JP2021116935A - 液化装置 - Google Patents
液化装置 Download PDFInfo
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- JP2021116935A JP2021116935A JP2020008148A JP2020008148A JP2021116935A JP 2021116935 A JP2021116935 A JP 2021116935A JP 2020008148 A JP2020008148 A JP 2020008148A JP 2020008148 A JP2020008148 A JP 2020008148A JP 2021116935 A JP2021116935 A JP 2021116935A
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- 238000000926 separation method Methods 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 24
- 229910001873 dinitrogen Inorganic materials 0.000 description 16
- 239000007789 gas Substances 0.000 description 15
- 239000007788 liquid Substances 0.000 description 9
- 239000003949 liquefied natural gas Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
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- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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Abstract
Description
ところが、商用電力は電力会社など予め契約で定められており、これを守らないと多額の罰金が科せられる。つまり、電力契約の超過防止が絶対に必要である。
そこで、本発明は、各時間帯における契約電力上限値に応じた液化装置の自動負荷調整を行い、液化製品の製造量の最大化及び最適効率運用が可能な液化装置を提供することを目的とする。
また、液化装置を備える空気分離装置を提供することを目的とする。
使用電力を積算した積算電力値に基づいて、所定時間経過後(例えば10〜40分後)の予測電力量を求める予測電力算出部と、
前記予測電力量と、瞬時電力の移動平均(例えば1分)とを比較し、大きい値の方を制御対象として、目標値を超えないように限りなく近づけるように、圧縮機の吐出流量(の可変)を制御する電力デマンド制御部と、を備える。
「目標値」は、例えば、各時間帯における契約電力の上限値まで使用させるときは、契約の最大電力量である。
液化装置の負荷調整を自動化し、効率を高めることができる。
前記圧縮機の吐出流量を可変にすることで、液化装置全体の製造量を増減できる。
製品ガスを圧縮する圧縮機と、
圧縮された圧縮製品ガスを冷却する熱交換器と、
熱交換器の中間から導出された圧縮製品ガスを膨張する膨張タービンと、
熱交換器から導出された冷却(または液化)圧縮製品ガスを膨張する膨張弁と、
膨張弁で膨張された液化製品ガスを気液に分離する気液分離器と、
液化製品の実製造量を求める製造量算出部と、
を備えていてもよい。
前記液化装置は、前記膨張タービンの入口圧力を一定に制御し、膨張率を最大値に維持する膨張タービン入口ノズルを備えていてもよい。
前記液化装置は、
前記膨張弁の入口と出口の温度を測定する温度センサと、
前記温度センサで測定された、膨張弁の入口と出口の温度の差を制御する温度制御部を備えていてもよい。
これにより、膨張タービンの処理量が変化してもフラッシュロスを最小にできる。膨張タービンと膨張弁への流量バランスが崩れると膨張弁の2次側でのフラッシュロスが増えるが、膨張弁の入口と出口の温度差を小さくするようにまたは所定範囲内に収まるように制御することでこれを防止できる。
上記構成によれば、液化装置全体の負荷調整に伴い、原料となる窒素ガスなどの供給元である空気分離装置も連動して負荷調整されることで原料の放出ロスが完全にゼロに制御される。
また、空気分離装置の全体負荷調整は、電力デマンド制御部の制御により決まる液化装置の負荷目標に応じて高度制御を使用し、一切の手動介在なく自動的に負荷調整が行われ、各製品純度や発生量を適切に制御される。
また、意図的に液化製品の減量を行う場合は、電力デマンド制御部による制御において「目標値」を任意設定することで任意の製造量に自動的に減量制御される。
実施形態1の液化装置1および空気分離装置2について図1を用いて説明する。
液化装置1は、空気分離装置2からの窒素ガス導入管L1と、窒素ガスを圧縮する圧縮機3と、圧縮機3で圧縮した圧縮窒素ガスをLNG寒冷源7の寒冷を利用して冷却、液化する熱交換器6と、熱交換器6で中間温度まで冷却された圧縮窒素ガスの一部を分岐して導出する管L4と、管L4に設けた圧縮窒素ガスを膨張させて寒冷を発生させる膨張タービン4と、膨張タービン4で膨張した窒素ガスを、窒素ガスの冷源として熱交換器6に導入し、昇温後に圧縮機3の吸入側に合流させる管L5と、気液分離器13と、気液分離器13から取り出される液化製品の導出ラインL8と、分散制御装置9とを備える。
本実施形態において、膨張タービン入口ノズルは、膨張タービン4の入口圧力を一定に制御し、膨張率を最大値に維持する。
また、膨張弁5の入口と出口の温度を測定する温度センサが設けられている。
製造量算出部91は、液化窒素の実製造量を求める。
予測電力算出部92は、使用電力を積算した積算電力値に基づいて、圧縮機3に使用される、所定時間経過後の予測電力量を求める。
積算電力値は、設定された所定時間内(例えば、算出する直前の20分〜60分間などの設定時間内)の総使用電力量である。積算電力値=Σ使用電力値(所定時間内の累積値)。
本実施形態では、予測電力算出部92は、30分経過後の予測電力量をリアルタイムに算出する。
予測電力量(kW/h)の算出方法は、上記積算電力値を所定時間で除算して平均値を求め、これを予測電力量としてもよく、積算電力値の単位時間当たりの変化量(傾き)求め、この変化量に応じてと予測電力量を算出してもよい。
電力デマンド制御部93は、予測電力量と、圧縮機3に使用された瞬時電力の移動平均(例えば1分)とを比較し、大きい値の方を制御対象として、目標値を超えないように限りなく近づけるように、圧縮機3の吐出流量の可変制御をする。
温度制御部94は、膨張弁5の入口と出口の温度の差を制御する。
本実施形態によれば、契約電力の使用を最大化でき、液体窒素の製造量を従来よりも3から5%増量することができ、液化効率も2%向上することができた。また、契約電力に近づいたときに発せられていたアラームがなくなり、液化装置1の操作変更回数も削減でき、空気分離装置2及び液化装置1の自動運転化にも寄与するものとなった。
(1)特に明示していないが、各配管に、制御弁、圧力調整装置、流量制御装置などが設置され、弁開閉調整、圧力調整または流量調整が行われていてもよい。
(2)膨張タービン4は、軸流式とラジアル式のいずれでもあってもよい。液化装置1は、単一の膨張タービンを有している構成に限定されず、複数の膨張タービンが直列または並列に配置されていてもよい。
(3)圧縮機3は、単体で構成されていてもよい、複数の圧縮機が直列に多段に配置されて圧縮機ユニットを構成してあってもよい。
(4)液化装置1は、単一の熱交換機6を有している構成に限定されず、複数の熱交換器を並列配置し、圧縮機ユニットの多段階構成に合わせて、熱交換器の温端と冷端、中間端への配管経路が構成されていてもよい。
(5)熱交交換器6は、LNG寒冷源7の寒冷を利用していたが、これに制限されず、冷凍機から供給される寒冷を利用してもよく、複数の膨張タービンからの寒冷を利用してもよい。
2 空気分離装置
3 圧縮機
4 膨張タービン
5 膨張弁
6 熱交換器
9 分散制御装置
13 気液分離器
Claims (4)
- 使用電力を積算 した積算電力値に基づいて、所定時間経過後の予測電力量を求める予測電力算出部と、
前記予測電力量と、瞬時電力の移動平均とを比較し、大きい値の方を制御対象として、目標値を超えないように限りなく近づけるように、圧縮機の吐出流量を制御する電力デマンド制御部と、を備える、液化装置。 - 前記液化装置は、
膨張タービンと、
前記膨張タービンの入口圧力を一定に制御し、膨張率を最大値に維持する膨張タービン入口ノズルを備える、請求項1に記載の液化装置。 - 前記液化装置は、
膨張弁と、
前記膨張弁の入口と出口の温度差を制御する温度制御部を備える、請求項1または2に記載の液化装置。 - 請求項1〜3のいずれか1項に記載の液化装置を備える空気分離装置。
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ES20215875T ES2963943T3 (es) | 2020-01-22 | 2020-12-21 | Aparato de licuefacción |
EP20215875.4A EP3855099B1 (en) | 2020-01-22 | 2020-12-21 | Liquefaction apparatus |
SG10202100379YA SG10202100379YA (en) | 2020-01-22 | 2021-01-13 | Liquefaction apparatus |
CN202110062714.5A CN113154794B (zh) | 2020-01-22 | 2021-01-18 | 液化装置 |
US17/155,749 US11913719B2 (en) | 2020-01-22 | 2021-01-22 | Liquefaction apparatus |
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US11913719B2 (en) | 2024-02-27 |
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