JP2001221429A - Apparatus and method for supplying oxygen to oxygen combusting facility - Google Patents
Apparatus and method for supplying oxygen to oxygen combusting facilityInfo
- Publication number
- JP2001221429A JP2001221429A JP2000031604A JP2000031604A JP2001221429A JP 2001221429 A JP2001221429 A JP 2001221429A JP 2000031604 A JP2000031604 A JP 2000031604A JP 2000031604 A JP2000031604 A JP 2000031604A JP 2001221429 A JP2001221429 A JP 2001221429A
- Authority
- JP
- Japan
- Prior art keywords
- oxygen
- steam
- generated
- facility
- 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
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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04036—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of oxygen
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
- F25J3/04121—Steam turbine as the prime mechanical driver
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—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
- 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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
- Air Supply (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、酸素燃焼設備への
酸素供給装置及び供給方法に関し、特に、中・小型規模
の産業用の酸素燃焼設備への酸素供給装置及び供給方法
に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an apparatus and a method for supplying oxygen to an oxyfuel facility, and more particularly to an apparatus and a method for supplying oxygen to an industrial oxyfuel facility of a medium or small scale.
【０００２】[0002]
【従来の技術】金属やガラス溶融などに用いられていた
従来の酸素を支燃性ガスとする酸素燃焼設備では、生成
する熱量を充分に有効利用していなかった。産業用ボイ
ラーは、空気燃焼方式であったが、ボイラーの高性能化
が要求されてきた。このため、ボイラーを酸素燃焼方式
にして、ボイラーの燃焼エネルギー効率を高めるととも
に、ボイラーのコンパクト化による設備コストの低減を
図るようにしている。また、ゴミの燃焼や溶融において
も、ダイオキシンの発生の問題から酸素燃焼方式の採用
が検討されつつある。しかし、このような酸素燃焼設備
への酸素供給装置は、動力源として電動機駆動が一般的
であった。2. Description of the Related Art In a conventional oxyfuel combustion system using oxygen as a combustion supporting gas, which has been used for melting metals and glass, the amount of heat generated has not been sufficiently utilized. Industrial boilers are of the air combustion type, but high performance boilers have been required. For this reason, the boiler is changed to an oxyfuel combustion system to increase the combustion energy efficiency of the boiler and to reduce the equipment cost by downsizing the boiler. Also, in the burning and melting of refuse, the use of an oxyfuel combustion method is being studied due to the problem of dioxin generation. However, such an oxygen supply device for oxyfuel combustion equipment is generally driven by an electric motor as a power source.
【０００３】一方、酸素燃焼方式の場合は、酸素供給手
段が必要になる。この供給手段としては、タンクに貯蔵
した液化酸素をガス化して供給する手段と、空気分離装
置で酸素ガスを製造して供給する手段とがある。On the other hand, in the case of the oxyfuel combustion system, an oxygen supply means is required. As the supply means, there are means for gasifying and supplying liquefied oxygen stored in the tank, and means for producing and supplying oxygen gas by an air separation device.
【０００４】[0004]
【発明が解決しようとする課題】しかしながら、液化酸
素をガス化して供給する手段は、貯蔵タンクまで液化酸
素をタンクローリーで搬送する手間が掛かるため、空気
分離装置で製造した酸素ガスを配管を介して酸素燃焼設
備に供給して使用することが至便であった。この空気分
離装置としては、圧力変動吸着式や深冷式が広く知られ
ている。However, the means for gasifying and supplying liquefied oxygen requires time for transporting the liquefied oxygen to the storage tank by a tank lorry, so that the oxygen gas produced by the air separation device is supplied through a pipe. It was convenient to supply it to an oxygen combustion facility for use. As the air separation device, a pressure fluctuation adsorption type and a cryogenic type are widely known.
【０００５】ところが、圧力変動吸着式空気分離装置
は、３塔真空再生式の場合、一般に、原料空気を吸着筒
に送り込むための原料空気ブロワ、分離した酸素ガスを
酸素燃焼設備に送るための酸素圧縮機及び吸着筒の再生
のために使用される真空ポンプが、一般に電動機で駆動
されており、例えば、９３％濃度の酸素ガスを製造する
場合、酸素ガスの製造に要する電力は、原料空気ブロワ
で約０．０３ｋＷｈ／Ｎｍ３、真空ポンプで約０．３８
ｋＷｈ／Ｎｍ３、そして酸素圧縮機で約０．１ｋＷｈ／
Ｎｍ３程度である。[0005] However, in the case of a three-column vacuum regeneration system, a pressure fluctuation adsorption type air separation device generally has a raw air blower for feeding raw air to an adsorption column, and an oxygen blower for feeding separated oxygen gas to an oxygen combustion facility. A vacuum pump used for regeneration of a compressor and an adsorption column is generally driven by an electric motor. For example, when producing 93% -concentration oxygen gas, electric power required for producing oxygen gas is supplied from a raw material air blower. About 0.03 kWh / Nm 3 and about 0.38 with a vacuum pump
kWh / Nm 3 , and about 0.1 kWh /
Is a Nm 3 about.
【０００６】また、大気圧再生式の場合は、真空ポンプ
無しで再生するので、真空ポンプの動力は不要となる
が、吸着圧力と再生圧力との圧力差を大きくするため、
原料空気の供給圧力を高めなければならず、原料空気圧
縮機の動力が大きくなる。In the case of the atmospheric pressure regeneration type, since the regeneration is performed without a vacuum pump, the power of the vacuum pump is not required, but the pressure difference between the adsorption pressure and the regeneration pressure is increased.
The supply pressure of the raw air must be increased, and the power of the raw air compressor increases.
【０００７】一方、深冷式空気分離装置は、一般に、原
料空気を精留操作圧力に昇圧する原料空気圧縮機や、分
離した酸素ガスを酸素供給設備に送るための酸素圧縮機
を電動機で駆動しており、例えば、９３％濃度の酸素ガ
スを製造する場合、酸素ガスの製造に要する電力は、原
料空気圧縮機で約０．３３ｋＷｈ／Ｎｍ３、酸素圧縮機
で約０．１ｋＷｈ／Ｎｍ３程度となる。[0007] On the other hand, a cryogenic air separation apparatus generally uses a motor to drive a raw air compressor for raising the raw air to a rectifying operation pressure or an oxygen compressor for sending separated oxygen gas to an oxygen supply facility. and is, for example, when manufacturing a 93% concentration of oxygen gas, electric power required for the production of oxygen gas, about 0.33kWh / Nm 3 in the feed air compressor, about 0.1 kWh / Nm 3 oxygen compressor About.
【０００８】そこで本発明は、圧力変動吸着式の原料空
気ブロワ、酸素圧縮機や真空ポンプ、深冷式の原料空気
圧縮機や酸素圧縮機等の酸素製造装置に用いられる回転
機を蒸気タービンで駆動して、使用電力を節約できる酸
素燃焼設備への酸素供給装置及び供給方法を提供するこ
とを目的としている。Accordingly, the present invention provides a steam turbine for rotating a rotary machine used for an oxygen production apparatus such as a pressure fluctuation adsorption type material air blower, an oxygen compressor or a vacuum pump, or a cryogenic type material air compressor or an oxygen compressor. It is an object of the present invention to provide an oxygen supply apparatus and a supply method for an oxyfuel facility that can be driven to save power consumption.
【０００９】[0009]
【課題を解決するための手段】上記目的を達成する本発
明の酸素供給装置は、酸素を支燃性ガスとする酸素燃焼
設備と、該酸素燃焼設備で生成した熱量を熱源とするボ
イラーと、該ボイラーで発生した蒸気を駆動源として動
力を発生する蒸気タービンと、該蒸気タービンで発生し
た動力により駆動する回転機を設けた酸素製造装置と、
該酸素製造装置で製造した酸素を前記酸素燃焼設備に供
給する酸素ガス供給経路とを備えたことを特徴とし、酸
素供給方法は、酸素を支燃性ガスとする酸素燃焼設備で
生成した熱量を熱源としてボイラーで製品蒸気圧よりも
高い圧力の蒸気を発生させ、この発生蒸気で蒸気タービ
ンを駆動して動力を発生し、該発生動力により酸素製造
装置に設けた回転機を駆動し、該酸素製造装置で製造し
た酸素を酸素ガス供給経路を介して前記酸素燃焼設備に
供給することを特徴としている。According to the present invention, there is provided an oxygen supply system comprising: an oxygen combustion facility using oxygen as a supporting gas; a boiler using a heat generated by the oxygen combustion facility as a heat source; A steam turbine that generates power using the steam generated by the boiler as a driving source, and an oxygen production apparatus that includes a rotating machine that is driven by the power generated by the steam turbine;
An oxygen gas supply path for supplying oxygen produced by the oxygen production apparatus to the oxyfuel combustion facility, wherein the oxygen supply method comprises: A steam having a pressure higher than the product steam pressure is generated by a boiler as a heat source, and the generated steam drives a steam turbine to generate power, and the generated power drives a rotary machine provided in an oxygen production apparatus to generate oxygen. The method is characterized in that oxygen produced by the production apparatus is supplied to the oxygen combustion equipment via an oxygen gas supply path.
【００１０】[0010]
【発明の実施の形態】図１は酸素製造装置が圧力変動吸
着式である場合の本発明の第１形態例を示す系統図、図
２は同じく深冷式である場合の本発明の第２形態例を示
す系統図である。DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 is a system diagram showing a first embodiment of the present invention when an oxygen production apparatus is of a pressure fluctuation adsorption type, and FIG. 2 is a second embodiment of the present invention when the oxygen production apparatus is also of a cryogenic type. It is a system diagram showing an example of a form.
【００１１】まず、図１及び２において、酸素を支燃性
ガスとする酸素燃焼設備１には、ボイラー１ａが付設さ
れ、さらに、重油等の燃料供給経路２と、支燃用の酸素
ガス供給経路３とが接続され、ボイラー１ａには、給水
タンク４及び熱交換器５を有する給水経路６と、製品蒸
気送出経路７と、排ガス経路８とが接続されている。ま
た、補給水タンク９及び熱交換器１０を有する補給水経
路１１が給水タンク４に接続している。前記排ガス経路
８の排ガスは、熱交換器５の熱媒体として使用された
後、さらに熱交換器１０の熱媒体として使用されてから
排気される。First, in FIGS. 1 and 2, a boiler 1a is attached to an oxyfuel combustion facility 1 using oxygen as a supporting gas, and a fuel supply path 2 for heavy oil or the like and an oxygen gas supply for supporting. The path 3 is connected, and a water supply path 6 having a water supply tank 4 and a heat exchanger 5, a product steam delivery path 7, and an exhaust gas path 8 are connected to the boiler 1a. A makeup water path 11 having a makeup water tank 9 and a heat exchanger 10 is connected to the water supply tank 4. The exhaust gas in the exhaust gas path 8 is exhausted after being used as a heat medium of the heat exchanger 10 after being used as a heat medium of the heat exchanger 5.
【００１２】したがって、給水経路６を介してボイラー
１ａに送られた供給水は、酸素燃焼装置１での燃料と酸
素ガスとの燃焼熱によって加熱され蒸気となって、製品
蒸気送出経路７を介して使用先へ送給される。燃焼によ
って生じた排ガスは、ボイラー１ａを経て排ガス経路８
から熱交換器５に導入されて、給水タンク４からボイラ
ー１ａに送られる供給水を加熱し、さらに、熱交換器１
０に導入されて、補給水タンク９から給水タンク４に補
給される補給水を加熱する。Therefore, the supply water sent to the boiler 1a via the water supply path 6 is heated by the heat of combustion of the fuel and the oxygen gas in the oxycombustion device 1 to be turned into steam, and is supplied through the product steam delivery path 7. To be used. The exhaust gas generated by the combustion passes through the boiler 1a and passes through an exhaust gas path 8
From the feed water tank 4 to the boiler 1a to heat the supply water.
0, and heats the make-up water supplied from the make-up water tank 9 to the water supply tank 4.
【００１３】次に、図１に基づいて、前記酸素燃焼設備
１と該設備１に供給される酸素ガスを製造する酸素製造
装置の１つである圧力変動吸着式空気分離装置（ＰＳＡ
装置）とを組み合わせた酸素燃焼設備への酸素供給装置
の第１形態例について説明する。Next, based on FIG. 1, the pressure fluctuation adsorption type air separation apparatus (PSA) which is one of the oxygen combustion equipment 1 and an oxygen production apparatus for producing oxygen gas supplied to the equipment 1 will be described.
A first embodiment of an apparatus for supplying oxygen to oxycombustion equipment, which is a combination of the apparatus and the apparatus, will be described.
【００１４】このＰＳＡ装置２０は、３塔真空再生式で
あって、吸着筒２１ａ，２１ｂ，２１ｃを吸着工程，再
生工程，加圧工程に順次切換えることにより、窒素と酸
素とを分離し、酸素を連続的に製造するものであって、
経路２２から吸入して原料空気ブロワ２３で昇圧した大
気を吸着工程にある吸着筒に導入し、該吸着筒内に充填
した吸着剤に窒素を吸着させ、分離した酸素ガスを経路
２４に導出する。経路２４に導出した酸素ガスは、酸素
圧縮機３０で圧縮された後、アキュームレータ３１及び
流量制御装置３２を経て、酸素ガス供給経路３から燃料
支燃用として酸素燃焼設備１に供給される。また、再生
工程にある吸着筒は、真空ポンプ２５により経路２６を
介して当該吸着筒内を真空排気することにより行われ
る。なお、このような構成のＰＳＡ装置は従来から存在
する典型的なものであるので、弁等の詳細な構成要素に
ついて省略している。The PSA apparatus 20 is of a three-column vacuum regeneration type, in which nitrogen and oxygen are separated by sequentially switching the adsorption columns 21a, 21b, 21c to an adsorption step, a regeneration step, and a pressurization step. Is manufactured continuously,
The air sucked from the passage 22 and pressurized by the raw material air blower 23 is introduced into the adsorption column in the adsorption step, nitrogen is adsorbed by the adsorbent filled in the adsorption column, and the separated oxygen gas is led out to the line 24. . After being compressed by the oxygen compressor 30, the oxygen gas led out to the path 24 is supplied to the oxygen combustion equipment 1 through the accumulator 31 and the flow rate control device 32 from the oxygen gas supply path 3 for fuel support. The adsorption cylinder in the regeneration step is evacuated by vacuum pump 25 through a path 26 to evacuate the interior of the adsorption cylinder. Since a PSA device having such a configuration is a typical one existing in the related art, detailed components such as valves are omitted.
【００１５】そして、上記形態例では、動力の大きい真
空ポンプ２５の駆動にのみ蒸気タービン１２の動力を使
用して、消費電力の低減を図っている。すなわち、ボイ
ラー１ａから製品蒸気送出経路７を介して使用先に向か
う製品蒸気を、その途中で蒸気タービン１２に導入する
ことによって真空ポンプ２５を駆動している。この場
合、真空ポンプ２５を駆動した製品蒸気は、この駆動に
よりエネルギーが消費されて使用先に送られるため、ボ
イラー１ａでは、それに見合うように、製品蒸気圧より
も高い圧力の蒸気を発生させている。In the above embodiment, the power of the steam turbine 12 is used only for driving the vacuum pump 25 having a large power, thereby reducing power consumption. That is, the vacuum pump 25 is driven by introducing the product steam from the boiler 1a to the use destination via the product steam delivery path 7 into the steam turbine 12 on the way. In this case, since the product steam driven by the vacuum pump 25 consumes energy by this drive and is sent to the place of use, the boiler 1a generates steam having a pressure higher than the product steam pressure to match the consumption. I have.
【００１６】なお、ＰＳＡ装置２０のもう一つの回転機
である原料空気ブロワ２３や、酸素圧縮機３０にも蒸気
タービンを適用することは可能であるが、これらに必要
な動力、例えば電力は、９３％濃度の酸素ガスを製造す
る場合で、真空ポンプ２５が約０．３８ｋＷｈ／Ｎｍ３
程度であるのに比べて、原料空気ブロワ２３が約０．０
３ｋＷｈ／Ｎｍ３、酸素圧縮機３０が約０．１ｋＷｈ／
Ｎｍ３程度と小さいので、装置コスト、即ち初期投資額
との兼ね合いで、モーター駆動とするかどうかを選定す
ればよい。Although the steam turbine can be applied to the raw air blower 23 and the oxygen compressor 30 which are the other rotating machines of the PSA apparatus 20, the power required for these, for example, the electric power is When producing 93% oxygen gas, the vacuum pump 25 is operated at about 0.38 kWh / Nm 3.
The raw material air blower 23 is about 0.0
3 kWh / Nm 3 , and the oxygen compressor 30 is about 0.1 kWh /
Since it is as small as about Nm 3, it is sufficient to select whether or not to use the motor drive in consideration of the apparatus cost, that is, the initial investment amount.
【００１７】次に、図２に基づいて、前記酸素燃焼設備
１と該設備１に供給される酸素ガスを製造する酸素製造
装置の別の１つである深冷式空気分離装置とを組み合わ
せた酸素燃焼設備への酸素供給装置の第２形態例につい
て説明する。Next, based on FIG. 2, the oxy-combustion facility 1 and a cryogenic air separation apparatus, which is another oxygen production apparatus for producing oxygen gas supplied to the facility 1, are combined. A description will be given of a second embodiment of the oxygen supply device for the oxygen combustion equipment.
【００１８】この深冷式空気分離装置４０は、原料空気
圧縮機４１で圧縮されて冷却器４２で冷却された原料空
気を精製する精製設備４３と、原料空気を冷却する主熱
交換器４４と、原料空気の一部を断熱膨張させて寒冷を
発生する膨張タービン４５と、原料空気を精留して酸素
を分離するための高圧塔（下部塔）４６，低圧塔（上部
塔）４７及び主凝縮蒸発器４８からなる複精留塔４９
と、過冷器５０，減圧弁５１，５２等とを主要な構成要
素としている。The cryogenic air separation device 40 includes a purification equipment 43 for purifying raw air compressed by a raw air compressor 41 and cooled by a cooler 42, a main heat exchanger 44 for cooling raw air, and An expansion turbine 45 for adiabatically expanding a part of the raw air to generate cold, a high-pressure tower (lower tower) 46, a low-pressure tower (upper tower) 47 for rectifying the raw air, and separating oxygen. Double rectification column 49 consisting of condensation evaporator 48
And the subcooler 50, the pressure reducing valves 51 and 52, and the like as main components.
【００１９】原料空気圧縮機４１で圧縮された原料空気
は、精製設備４３で水分や二酸化炭素等の不純物が除去
されて精製され、主熱交換器４４で冷却された後、一部
が膨張タービン４５を介して低圧塔４７に、残部が高圧
塔４６にそれぞれ導入され、複精留塔４９で液化精留分
離されて低圧塔４７上部の窒素ガスと、下部の液化酸素
とに分離する。この液化酸素は、主凝縮蒸発器４８で高
圧塔４６からの窒素ガスにより加熱されて蒸発し、酸素
ガスとなる。この酸素ガスの一部は、低圧塔４７の下部
から経路５３に抜き出され、主熱交換器４４で常温に戻
って経路５４に導出され、該経路５４を通って酸素圧縮
機３０に導入される。酸素圧縮機３０で圧縮された酸素
ガスは、アキュームレータ３１及び流量制御装置３２を
経て、酸素ガス供給経路３から燃料支燃用として酸素燃
焼設備１に供給される。なお、このような構成の深冷式
空気分離装置は従来から存在する典型的なものであるの
で、弁等の詳細な構成要素について省略している。The raw material air compressed by the raw material air compressor 41 is purified by removing impurities such as moisture and carbon dioxide in a purifying facility 43, cooled in a main heat exchanger 44, and partially expanded in an expansion turbine. The mixture is introduced into the low-pressure column 47 through 45, and the remainder is introduced into the high-pressure column 46, and is liquefied and rectified and separated in the double rectification column 49 to be separated into nitrogen gas in the upper portion of the low-pressure column 47 and liquefied oxygen in the lower portion. The liquefied oxygen is heated by the nitrogen gas from the high-pressure column 46 in the main condensing evaporator 48 and evaporates to become oxygen gas. A part of this oxygen gas is extracted from the lower part of the low-pressure column 47 to the path 53, returned to room temperature by the main heat exchanger 44, led out to the path 54, and introduced into the oxygen compressor 30 through the path 54. You. The oxygen gas compressed by the oxygen compressor 30 is supplied from the oxygen gas supply path 3 to the oxyfuel combustion facility 1 through the accumulator 31 and the flow rate control device 32 for fuel support. Note that the cryogenic air separation device having such a configuration is a typical one existing in the related art, and detailed components such as valves are omitted.
【００２０】そして、上記形態例では、９３％濃度の酸
素ガスを製造する場合の電力が、約０．３３ｋＷｈ／Ｎ
ｍ３程度の原料空気圧縮機４１の駆動に蒸気タービン１
２の動力を、約０．１ｋＷｈ／Ｎｍ３程度の酸素圧縮機
３０の駆動に蒸気タービン１２ａの動力を使用して、消
費電力の低減を図っている。すなわち、ボイラー１ａか
ら製品蒸気送出経路７を介して使用先に向かう製品蒸気
を、その途中で蒸気タービン１２に導入することによっ
て原料空気圧縮機４１を駆動するとともに、蒸気タービ
ン１２の手前で製品蒸気送出経路７から分岐した分岐経
路７ａを介して使用先に向かう製品蒸気を、その途中で
蒸気タービン１２ａに導入することによって酸素圧縮機
３０を駆動している。この場合、原料空気圧縮機４１及
び酸素圧縮機３０を駆動した製品蒸気は、これらの駆動
によりエネルギーが消費されて使用先に送られるため、
ボイラー１ａでは、それに見合うように、製品蒸気圧よ
りも高い圧力の蒸気を発生させている。In the above embodiment, the power for producing 93% oxygen gas is about 0.33 kWh / N.
m steam turbine 1 to drive a 3 degree of feed air compressor 41
The power of No. 2 is used to drive the oxygen compressor 30 of about 0.1 kWh / Nm 3 to reduce the power consumption by using the power of the steam turbine 12a. That is, the raw material air compressor 41 is driven by introducing the product steam from the boiler 1a to the use destination via the product steam delivery path 7 into the steam turbine 12 on the way, and the product steam is supplied before the steam turbine 12 The oxygen compressor 30 is driven by introducing product steam toward a use destination via a branch path 7a branched from the delivery path 7 into the steam turbine 12a on the way. In this case, the product steam that drives the raw air compressor 41 and the oxygen compressor 30 consumes energy by these drives and is sent to the use destination.
In the boiler 1a, steam having a pressure higher than the product steam pressure is generated correspondingly.
【００２１】なお、上記両形態例では、蒸気タービンを
出た蒸気全量を使用先に供給しているが、必ずしもこれ
に限定されるものではない。例えば、蒸気タービンで製
品蒸気よりも低圧まで膨張させて、給水タンク４等に戻
すようにしてもよいし、蒸気タービン等の回転機の駆動
に使用した後に廃棄してもよい。また、上記両形態例で
は、ボイラー１ａは、酸素燃焼設備１に付設されている
ものとしたが、酸素燃焼設備がボイラーの加熱釜とし
て、ボイラーに付設されていてもよい。さらに、ボイラ
ーは、酸素燃焼により発生した熱量の全部又は一部を利
用して蒸気を発生することができる。In both of the above embodiments, the entire amount of steam exiting the steam turbine is supplied to the user, but the invention is not necessarily limited to this. For example, the steam may be expanded to a pressure lower than the product steam by the steam turbine and returned to the water supply tank 4 or the like, or may be discarded after being used for driving a rotating machine such as a steam turbine. Further, in both of the above embodiments, the boiler 1a is attached to the oxyfuel combustion facility 1, but the oxyfuel combustion facility may be attached to the boiler as a heating pot of the boiler. Further, the boiler can generate steam using all or a part of the heat generated by the oxyfuel combustion.
【００２２】[0022]
【実施例】酸素を支燃性ガスとする酸素燃焼設備を加熱
釜として付設した酸素燃焼ボイラーの発生蒸気を利用し
て、酸素量として１５００Ｎｍ３／ｈを製造する３塔圧
力変動吸着式空気分離装置の真空ポンプを駆動させた。DESCRIPTION OF THE PREFERRED EMBODIMENTS Three-column pressure fluctuation adsorption type air separation system producing 1500 Nm 3 / h as an oxygen amount by using steam generated from an oxyfuel boiler provided with an oxyfuel combustion facility using oxygen as a supporting gas as a heating pot. The vacuum pump of the device was turned on.
【００２３】酸素量１５００Ｎｍ３／ｈを用いて酸素燃
焼ボイラーで２．５ＭＰａ、５４３Ｋの過熱蒸気（２９
４０ｋＪ／ｋｇ）を１０トン／ｈ発生させ、発生蒸気の
全量を背圧蒸気タービンに供給して真空ポンプを駆動さ
せた。背圧蒸気タービン出口の蒸気（１０トン／ｈ）は
０．４ＭＰａの飽和蒸気（４１３Ｋ、２７４０ｋＪ／ｋ
ｇ）となり、製品蒸気として回収した。Using an oxygen combustion boiler with an oxygen amount of 1500 Nm 3 / h, superheated steam of 2.5 MPa, 543 K (29
(40 kJ / kg) was generated at 10 tons / h, and the entire amount of generated steam was supplied to a back-pressure steam turbine to drive a vacuum pump. The steam (10 tons / h) at the outlet of the back pressure steam turbine is saturated steam of 0.4 MPa (413 K, 2740 kJ / k).
g) and recovered as product vapor.
【００２４】酸素量として１５００Ｎｍ３／ｈを製造す
る圧力変動吸着式空気分離装置は、空気ブロワーが電動
機駆動（５５ｋＷ）で、真空ポンプを出力５５０ｋＷの
蒸気タービンで駆動させた。In the pressure fluctuation adsorption type air separation device for producing 1500 Nm 3 / h as the oxygen amount, the air blower was driven by an electric motor (55 kW), and the vacuum pump was driven by a steam turbine having an output of 550 kW.
【００２５】エネルギー単位の換算値としては、１ｋＷ
・ｈ＝３６００ｋＪ（８６０ｋｃａｌ）であるが、発電
効率や送電ロスを考慮すると電力の使用端におけるエネ
ルギー換算値は１ｋＷ・ｈ＝１０２６０ｋＪ（２４５０
ｋｃａｌ）であるため、従来技術の電動機駆動による真
空ポンプと比較して、その電力換算値は１９５ｋＷと評
価できた。The converted value of the energy unit is 1 kW
H = 3600 kJ (860 kcal), but in consideration of power generation efficiency and transmission loss, the energy conversion value at the end of use of electric power is 1 kW · h = 10260 kJ (2450)
kcal), the power conversion value could be evaluated to be 195 kW as compared with a conventional vacuum pump driven by an electric motor.
【００２６】[0026]
【発明の効果】以上説明したように、本発明によれば、
酸素製造装置に設置されている真空ポンプ、原料空気圧
縮機、酸素圧縮機等の回転機の動力を、酸素燃焼設備の
燃焼熱で発生した蒸気を動力源とする蒸気タービンで賄
うようにしているので、電力の大幅な削減が図れる。As described above, according to the present invention,
The power of rotating machines such as vacuum pumps, raw material air compressors and oxygen compressors installed in the oxygen production equipment is supplied by a steam turbine powered by steam generated by the combustion heat of oxycombustion equipment. As a result, the power can be significantly reduced.
【図１】 酸素製造装置が圧力変動吸着式である場合の
本発明の第１形態例を示す系統図である。FIG. 1 is a system diagram showing a first embodiment of the present invention when an oxygen production apparatus is of a pressure fluctuation adsorption type.
【図２】 同じく深冷式である場合の本発明の第２形態
例を示す系統図である。FIG. 2 is a system diagram showing a second embodiment of the present invention in the case of a cryogenic cooling system.
１…酸素燃焼設備、１ａ…ボイラー、２…燃料供給経
路、３…酸素ガス供給経路、６…給水経路、７…製品蒸
気送出経路、７ａ…分岐経路、１２，１２ａ…蒸気ター
ビン、２０…圧力変動吸着式空気分離装置、２１ａ，２
１ｂ，２１ｃ…吸着筒、２３…原料空気ブロワ、２５…
真空ポンプ、３０…酸素圧縮機、３１…アキュームレー
タ、４０…深冷式空気分離装置、４１…原料空気圧縮
機、４２…冷却器、４３…精製設備、４４…主熱交換
器、４５…膨張タービン、４６…高圧塔（下部塔）、４
７…低圧塔（上部塔）、４８…主凝縮蒸発器、４９…複
精留塔、５０…過冷器、５１，５２…減圧弁DESCRIPTION OF SYMBOLS 1 ... Oxygen combustion equipment, 1a ... Boiler, 2 ... Fuel supply path, 3 ... Oxygen gas supply path, 6 ... Water supply path, 7 ... Product steam delivery path, 7a ... Branch path, 12, 12a ... Steam turbine, 20 ... Pressure Variable adsorption air separation device, 21a, 2
1b, 21c: adsorption cylinder, 23: raw air blower, 25:
Vacuum pump, 30 oxygen compressor, 31 accumulator, 40 cryogenic air separator, 41 raw air compressor, 42 cooler, 43 purification equipment, 44 main heat exchanger, 45 expansion turbine , 46 ... High pressure tower (lower tower), 4
7 low-pressure tower (upper tower), 48 main condensing evaporator, 49 double rectification tower, 50 subcooler, 51, 52 pressure reducing valve
───────────────────────────────────────────────────── フロントページの続き (72)発明者 井上 篤 東京都港区西新橋１丁目16番７号 日本酸 素株式会社内 Ｆターム(参考） 3G081 BA02 BB00 BC07 BD00 DA12 3K023 JA01 4G075 AA05 AA44 BA06 BB02 CA02 DA01 EA06 ────────────────────────────────────────────────── ─── Continued on the front page (72) Inventor Atsushi Inoue 1-16-7 Nishi-Shimbashi, Minato-ku, Tokyo F-term in Nippon Oxide Co., Ltd. (reference) 3G081 BA02 BB00 BC07 BD00 DA12 3K023 JA01 4G075 AA05 AA44 BA06 BB02 CA02 DA01 EA06
Claims (2)
と、該酸素燃焼設備で生成した熱量を熱源とするボイラ
ーと、該ボイラーで発生した蒸気を駆動源として動力を
発生する蒸気タービンと、該蒸気タービンで発生した動
力により駆動する回転機を設けた酸素製造装置と、該酸
素製造装置で製造した酸素を前記酸素燃焼設備に供給す
る酸素ガス供給経路とを備えたことを特徴とする酸素燃
焼設備への酸素供給装置An oxygen combustion facility using oxygen as a supporting gas, a boiler using heat generated by the oxygen combustion facility as a heat source, and a steam turbine generating power using steam generated by the boiler as a drive source. An oxygen producing apparatus provided with a rotating machine driven by power generated by the steam turbine, and an oxygen gas supply path for supplying oxygen produced by the oxygen producing apparatus to the oxyfuel combustion facility. Oxygen supply equipment for oxyfuel combustion equipment
生成した熱量を熱源としてボイラーで製品蒸気圧よりも
高い圧力の蒸気を発生させ、この発生蒸気で蒸気タービ
ンを駆動して動力を発生し、該発生動力により酸素製造
装置に設けた回転機を駆動し、該酸素製造装置で製造し
た酸素を酸素ガス供給経路を介して前記酸素燃焼設備に
供給することを特徴とする酸素燃焼設備への酸素供給方
法。2. A boiler is used to generate steam having a pressure higher than a product steam pressure by using a heat amount generated by an oxyfuel combustion facility using oxygen as a supporting gas, and a steam turbine is driven by the generated steam to generate power. Oxygen combustion equipment, wherein the generated power drives a rotating machine provided in an oxygen production apparatus to supply oxygen produced by the oxygen production apparatus to the oxygen combustion facility via an oxygen gas supply path. How to supply oxygen to
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000031604A JP2001221429A (en) | 2000-02-09 | 2000-02-09 | Apparatus and method for supplying oxygen to oxygen combusting facility |
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|---|---|
| JP2001221429A true JP2001221429A (en) | 2001-08-17 |
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Cited By (5)
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| KR101376717B1 (en) | 2012-04-24 | 2014-03-20 | 두산중공업 주식회사 | IGCC plant using the heat recovery in compressed air process |
| KR101448129B1 (en) | 2013-04-17 | 2014-10-08 | 한국에너지기술연구원 | an organic rankine cycle system and controlling apparatus and method thereof |
| US10543450B2 (en) | 2016-03-25 | 2020-01-28 | Ihi Corporation | Carbon dioxide recovery method and recovery apparatus |
| US10682603B2 (en) | 2016-03-16 | 2020-06-16 | Ihi Corporation | Carbon dioxide recovery method and recovery device |
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| KR101448129B1 (en) | 2013-04-17 | 2014-10-08 | 한국에너지기술연구원 | an organic rankine cycle system and controlling apparatus and method thereof |
| US10682603B2 (en) | 2016-03-16 | 2020-06-16 | Ihi Corporation | Carbon dioxide recovery method and recovery device |
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