JPH09145003A - Lng fire power installation - Google Patents
Lng fire power installationInfo
- Publication number
- JPH09145003A JPH09145003A JP7307373A JP30737395A JPH09145003A JP H09145003 A JPH09145003 A JP H09145003A JP 7307373 A JP7307373 A JP 7307373A JP 30737395 A JP30737395 A JP 30737395A JP H09145003 A JPH09145003 A JP H09145003A
- Authority
- JP
- Japan
- Prior art keywords
- oxygen
- natural gas
- air
- liquefied natural
- boiler
- 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
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、ＬＮＧ火力設備に
関するものである。TECHNICAL FIELD The present invention relates to LNG thermal power equipment.
【０００２】[0002]
【従来の技術】ボイラなどの火力設備では、通常、重油
や石炭などの燃料を空気で燃焼させるようにしている。2. Description of the Related Art In a thermal power plant such as a boiler, fuel such as heavy oil or coal is usually burned with air.
【０００３】[0003]
【発明が解決しようとする課題】しかるに、ボイラなど
の火力設備で空気を用いて燃料を燃焼させた場合、空気
中に約８０％含まれている窒素が、ボイラからの排ガス
中にもそのまま含まれることとなるので、排ガスの組成
は、窒素が約８０％、二酸化炭素が約１５％、酸素が約
５％となる。However, when the fuel is burned by using air in a thermal power plant such as a boiler, nitrogen contained in the air at about 80% is contained in the exhaust gas from the boiler as it is. Therefore, the composition of the exhaust gas is about 80% nitrogen, about 15% carbon dioxide, and about 5% oxygen.
【０００４】一方、地球温暖化の原因物質として、二酸
化炭素が注目されており、多量の二酸化炭素を排出する
ボイラなどの火力設備でも、排ガスから二酸化炭素を分
離・回収する技術の確立が急がれている。On the other hand, carbon dioxide is drawing attention as a causative agent of global warming, and even in thermal power facilities such as boilers that emit a large amount of carbon dioxide, there is an urgent need to establish a technology for separating and recovering carbon dioxide from exhaust gas. Has been.
【０００５】しかし、排ガス中の二酸化炭素の割合が約
１５％であると、排ガスからの二酸化炭素の分離が困難
であり、多額の回収費用が掛るという問題がある。However, if the proportion of carbon dioxide in the exhaust gas is about 15%, it is difficult to separate the carbon dioxide from the exhaust gas, resulting in a large amount of recovery cost.
【０００６】本発明は、上述の実情に鑑み、発生する二
酸化炭素を経済的に回収し得るようにしたＬＮＧ火力設
備を提供することを目的とするものである。The present invention has been made in view of the above circumstances, and an object thereof is to provide an LNG thermal power plant capable of economically recovering generated carbon dioxide.
【０００７】[0007]
【課題を解決するための手段】本発明は、空気から酸素
を分離する酸素製造装置と、天然ガスを酸素製造装置か
らの酸素で燃焼させるボイラとを設けると共に、液化天
然ガスの冷熱を酸素製造装置の動力源の一部として使用
した後、液化天然ガスが気化してなる天然ガスをボイラ
の燃料として利用するよう構成したことを特徴とするＬ
ＮＧ火力設備にかかるものである。According to the present invention, an oxygen producing apparatus for separating oxygen from air and a boiler for combusting natural gas with oxygen from the oxygen producing apparatus are provided, and the cold heat of liquefied natural gas is used for producing oxygen. After being used as a part of the power source of the apparatus, the natural gas obtained by vaporizing the liquefied natural gas is used as a fuel for the boiler.
It is related to NG thermal power equipment.
【０００８】この場合において、液化天然ガスの冷熱
を、酸素製造装置における複精留塔の上部塔へ直接供給
する空気を断熱膨張させるための膨張タービンの駆動源
として利用するようにしても良い。In this case, the cold heat of the liquefied natural gas may be used as a drive source of an expansion turbine for adiabatically expanding the air directly supplied to the upper column of the double rectification column in the oxygen production apparatus.
【０００９】上記手段によれば、以下のような作用が得
られる。According to the above means, the following effects can be obtained.
【００１０】先ず、酸素製造装置で空気から酸素を分離
する。First, oxygen is separated from air in an oxygen production apparatus.
【００１１】この際、酸素製造装置に、液化天然ガスを
送って、液化天然ガスの冷熱で酸素製造装置の膨張ター
ビンを駆動させ、酸素の一部を膨張させる動力として使
用させると共に、膨張タービンの動力に使用された液化
天然ガスが気化されてなる天然ガスを、そのままボイラ
で使用させるようにする。At this time, the liquefied natural gas is sent to the oxygen production apparatus, and the expansion turbine of the oxygen production apparatus is driven by the cold heat of the liquefied natural gas to be used as a power for expanding a part of the oxygen. The natural gas obtained by vaporizing the liquefied natural gas used for power is used as it is in the boiler.
【００１２】ボイラで燃料として使用される天然ガス
は、液化天然ガスを気化させて使用することになるが、
液化天然ガスの冷熱を捨てないで利用するようにしたこ
とにより、電力のみを使用する場合に比べて、酸素製造
装置の動力が３％程度も削減されるようになる。The natural gas used as fuel in the boiler is liquefied natural gas after being vaporized.
By using the cold heat of the liquefied natural gas without discarding it, the power of the oxygen production device can be reduced by about 3% as compared with the case of using only electric power.
【００１３】次に、ボイラで、酸素製造装置で利用され
た天然ガスを、酸素製造装置で製造された酸素によって
燃焼させる。Next, in the boiler, the natural gas used in the oxygen production apparatus is burned by the oxygen produced in the oxygen production apparatus.
【００１４】このように、ボイラにて天然ガスを窒素を
含まない純粋な酸素で燃焼させることにより、排ガス中
の二酸化炭素の割合が約９０％にまで高められ、容易に
回収することができるようになる。Thus, by burning the natural gas in the boiler with pure oxygen that does not contain nitrogen, the proportion of carbon dioxide in the exhaust gas can be increased to about 90% and can be easily recovered. become.
【００１５】[0015]
【発明の実施の形態】以下、本発明の実施の形態を、図
示例と共に説明する。Embodiments of the present invention will be described below with reference to the drawings.
【００１６】図１・図２は、本発明の実施の形態の一例
である。FIG. 1 and FIG. 2 show an embodiment of the present invention.
【００１７】図１に示すように、空気１から酸素２を分
離する酸素製造装置３を設け、図示しない液化天然ガス
供給源からの天然ガス４（ＮＧ）を酸素製造装置３から
の酸素２で燃焼させるボイラ５を設けると共に、ボイラ
５で発生した排ガス６から二酸化炭素７を回収する二酸
化炭素回収設備８を設ける。As shown in FIG. 1, an oxygen production apparatus 3 for separating oxygen 2 from air 1 is provided, and natural gas 4 (NG) from a liquefied natural gas supply source (not shown) is converted into oxygen 2 from the oxygen production apparatus 3. A boiler 5 for burning is provided, and a carbon dioxide recovery facility 8 for recovering carbon dioxide 7 from an exhaust gas 6 generated in the boiler 5 is provided.
【００１８】この際、酸素製造装置３に、図示しない液
化天然ガス供給源からの液化天然ガス９（ＬＮＧ）を送
って、液化天然ガス９の冷熱で後述する膨張タービン１
０などを駆動させ、酸素２の一部を膨張させる動力とし
て使用させ得るようにする。At this time, liquefied natural gas 9 (LNG) from a liquefied natural gas supply source (not shown) is sent to the oxygen production apparatus 3, and the expansion turbine 1 to be described later is cooled by cooling the liquefied natural gas 9.
0 is driven so that it can be used as power for expanding a part of oxygen 2.
【００１９】尚、膨張タービン１０の駆動に使用された
液化天然ガス９は、気化されて天然ガス４となり、その
ままボイラ５で使用される。The liquefied natural gas 9 used to drive the expansion turbine 10 is vaporized into the natural gas 4, which is used as it is in the boiler 5.
【００２０】又、図中、１１は酸素製造装置３からの酸
素２をボイラ５へ送る酸素供給路、１２は酸素製造装置
３の膨張タービン１０を出た天然ガス４をボイラ５へ送
る天然ガス供給路、１３はボイラ５で発生した排ガス６
を二酸化炭素回収設備８へ送る排ガスダクト、１４は排
ガスダクト１３とボイラ５との間に設けられた排ガス循
環路、１５は排ガス循環路１４の途中に設けられた排ガ
ス循環ファンである。In the figure, 11 is an oxygen supply path for sending oxygen 2 from the oxygen producing apparatus 3 to the boiler 5, and 12 is natural gas 4 for sending the natural gas 4 from the expansion turbine 10 of the oxygen producing apparatus 3 to the boiler 5. Supply path, 13 is exhaust gas 6 generated in boiler 5
Is an exhaust gas circulation path provided between the exhaust gas duct 13 and the boiler 5, and 15 is an exhaust gas circulation fan provided in the middle of the exhaust gas circulation path 14.
【００２１】上記酸素製造装置３は、図２に示すような
構成を備えている。The oxygen production apparatus 3 has a structure as shown in FIG.
【００２２】即ち、空気流路１６に、上流側から順に、
原料となる空気１を吸入する吸入塔１７と、空気１を除
塵する空気濾過器１８と、空気１を約５ａｔの圧力に圧
縮するターボ式の空気圧縮機１９と、水ポンプ２０及び
水循環流路２１を介して冷水塔２２との間を循環される
冷水２３により空気１を冷却するようにした水洗冷却塔
２４と、２本１組の蓄冷槽２５を備えて、後述する不純
窒素２６で冷却された蓄冷槽２５内で空気１を約−１７
０℃に冷却して不純物である水分や空気中に含まれるわ
ずかな二酸化炭素を氷結分離させる２組の蓄冷器２７
と、上部塔２８と下部塔２９を備えて約５ａｔの圧力の
もとに冷却された空気１を精留するようにした複精留塔
３０の下部塔２９とを、接続する。That is, in the air flow path 16, from the upstream side,
A suction tower 17 for sucking air 1 as a raw material, an air filter 18 for removing dust of the air 1, a turbo type air compressor 19 for compressing the air 1 to a pressure of about 5 at, a water pump 20, and a water circulation passage. The washing water cooling tower 24 is configured to cool the air 1 with the cold water 23 circulated between the cold water tower 22 and the cold water tower 22, and a set of two cold storage tanks 25 are cooled with impure nitrogen 26 described later. Approximately -17 of air 1 in the stored cool storage tank 25
Two sets of regenerators 27 that are cooled to 0 ° C to separate impurities such as moisture and a small amount of carbon dioxide contained in the air by freezing
And the lower tower 29 of the double rectification tower 30 which is provided with the upper tower 28 and the lower tower 29 to rectify the cooled air 1 under the pressure of about 5 at.
【００２３】又、前記蓄冷槽２５の中間における−１２
０〜−１３０℃となる位置から空気１の一部を抽気する
抽気流路３１に、上流側から順に、吸着材を充填された
二酸化炭素吸着器３２と、空気流路１６の蓄冷器２７出
側から分岐された分岐空気流路３３と、液化天然ガス９
の冷熱によって駆動され、空気１をほぼ複精留塔３０の
上部塔２８圧力まで断熱膨張して、約−１９０℃とする
前記膨張タービン１０と、前記複精留塔３０の上部塔２
８とを、接続する。尚、３４は海水３５などを使用して
膨張タービン１０へ入れる前に液化天然ガス９を加熱す
る過熱器である。-12 in the middle of the cold storage tank 25
A carbon dioxide adsorber 32 filled with an adsorbent and a regenerator 27 of the air flow passage 16 are sequentially output from an upstream side to an extraction flow passage 31 for extracting a part of the air 1 from a position of 0 to −130 ° C. Branch air flow path 33 branched from the side, and liquefied natural gas 9
Driven by the cold heat of the double rectification column 30 to adiabatically expand the air 1 up to about the pressure of the upper column 28 of the double rectification column 30 to about -190 ° C. and the upper column 2 of the double rectification column 30.
8 and 8 are connected. Reference numeral 34 is a superheater that heats the liquefied natural gas 9 before it is put into the expansion turbine 10 using seawater 35 or the like.
【００２４】更に、下部塔２９の上部と上部塔２８との
間に、下部塔２９で分離された純度９８％程度の液体窒
素３６を上部塔２８へ送る流路３７を設け、且つ、下部
塔２９の下端と上部塔２８との間に、アセチレン吸着器
３８を備えて、下部塔２９で分離された酸素２を４０％
程度含む液体空気３９を上部塔２８へ送る流路４０を設
けると共に、複精留塔３０に、液酸循環ポンプ４１と循
環吸着器４２とを備えた液酸循環流路４３を設ける。Further, between the upper part of the lower tower 29 and the upper tower 28, there is provided a flow path 37 for sending the liquid nitrogen 36 having a purity of about 98% separated by the lower tower 29 to the upper tower 28, and the lower tower. An acetylene adsorber 38 is provided between the lower end of 29 and the upper column 28, and 40% of oxygen 2 separated in the lower column 29 is provided.
A flow passage 40 for sending the liquid air 39 containing a certain amount to the upper tower 28 is provided, and the double rectification tower 30 is provided with a liquid acid circulation passage 43 having a liquid acid circulation pump 41 and a circulation adsorber 42.
【００２５】更に、複精留塔３０の上部塔２８の下部と
前記蓄冷器２７の内部に設けられた蛇管４４との間に、
複精留塔３０で分離された純度９９．６〜９９．８％の
酸素２を蓄冷器２７へ送る酸素流路４５を接続し、酸素
流路４５に酸素圧縮機４６を介してボイラ５への酸素供
給路１１を接続する。Further, between the lower part of the upper column 28 of the double rectification column 30 and the flexible pipe 44 provided inside the regenerator 27,
An oxygen passage 45 for sending oxygen 2 having a purity of 99.6 to 99.8% separated in the double rectification column 30 to the regenerator 27 is connected, and the oxygen passage 45 is connected to the boiler 5 via the oxygen compressor 46. The oxygen supply path 11 is connected.
【００２６】更に又、複精留塔３０の上部塔２８の上部
と前記蓄冷器２７の下部との間に、複精留塔３０で分離
された純度９６〜９８％の不純窒素２６を蓄冷器２７へ
送る窒素流路４７を接続し、窒素流路４７の途中に過冷
器４８、液化器４９を接続する。更に、蓄冷器２７の上
部と、冷水塔２２との間を窒素流路４７で接続し、冷水
塔２２の出側で窒素流路４７を大気に解放する。Further, between the upper part of the upper column 28 of the double rectification column 30 and the lower part of the regenerator 27, the impure nitrogen 26 having a purity of 96 to 98% separated by the double rectification column 30 is stored in the regenerator. The nitrogen flow path 47 for sending to 27 is connected, and the subcooler 48 and the liquefier 49 are connected in the middle of the nitrogen flow path 47. Furthermore, the upper part of the regenerator 27 and the cold water tower 22 are connected by a nitrogen flow path 47, and the nitrogen flow path 47 is opened to the atmosphere on the outlet side of the cold water tower 22.
【００２７】尚、５０，５１は蓄冷槽２５に対して空気
１と不純窒素２６とを切替えるためのバルブである。Numerals 50 and 51 are valves for switching the air 1 and the impure nitrogen 26 to the cold storage tank 25.
【００２８】次に、作動について説明する。Next, the operation will be described.
【００２９】先ず、図１に示すように、酸素製造装置３
で空気１から酸素２を分離する。First, as shown in FIG. 1, the oxygen production apparatus 3
To separate oxygen 2 from air 1.
【００３０】この際、酸素製造装置３に、図示しない液
化天然ガス供給源からの液化天然ガス９（ＬＮＧ）を送
って、液化天然ガス９の冷熱で後述する膨張タービン１
０などを駆動させ、酸素２の一部を膨張させる動力とし
て使用させると共に、膨張タービン１０の動力に使用さ
れた液化天然ガス９が気化されてなる天然ガス４を、そ
のままボイラ５で使用させるようにする。At this time, liquefied natural gas 9 (LNG) from a liquefied natural gas supply source (not shown) is sent to the oxygen production apparatus 3, and the expansion turbine 1 to be described later is cooled by the liquefied natural gas 9 by heat.
0 and the like are used as power for expanding part of oxygen 2, and natural gas 4 obtained by vaporizing liquefied natural gas 9 used for power of expansion turbine 10 is used as it is in boiler 5. To
【００３１】ボイラ５で燃料として使用される天然ガス
４は、図示しない液化天然ガス供給源からの液化天然ガ
ス９を気化させて使用することになるが、液化天然ガス
９の冷熱を捨てないで利用するようにしたことにより、
電力のみを使用する場合に比べて、酸素製造装置３の動
力が３％程度も削減されるようになる。As the natural gas 4 used as a fuel in the boiler 5, the liquefied natural gas 9 from a liquefied natural gas supply source (not shown) is vaporized and used, but the cold heat of the liquefied natural gas 9 is not discarded. By using it,
Compared with the case of using only electric power, the power of the oxygen production apparatus 3 is reduced by about 3%.
【００３２】次に、ボイラ５で、酸素製造装置３で利用
された天然ガス４（ＮＧ）を、酸素製造装置３で製造さ
れた酸素２によって燃焼させる。Next, in the boiler 5, the natural gas 4 (NG) used in the oxygen production apparatus 3 is burned by the oxygen 2 produced in the oxygen production apparatus 3.
【００３３】このように、ボイラ５にて天然ガス４を窒
素を含まない純粋な酸素２で燃焼させることにより、排
ガス６中の二酸化炭素７の割合が約９０％にまで高めら
れる。Thus, by burning the natural gas 4 with the pure oxygen 2 which does not contain nitrogen in the boiler 5, the ratio of carbon dioxide 7 in the exhaust gas 6 can be increased to about 90%.
【００３４】そして、二酸化炭素回収設備８で、二酸化
炭素７を９０％含むボイラ５の排ガス６から二酸化炭素
７を回収させる。Then, the carbon dioxide recovery facility 8 recovers the carbon dioxide 7 from the exhaust gas 6 of the boiler 5 containing 90% of carbon dioxide 7.
【００３５】すると、ボイラ５の排ガス６中には、上記
したように９０％と高濃度の二酸化炭素７が含まれてい
るので、排ガス６から容易に二酸化炭素７を回収するこ
とができるようになる。Then, since the exhaust gas 6 of the boiler 5 contains carbon dioxide 7 with a high concentration of 90% as described above, the carbon dioxide 7 can be easily recovered from the exhaust gas 6. Become.
【００３６】尚、排ガスダクト１３から排出された排ガ
ス６の一部は、排ガス循環ファン１５により、排ガス循
環路１４を介してボイラ５へ送られ、排ガス６で酸素２
を希釈することにより、酸素２による天然ガス４の燃焼
温度が高くなりすぎないようにするのに使用される。A part of the exhaust gas 6 discharged from the exhaust gas duct 13 is sent to the boiler 5 via the exhaust gas circulation passage 14 by the exhaust gas circulation fan 15, and the exhaust gas 6 contains oxygen 2
Is used to prevent the combustion temperature of the natural gas 4 from oxygen 2 from becoming too high.
【００３７】上記酸素製造装置３の詳細な作動は、以下
の通りである。The detailed operation of the oxygen production apparatus 3 is as follows.
【００３８】先ず、図２に示すように、吸入塔１７から
吸入された原料となる空気１は、空気流路１６を通り、
空気濾過器１８で除塵された後、ターボ式の空気圧縮機
１９で約５ａｔの圧力に圧縮される。圧縮後の空気１は
空気流路１６を介して水洗冷却塔２４へ送られ、水洗冷
却塔２４で、水ポンプ２０及び水循環流路２１を介して
冷水塔２２との間を循環される冷水２３により冷却され
た後、空気流路１６を介して２本１組の蓄冷槽２５を備
えた２組の蓄冷器２７のそれぞれの一方の蓄冷槽２５へ
送入される。このとき、後述する不純窒素２６が、窒素
流路４７を介して、各蓄冷器２７の他方の蓄冷槽２５へ
反対方向から流入される。そして、一定時間が経過する
と、各組の蓄冷器２７における原料となる空気１と不純
窒素２６はバルブ５０，５１により周期的に切替わる。
更に、蓄冷器２７内部に設けられた蛇管４４へ、後述す
る酸素２が酸素流路４５を介して供給される。その後、
酸素２は蓄冷器２７で加温されて常温となり、酸素圧縮
機４６で必要な圧力に調整された後、酸素供給路１１か
らボイラ５へと送られる。First, as shown in FIG. 2, the air 1 as the raw material sucked from the suction tower 17 passes through the air flow path 16,
After the dust is removed by the air filter 18, it is compressed to a pressure of about 5 at by a turbo type air compressor 19. The compressed air 1 is sent to the washing / cooling tower 24 via the air flow passage 16, and in the washing / cooling tower 24, the cold water 23 circulated between the water pump 20 and the cold water tower 22 via the water circulation passage 21. After being cooled by, the air is supplied to one of the cool storage tanks 25 of each of the two sets of regenerators 27 provided with one set of the cool storage tanks 25 via the air flow path 16. At this time, impure nitrogen 26 described later flows from the opposite direction to the other cold storage tank 25 of each cold storage device 27 via the nitrogen flow path 47. Then, after a lapse of a certain time, the air 1 as a raw material and the impure nitrogen 26 in the regenerators 27 of each set are periodically switched by the valves 50 and 51.
Further, oxygen 2 described later is supplied to the flexible pipe 44 provided inside the regenerator 27 via the oxygen flow path 45. afterwards,
The oxygen 2 is heated in the regenerator 27 to reach normal temperature, adjusted to a required pressure by the oxygen compressor 46, and then sent from the oxygen supply path 11 to the boiler 5.
【００３９】こうして、常温で約５ａｔの圧力に圧縮さ
れた空気１は、蓄冷器２７を通る間に冷却され、蓄冷槽
２５内で、不純物である水分や空気中に含まれているわ
ずかな二酸化炭素を氷結分離されると共に、約−１７０
℃になって、空気流路１６から複精留塔３０の下部塔２
９へ送られる。Thus, the air 1 compressed to a pressure of about 5 at room temperature is cooled while passing through the regenerator 27, and in the regenerator tank 25, a slight amount of impurities such as moisture and air contained in the air. The carbon is separated by freezing and is about -170.
℃, the lower tower 2 of the double rectification tower 30 from the air flow path 16
It is sent to 9.
【００４０】尚、このとき、原料となる空気１の一部は
蓄冷槽２５の中間における空気１が−１２０〜−１３０
℃となる位置から抽気流路３１を介して抽気される。こ
のため、蓄冷器２７下部における原料となる空気１の量
が減少するので、切替えられた次の周期において、不純
窒素２６による空気中に含まれるわずかな二酸化炭素の
除去が完全となる。しかし、抽気された空気１には空気
１の成分量に応じた二酸化炭素がわずかに含まれたまま
なので、吸着材を充填された二酸化炭素吸着器３２で除
去するようにする。二酸化炭素吸着器３２を出た原料と
なる空気１は、蓄冷器２７下部から分岐空気流路３３を
介して分岐される若干の冷却された空気１を混合され、
−１４０〜−１５０℃となって膨張タービン１０へ入
る。膨張タービン１０は、前記したように液化天然ガス
９の冷熱を駆動力に変えて空気１をほぼ複精留塔３０の
上部塔２８圧力まで断熱膨張させ、約−１９０℃とし上
部塔２８へ送入させる。尚、膨張タービン１０へ入れる
前に液化天然ガス９は、過熱器３４で海水３５などによ
って加熱させておく。At this time, a part of the air 1 as a raw material is the air 1 in the middle of the regenerator 25, which is -120 to -130.
Air is extracted from the position at which the temperature reaches 0 ° C. through the extraction passage 31. For this reason, the amount of the raw material air 1 in the lower part of the regenerator 27 is reduced, so that in the next cycle after switching, the impure nitrogen 26 completely removes a slight amount of carbon dioxide contained in the air. However, since the extracted air 1 still contains a small amount of carbon dioxide according to the amount of components of the air 1, the adsorbent is filled with the carbon dioxide adsorber 32 to remove the carbon dioxide. The air 1 as the raw material that has left the carbon dioxide adsorber 32 is mixed with a small amount of the cooled air 1 that is branched from the lower part of the regenerator 27 through the branch air flow path 33,
The temperature becomes −140 to −150 ° C. and enters the expansion turbine 10. As described above, the expansion turbine 10 converts the cold heat of the liquefied natural gas 9 into a driving force to adiabatically expand the air 1 to approximately the pressure of the upper column 28 of the double rectification column 30, and sends it to the upper column 28 at about -190 ° C. Let in. The liquefied natural gas 9 is heated in the superheater 34 with seawater 35 or the like before being put into the expansion turbine 10.
【００４１】複精留塔３０では下部塔２９にて約５ａｔ
の圧力のもとに蓄冷器２７下部からの空気１を精留す
る。これにより、下部塔２９の上部に純度９８％程度の
液体窒素３６が分離され、又、下部塔２９の下端に酸素
２を４０％程度含む液体空気３９が分離される。この液
体窒素３６と液体空気３９は、それぞれ流路３７，４０
を介して上部塔２８へ送られて膨張タービン１０からの
空気１と共に、約０．５ａｔの圧力のもとに精留され
る。このとき、原料となる空気１中に含有されるアセチ
レンなどの炭化水素は、流路４０の途中に設けられたア
セチレン吸着器３８や、液酸循環ポンプ４１を備えた液
酸循環流路４３の途中の循環吸着器４２などで吸着分離
される。In the double rectification column 30, about 5 at in the lower column 29.
The air 1 from the lower part of the regenerator 27 is rectified under the pressure of. As a result, liquid nitrogen 36 having a purity of about 98% is separated at the upper part of the lower tower 29, and liquid air 39 containing about 40% of oxygen 2 is separated at the lower end of the lower tower 29. The liquid nitrogen 36 and the liquid air 39 are supplied to the flow paths 37 and 40, respectively.
Is sent to the upper tower 28 via the and is rectified together with the air 1 from the expansion turbine 10 under a pressure of about 0.5 at. At this time, hydrocarbons such as acetylene contained in the raw material air 1 are acetylene adsorber 38 provided in the middle of the flow passage 40 and liquid acid circulation flow passage 43 provided with a liquid acid circulation pump 41. It is adsorbed and separated by the circulation adsorber 42 or the like on the way.
【００４２】この結果、上部塔２８の下部より純度９
９．６〜９９．８％の酸素２が分離され、該酸素２は酸
素流路４５を介して前記蓄冷器２７へ送られて、蓄冷器
２７内の蛇管４４で加温された後、上記したようにボイ
ラ５へ送られる。As a result, the purity of the lower part of the upper tower 28 is 9
After 9.6 to 99.8% of oxygen 2 is separated, the oxygen 2 is sent to the regenerator 27 through the oxygen flow path 45 and heated by the flexible pipe 44 in the regenerator 27, It is sent to the boiler 5 as described above.
【００４３】一方、不純窒素２６は９６〜９８％の純度
で上部塔２８の上部より分離され、窒素流路４７を通
り、過冷器４８、液化器４９を経て蓄冷器２７に至る。
蓄冷器２７で不純窒素２６は、蓄冷槽２５内に氷結した
二酸化炭素７や水分を昇華吸収すると共に、温度が上昇
されて蓄冷器２７を出る。次に、不純窒素２６は冷水塔
２２に至り、水を冷却して冷水２３とするのに利用され
た後、大気へ放出される。On the other hand, the impure nitrogen 26 is separated from the upper part of the upper column 28 with a purity of 96 to 98%, passes through the nitrogen flow path 47, passes through the subcooler 48 and the liquefier 49, and reaches the regenerator 27.
In the regenerator 27, the impure nitrogen 26 sublimates and absorbs the carbon dioxide 7 and water that have frozen in the regenerator tank 25, and the temperature is raised to exit the regenerator 27. Next, the impure nitrogen 26 reaches the cold water tower 22, is used to cool the water into the cold water 23, and is then released to the atmosphere.
【００４４】尚、本発明は、上述の実施の形態にのみ限
定されるものではなく、本発明の要旨を逸脱しない範囲
内において種々変更を加え得ることは勿論である。The present invention is not limited to the above-described embodiments, and it goes without saying that various modifications can be made without departing from the gist of the present invention.
【００４５】[0045]
【発明の効果】以上説明したように、本発明のＬＮＧ火
力設備によれば、発生する二酸化炭素を経済的に回収す
ることができるという優れた効果を奏し得る。As described above, according to the LNG thermal power plant of the present invention, the excellent effect that the generated carbon dioxide can be economically recovered can be obtained.
【図１】本発明の実施の形態の一例の概略系統図であ
る。FIG. 1 is a schematic system diagram of an example of an embodiment of the present invention.
【図２】図１の酸素製造装置の系統図である。FIG. 2 is a system diagram of the oxygen production device of FIG.
１ 空気 ２ 酸素 ３ 酸素製造装置 ４ 天然ガス ５ ボイラ ９ 液化天然ガス １０ 膨張タービン ２８ 上部塔 ３０ 複精留塔 1 Air 2 Oxygen 3 Oxygen Production Device 4 Natural Gas 5 Boiler 9 Liquefied Natural Gas 10 Expansion Turbine 28 Upper Tower 30 Double Fractionation Tower
Claims (2)
と、天然ガスを酸素製造装置からの酸素で燃焼させるボ
イラとを設けると共に、液化天然ガスの冷熱を酸素製造
装置の動力源の一部として使用した後、液化天然ガスが
気化してなる天然ガスをボイラの燃料として利用するよ
う構成したことを特徴とするＬＮＧ火力設備。1. An oxygen producing device for separating oxygen from air and a boiler for burning natural gas with oxygen from the oxygen producing device are provided, and the cold heat of liquefied natural gas is used as a part of a power source of the oxygen producing device. An LNG thermal power plant characterized in that natural gas obtained by vaporizing liquefied natural gas after use is used as fuel for a boiler.
おける複精留塔の上部塔へ直接供給する空気を断熱膨張
させるための膨張タービンの駆動源として利用するよう
にした請求項１記載のＬＮＧ火力設備。2. The cold heat of liquefied natural gas is used as a drive source of an expansion turbine for adiabatically expanding the air directly supplied to the upper column of the double rectification column in the oxygen production apparatus. LNG thermal power equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7307373A JPH09145003A (en) | 1995-11-27 | 1995-11-27 | Lng fire power installation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7307373A JPH09145003A (en) | 1995-11-27 | 1995-11-27 | Lng fire power installation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09145003A true JPH09145003A (en) | 1997-06-06 |
Family
ID=17968287
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7307373A Pending JPH09145003A (en) | 1995-11-27 | 1995-11-27 | Lng fire power installation |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH09145003A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001221429A (en) * | 2000-02-09 | 2001-08-17 | Nippon Sanso Corp | Apparatus and method for supplying oxygen to oxygen combusting facility |
| CN101893252A (en) * | 2010-07-18 | 2010-11-24 | 赵军政 | High-efficient, energy-saving and environment-friendly thermal power generating unit |
| JP2011169570A (en) * | 2010-02-22 | 2011-09-01 | Jfe Steel Corp | Sintering machine |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0448185A (en) * | 1990-06-14 | 1992-02-18 | Central Res Inst Of Electric Power Ind | Recovering method of carbon dioxide discharged out of lng burning thermal power station |
| JPH06123553A (en) * | 1992-10-08 | 1994-05-06 | Osaka Gas Co Ltd | Method and device for separating air incorporating power generation equipment utilizing cold of liquefied natural gas |
-
1995
- 1995-11-27 JP JP7307373A patent/JPH09145003A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0448185A (en) * | 1990-06-14 | 1992-02-18 | Central Res Inst Of Electric Power Ind | Recovering method of carbon dioxide discharged out of lng burning thermal power station |
| JPH06123553A (en) * | 1992-10-08 | 1994-05-06 | Osaka Gas Co Ltd | Method and device for separating air incorporating power generation equipment utilizing cold of liquefied natural gas |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001221429A (en) * | 2000-02-09 | 2001-08-17 | Nippon Sanso Corp | Apparatus and method for supplying oxygen to oxygen combusting facility |
| JP2011169570A (en) * | 2010-02-22 | 2011-09-01 | Jfe Steel Corp | Sintering machine |
| CN101893252A (en) * | 2010-07-18 | 2010-11-24 | 赵军政 | High-efficient, energy-saving and environment-friendly thermal power generating unit |
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