail with reference to FIG. 1 regarding a nitrogen gas liquefaction apparatus.
第１図において、第２図と同一部分は同一符号
で示し説明を省略する。１４は高圧膨張タービン
６の出口と低圧膨張タービン７の入口とを連結し
た導管１１の途中に設けられたタービン熱交換
器、１５はタービン熱交換器１４を通る液化用ガ
スの自動調節弁、１６は液化器５の中間部を流れ
る液化用ガスの自動調節弁、１７はタービン熱交
換器１４に液化用ガスを導く導管、１８は液化器
５の中間から液化用ガスを導く導管、１９は自動
調節弁１５，１６を出た後の液化用ガスを再び液
化器５の後流側に導く導管、２０は液化ガス出口
温度を検出し高圧膨張タービン６の入口温度を調
節する温度調節装置２１のセツト値を変える自動
調節装置である。 In FIG. 1, the same parts as in FIG. 2 are designated by the same reference numerals and explanations will be omitted. 14 is a turbine heat exchanger provided in the middle of the conduit 11 connecting the outlet of the high-pressure expansion turbine 6 and the inlet of the low-pressure expansion turbine 7; 15 is an automatic control valve for the liquefied gas passing through the turbine heat exchanger 14; 16 17 is a conduit for guiding the liquefied gas to the turbine heat exchanger 14; 18 is a conduit for guiding the liquefied gas from the middle of the liquefier 5; 19 is an automatic control valve for the liquefied gas flowing through the middle of the liquefier 5; A conduit 20 guides the liquefied gas after exiting the control valves 15 and 16 to the downstream side of the liquefier 5, and 20 is a temperature control device 21 that detects the liquefied gas outlet temperature and adjusts the inlet temperature of the high-pressure expansion turbine 6. This is an automatic adjustment device that changes the set value.
第２図で説明したように、熱交換器４を出た高
圧の窒素ガスは２分され、寒冷発生用の窒素ガス
は導管９より高圧膨張タービン６に導かれ、ここ
で寒冷発生した窒素ガスは導管１１の途中に設け
られたタービン熱交換器１４に導かれる。一方、
導管１０より液化器５に導かれた液化用高圧窒素
ガスは更に２分され、一方の高圧窒素ガスは導管
１７よりタービン熱交換器１４に導かれる。ター
ビン熱交換器１４では、高圧膨張タービン６で低
温になつた寒冷発生用窒素ガスと液化用高圧窒素
ガスとが熱交換し、寒冷発生用ガスは所定の温度
まで昇温されて低圧膨張タービン７の入口に導か
れる。液化用高圧窒素ガスはここで液化され、液
化器５で分流されて液化された残りの液化用ガス
と自動調節弁１５および１６を経て導管１９で合
流し、再び液化器５の後流側に導かれて低圧膨張
タービン７で寒冷発生した出口窒素ガスと熱交換
し、過冷却されて導管１２、液化ガス出口弁８を
通つて製品液化ガスとして取出される。 As explained in FIG. 2, the high-pressure nitrogen gas that exits the heat exchanger 4 is divided into two parts, and the nitrogen gas for cold generation is guided through the conduit 9 to the high-pressure expansion turbine 6, where the cold generation nitrogen gas is guided to a turbine heat exchanger 14 provided in the middle of the conduit 11. on the other hand,
The high-pressure nitrogen gas for liquefaction led to the liquefier 5 through the conduit 10 is further divided into two parts, and one high-pressure nitrogen gas is led to the turbine heat exchanger 14 through the conduit 17. In the turbine heat exchanger 14 , the cold generation nitrogen gas that has become low temperature in the high pressure expansion turbine 6 and the liquefied high pressure nitrogen gas exchange heat, and the cold generation gas is heated to a predetermined temperature and then transferred to the low pressure expansion turbine 7 . will lead you to the entrance. The high-pressure nitrogen gas for liquefaction is liquefied here, and is divided in the liquefier 5 and joins with the remaining liquefied gas through the automatic control valves 15 and 16 in the conduit 19, and then flows back to the downstream side of the liquefier 5. The gas is guided and undergoes heat exchange with the cold generated outlet nitrogen gas in the low-pressure expansion turbine 7, is supercooled, and is taken out as a product liquefied gas through the conduit 12 and the liquefied gas outlet valve 8.
一方、低圧膨張タービン７の出口窒素ガス温度
は、温度調節装置１３により自動調節弁１５，１
６を介して自動制御される。また、製品液化ガス
の温度は導管１２に取付けられた温度検出器によ
り、高圧膨張タービン６の入口導管９に設置され
た温度調節装置２１のセツト値を自動セツトする
自動調節装置２０で液化ガス出口弁８を介して自
動制御される。 On the other hand, the temperature of the nitrogen gas at the outlet of the low-pressure expansion turbine 7 is controlled by the automatic control valves 15 and 1 by the temperature control device 13.
Automatically controlled via 6. Furthermore, the temperature of the product liquefied gas is determined by a temperature sensor attached to the conduit 12, and an automatic control device 20 that automatically sets a set value of a temperature control device 21 installed at the inlet conduit 9 of the high-pressure expansion turbine 6 is used to determine the temperature of the liquefied gas at the liquefied gas outlet. Automatically controlled via valve 8.
上述の実施例では、低圧膨張タービン７の出口
窒素ガス温度を検出して自動調節弁１５，１６を
作動する場合について説明したが、低圧膨張ター
ビン７の入口温度を検出しても間接的に同様な効
果が得られる。また、製品液化ガスの温度を検出
して液化ガス出口弁８を介して直接制御しても、
液化器５の熱交換性能上から高圧膨張タービン６
の入口温度は自動的に最適温度に制御されるが、
起動時など液化ガスが発生していない状態では温
度が定まらず、また、液化ガスの温度変化が小さ
いため制御性が悪い。本発明によれば、高圧膨張
タービン６入口の温度調節装置２１に、運転範囲
内の限界値にセツトポイントのリミツターを設け
ることもできるので、起動時の問題や制御性の問
題が解消される。 In the above-described embodiment, a case has been described in which the automatic control valves 15 and 16 are operated by detecting the nitrogen gas temperature at the outlet of the low-pressure expansion turbine 7, but the same effect can be indirectly achieved by detecting the inlet temperature of the low-pressure expansion turbine 7. You can get the following effect. Furthermore, even if the temperature of the product liquefied gas is detected and directly controlled via the liquefied gas outlet valve 8,
In view of the heat exchange performance of the liquefier 5, the high pressure expansion turbine 6
The inlet temperature is automatically controlled to the optimum temperature,
In a state where liquefied gas is not generated, such as during startup, the temperature is not fixed, and controllability is poor because the temperature change of liquefied gas is small. According to the present invention, the temperature control device 21 at the inlet of the high-pressure expansion turbine 6 can be provided with a set point limiter at a limit value within the operating range, so problems at startup and controllability are solved.
なお、本発明のタービン熱交換器１４の代り
に、従来の液化器５に高圧膨張タービン出口ガス
を昇温する通路と、液化器５を通らない高圧膨張
タービン出口から直接低圧膨張タービン入口にバ
イパスする導管を設けて、低圧膨張タービン出口
温度調節計でそれぞれの弁を作動させて制御して
も、本発明と類似の制御は可能であるが、液化器
５の伝熱面積の増加割合が大きくなるばかりでな
く、流量の大きな大口径導管に調節弁を設けるこ
とは経済的に不利となり、しかも弁の圧力損失増
加により膨張タービンの寒冷発生量も低下するた
め、性能上も損失が大きい。また、運転の変化に
よつて液化器の温度ゾーンが変化するため最適条
件とは成り得ず、液化器の温度ゾーンの変化に影
響しない本発明の方が有効である。 In addition, instead of the turbine heat exchanger 14 of the present invention, a passage for raising the temperature of high-pressure expansion turbine outlet gas is provided in the conventional liquefier 5, and a bypass is provided directly from the high-pressure expansion turbine outlet to the low-pressure expansion turbine inlet without passing through the liquefier 5. Although it is possible to perform control similar to the present invention by providing a conduit and controlling each valve by operating a low-pressure expansion turbine outlet temperature controller, the rate of increase in the heat transfer area of the liquefier 5 is large. Not only this, but it is economically disadvantageous to provide a control valve in a large-diameter conduit with a large flow rate, and furthermore, the increased pressure loss of the valve reduces the amount of refrigeration generated by the expansion turbine, resulting in a large performance loss. Furthermore, since the temperature zone of the liquefier changes due to changes in operation, the conditions cannot be optimal, and the present invention, which does not affect changes in the temperature zone of the liquefier, is more effective.
本発明は以上述べたように、高圧膨張タービン
出口と低圧膨張タービン入口を連結する導間の途
中に、低圧膨張タービン出口温度を調整するため
のタービン熱交換器を設けたことにより、従来の
ように液化器で低圧膨張タービン入口温度を昇温
していたものに比べて、低圧膨張タービン出口の
低圧、低温の窒素ガスの温度の影響が無いため、
いかなる運転条件においても低圧膨張タービン出
口温度を一定に制御することができ、しかも、液
化ガスの出口温度による高圧膨張タービン入口温
度制御を相俟つて、常にエネルギーロスの最小な
ガス液化装置の最適運転条件を容易に設定するこ
とができる効果がある。
As described above, the present invention provides a turbine heat exchanger for adjusting the low-pressure expansion turbine outlet temperature in the middle of the inductor connecting the high-pressure expansion turbine outlet and the low-pressure expansion turbine inlet. Compared to the liquefier that raised the temperature at the inlet of the low-pressure expansion turbine, there is no effect of the low pressure and low temperature of the nitrogen gas at the outlet of the low-pressure expansion turbine.
The low-pressure expansion turbine outlet temperature can be controlled constant under any operating conditions, and in combination with the high-pressure expansion turbine inlet temperature control based on the liquefied gas outlet temperature, optimal operation of the gas liquefaction equipment with minimum energy loss is achieved at all times. This has the effect that conditions can be easily set.
第１図は本発明の一実施例を示すガス液化装置
の系統図、第２図は高圧膨張タービンおよび低圧
膨張タービンを使用したいわゆる２段式膨張ター
ビンを採用した従来のガス液化装置の系統図であ
る。
１……循環圧縮機、２……予冷器、３……冷却
器、４……熱交換器、５……液化器、６……高圧
膨張タービン、７……低圧膨張タービン、８……
液化ガス出口弁、９〜１２，１７〜１９……導
管、１３，２１……温度調節装置、１４……ター
ビン熱交換器、１５，１６……自動調節弁、２０
……自動調節装置。
Fig. 1 is a system diagram of a gas liquefaction system showing an embodiment of the present invention, and Fig. 2 is a system diagram of a conventional gas liquefaction system that employs a so-called two-stage expansion turbine using a high-pressure expansion turbine and a low-pressure expansion turbine. It is. 1... circulation compressor, 2... precooler, 3... cooler, 4... heat exchanger, 5... liquefier, 6... high pressure expansion turbine, 7... low pressure expansion turbine, 8...
Liquefied gas outlet valve, 9-12, 17-19... conduit, 13, 21... temperature control device, 14... turbine heat exchanger, 15, 16... automatic control valve, 20
...Automatic adjustment device.
Claims (1)
戻りガスにより冷却した後、寒冷発生用ガスと液
化用ガスに２分流し、第１分流の寒冷発生用ガス
を高圧膨張タービンに導入して寒冷を発生させ、
高圧膨張タービン出口のガス温度を調節した後、
低圧膨張タービンに導入して更に寒冷を発生さ
せ、低温戻りガスを液化器を通して前記第２分流
の液化用ガスを液化すると共に、熱交換器を通し
て温度回復させた後、循環圧縮機に循環させるよ
うにしたガス液化装置において、 前記高圧膨張タービン出口と低圧膨張タービン
入口とを連結した導管の途中に、高圧膨張タービ
ン出口ガス温度を昇温するためのタービン熱交換
器を設け、前記第２分流の液化用ガスを液化器の
上流側で更に２分流し、一方の分流ガスを前記タ
ービン熱交換器を通して液化器の下流側で他方の
分流ガスと合流させる導管を設け、該導管および
他方の分流ガスの導管にそれぞれ流量を調整する
自動調節弁を設け、前記低圧膨張タービンの入口
温度または出口温度を検出して前記２台の自動調
節弁を作動する温度調節装置を設けたことを特徴
とするガス液化装置。 ２ 循環圧縮機で昇圧したガスを熱交換器で低温
戻りガスにより冷却した後、寒冷発生用ガスと液
化用ガスに２分流し、第１分流の寒冷発生用ガス
を高圧膨張タービンに導入して寒冷を発生させ、
高圧膨張タービン出口のガス温度を調節した後、
低圧膨張タービンに導入して更に寒冷を発生さ
せ、低温戻りガスを液化器を通して前記第２分流
の液化用ガスを液化すると共に、熱交換器を通し
て温度回復させた後、循環圧縮機に循環させるよ
うにしたガス液化装置において、 前記高圧膨張タービン出口と低圧膨張タービン
入口とを連結した導管の途中に、高圧膨張タービ
ン出口ガス温度を昇温するためのタービン熱交換
器を設け、前記第２分流の液化用ガスを液化器の
上流側で更に２分流し、一方の分流ガスを前記タ
ービン熱交換器を通して液化器の下流側で他方の
分流ガスと合流させる導管を設け、該導管および
他方の分流ガスの導管にそれぞれ流量を調整する
自動調節弁を設け、前記低圧膨張タービンの入口
温度または出口温度を検出して前記２台の自動調
節弁を作動する温度調節装置を設け、前記第１分
流の寒冷発生用ガスを高圧膨張タービンに導く導
管に高圧膨張タービン入口ガスの温度調節装置を
設け、液化器出口の液化ガス導管に製品液化ガス
温度を検出して前記温度調節装置のセツト値を自
動調整する自動調節装置を設けたことを特徴とす
るガス液化装置。[Scope of Claims] 1. After the gas pressurized by the circulation compressor is cooled by the low-temperature return gas in the heat exchanger, the gas is divided into two parts: cold generation gas and liquefaction gas, and the first division of cold generation gas is heated to high pressure. Introduced into an expansion turbine to generate cold,
After adjusting the gas temperature at the high pressure expansion turbine outlet,
The low-temperature return gas is introduced into a low-pressure expansion turbine to further generate refrigeration, and the low-temperature return gas is passed through a liquefier to liquefy the liquefied gas in the second branch, and after recovering its temperature through a heat exchanger, it is circulated to a circulation compressor. In the gas liquefaction apparatus, a turbine heat exchanger for increasing the temperature of the high-pressure expansion turbine outlet gas is provided in the middle of a conduit connecting the high-pressure expansion turbine outlet and the low-pressure expansion turbine inlet, and A conduit is provided in which the liquefied gas is further divided into two parts on the upstream side of the liquefier, and one of the divided gases passes through the turbine heat exchanger and joins with the other divided gas on the downstream side of the liquefier, and the conduit and the other divided gas are A gas conduit is provided with an automatic control valve that adjusts the flow rate, and a temperature control device is provided that detects the inlet temperature or outlet temperature of the low-pressure expansion turbine and operates the two automatic control valves. Liquefaction equipment. 2 After the gas pressurized by the circulation compressor is cooled by the low-temperature return gas in the heat exchanger, it is divided into two streams: cold generation gas and liquefaction gas, and the first divided cold generation gas is introduced into the high-pressure expansion turbine. generates cold,
After adjusting the gas temperature at the high pressure expansion turbine outlet,
The low-temperature return gas is introduced into a low-pressure expansion turbine to further generate refrigeration, and the low-temperature return gas is passed through a liquefier to liquefy the liquefied gas in the second branch, and after recovering its temperature through a heat exchanger, it is circulated to a circulation compressor. In the gas liquefaction apparatus, a turbine heat exchanger for increasing the temperature of the high-pressure expansion turbine outlet gas is provided in the middle of a conduit connecting the high-pressure expansion turbine outlet and the low-pressure expansion turbine inlet, and A conduit is provided in which the liquefied gas is further divided into two parts on the upstream side of the liquefier, and one of the divided gases passes through the turbine heat exchanger and joins with the other divided gas on the downstream side of the liquefier, and the conduit and the other divided gas are an automatic control valve for adjusting the flow rate in each of the conduits; a temperature control device for detecting the inlet temperature or outlet temperature of the low-pressure expansion turbine and operating the two automatic control valves; A temperature control device for the high pressure expansion turbine inlet gas is provided in the conduit that leads the generated gas to the high pressure expansion turbine, and the temperature of the product liquefied gas is detected in the liquefied gas conduit at the liquefier outlet to automatically adjust the set value of the temperature control device. A gas liquefaction device characterized by being equipped with an automatic adjustment device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15751184A JPS6136679A (en) | 1984-07-30 | 1984-07-30 | gas liquefaction equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15751184A JPS6136679A (en) | 1984-07-30 | 1984-07-30 | gas liquefaction equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6136679A JPS6136679A (en) | 1986-02-21 |
| JPH0210356B2 true JPH0210356B2 (en) | 1990-03-07 |
Family
ID=15651274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15751184A Granted JPS6136679A (en) | 1984-07-30 | 1984-07-30 | gas liquefaction equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6136679A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4961551B2 (en) * | 2006-06-20 | 2012-06-27 | 国立大学法人東北大学 | Cryogenic microslash generation system |
| BRPI0721364B1 (en) * | 2007-02-28 | 2017-03-28 | Hitachi Plant Technologies Ltd | method for treating oxidation reaction tailings gas in an aromatic dicarboxylic acid production process |
-
1984
- 1984-07-30 JP JP15751184A patent/JPS6136679A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6136679A (en) | 1986-02-21 |
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