JPH0468453B2 - - Google Patents
Info
- Publication number
- JPH0468453B2 JPH0468453B2 JP7637384A JP7637384A JPH0468453B2 JP H0468453 B2 JPH0468453 B2 JP H0468453B2 JP 7637384 A JP7637384 A JP 7637384A JP 7637384 A JP7637384 A JP 7637384A JP H0468453 B2 JPH0468453 B2 JP H0468453B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- cycle
- turbine
- temperature
- corrosive
- 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
- 238000000034 method Methods 0.000 claims description 29
- 238000010521 absorption reaction Methods 0.000 claims description 17
- 238000007254 oxidation reaction Methods 0.000 claims description 15
- 230000008929 regeneration Effects 0.000 claims description 12
- 238000011069 regeneration method Methods 0.000 claims description 12
- 230000003647 oxidation Effects 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 150000002894 organic compounds Chemical class 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 150000001491 aromatic compounds Chemical class 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 6
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 51
- 238000004140 cleaning Methods 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000011156 evaluation Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
- F02C3/26—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension
- F02C3/28—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension using a separate gas producer for gasifying the fuel before combustion
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】
本発明は、芳香族化合物の酸化プロセスオフガ
スの有効利用に関するものであり、詳細には芳香
族化合物の加圧液相酸化プロセスからのタービン
ブレードの高温腐蝕性元素含有有機化合物を含む
加圧オフガスを接触燃焼器にて燃焼させ、該有機
化合物を無機物としたのち、吸収塔で該無機物中
の腐蝕性成分を吸収して、実質的にタービンブレ
ード腐蝕性成分のないクリーンなオフガスとし、
ガスタービンサイクルの加圧作動媒体ガス中に導
入し、該ガスタービンサイクルの作動媒体である
空気の一部として用いるごとくしてなる酸化プロ
セス排ガスからの動力回収法であり、好ましい実
施態様においては、再生ガスタービンサイクルと
して、該クリーンなオフガスをタービン排気と熱
交換して予熱しなるものとして用いること、さら
に、吸収塔を二塔以上設け、後段吸収塔の循環及
び補給水で再生ガスタービンサイクルの低温部の
熱回収を行うごとくにしてなるものである。
芳香族化合物−特にｐ−、ｍ−キシレン等の加
圧液相酸化プロセスからの加圧オフガスは、オフ
ガス中の未反応成分等の有効成分の回収を目的と
して、通常、水による吸収装置を経て排出される
ため、温度は比較的低く通常50℃前後、圧力は10
〜20ata程度である。オフガス中の成分はその殆
どが酸化反応に寄与しなかつた窒素であり、残り
は酸化反応の生成物である炭酸ガス、酸化反応未
利用の酸素、前記した水による吸収装置からの同
伴飽和水蒸気である。また、微量であるが、該オ
フガス中には酸化反応のための触媒成分の元素を
含む有機化合物を含んでおり、この副生物は触媒
成分にもよるが、タービンブレードの高温腐蝕性
成分である、例えば、臭素などの化合物を１〜
3000ppm程度含むものである。
従来、この加圧オフガスの圧力エネルギーを回
収する方法としては、次のものが知られている。
まず、オフガス中の有機化合物が高温腐蝕を起
こさない程度の温度で且つ膨張後のオフガスが露
点より高い温度となる温度、例えば、オフガスを
約300℃程度まで外部の熱源で予熱し膨張機に導
入し動力回収し、その後、接触燃焼器により該有
機化合物を無機物とした後、吸収装置にて除去す
る方法がある。この方法はオフガスの温度が低
く、流量も少ないので、膨張機で回収される動力
は小さいものであつた。
また、オフガスをそのままガスタービンサイク
ルに導入し、圧縮空気の一部として使用する方法
が提案されている。この方法の場合、タービンブ
レードの腐蝕性成分が除去されていない為、膨張
機のノズル・ブレード、燃焼器等に高温腐蝕が発
生し、寿命、信頼性の点から、特殊な材料の選択
が必須となつたり、長時間の連続運転が不可能と
言う欠点があり、実用性の低いものであつた。
本発明者らは、以上の欠点について種々検討し
た結果、オフガス中のタービンブレードの腐蝕性
成分の除去を加圧下で行つた後、ガスタービンサ
イクルの作動媒体として使用する方法を見い出し
本発明を完成した。
以下、本発明を図面を用いて説明する
第１図は、本発明の最も好ましい実施態様の一
つであり、オフガスは、再生ガスタービンサイク
ル（圧縮機Ｃ、燃焼機CC、膨張機（＝タービン）
Ｔおよび再生器Ｒ１，Ｒ２をもつ）の熱回収媒体
（再生媒体）として利用され、さらに、洗浄塔CA
の洗浄用純水が該再生ガスタービンサイクルの低
温部の再生媒体として利用される例である。
第１図において、芳香族化合物の加圧液相酸化
プロセスからのオフガスが管１より予熱器Ｒで予
熱され、接触燃焼器TCに導入され、燃焼してタ
ービンブレードの腐蝕性元素含有の有機化合物を
無機物に変換し加熱された後、前記予熱器Ｒで熱
回収され、吸収塔Ａに管４を経て導入される。吸
収塔Ａにおいては、タービンブレードの腐蝕性成
分である無機物の吸収性に優れた添加成分を含む
水がポンプにより管２１を経て循環されておら
ず、ここで、実質的にタービングブレードの腐食
性成分である無機物は吸収除去される。吸収塔Ａ
からのオフガスは管５を経て洗浄塔CAに導入さ
れ、ここで、吸収塔Ａで除去不十分の成分および
吸収用添加剤などの不純物が、ポンプにより管２
２〜２３を経て循環される純水により除去され
る。このようにして実質的にタービングブレード
の腐蝕性成分を除かれたオフガスは管６を経てガ
スタービンサイクルの作動媒体空気の一部に混合
使用される。
第１図においては、さらに管６よりのオフガス
は、圧縮機Ｃ、燃焼器CC、膨張器（タービン）
Ｔおよび再生器Ｒ１，Ｒ２により構成される再生
ガスタービンサイクルの再生媒体として利用され
予熱されるともに、さらに、洗浄塔CAの洗浄純
水が該再生ガスタービンサイクルの低温部の再生
媒体として管２２より低温側の再生器Ｒ２に導入
され、管３５よりのタービン排気とここで熱交換
し予熱された後、管２３の経て洗浄塔CAに循環
されている。
以上、本発明の好ましい実施態様に基づいて本
発明を図面により説明したが、本発明は第１図の
方法に限定されるものではなく、実質的にタービ
ングブレードの腐蝕性成分である無機物を吸収除
去したりクリーンなオフガスを単純ガスタービン
サイクルの作動媒体空気の一部として単に使用す
る方法、再生ガスタービンサイクルの再生媒体と
して使用する方法、ガスタービンサイクルにて得
られる圧縮奇しきの一部を該液相酸化プロセスの
酸化用空気として用いる方法、前記圧縮空気の一
部若しくは全部にもクリーンなオフガスと同様の
熱回収操作を行い循環及び補給水による再生ガス
タービンサイクルの低温部の熱回収とそれによる
空気／水蒸気の混合物を再生媒体として使用する
方法なども当然ふくまれる。
以上の如くである本発明の方法は、芳香族化合
物の加圧液相酸化プロセスからのタービンブレー
ドの高温腐蝕性元素含有有機化合物を含むオフガ
スから、該有害成分を減圧することなく除去し、
且つ、熱損失も最低限に押さえて、タービンの高
温作動媒体の一部として利用するものであり、極
めて優れた省エネルギープロセスを提供するもの
であり、工業的実用性の極めて高いものである。
実施例 １
（クリーンなオフガスの製造）
デイクソンパツキンを充填した洗浄塔（50φ×
1000L）を使用して、管１〜５の流路を構成し、
クリーンなオフガスを得た。ここに、接触燃焼器
の操作温度は500℃とした。
このクリーンなオフガス（＝CPOG）は流量
40Nm3／ｈ、圧力14ata、温度45℃となる様、洗
浄塔の循環水（＝アルカリ性水溶液）温度は調節
された。又、CPOG中のBr2の含有量は1ppmV未
満であり、測定にかからなかつた。
検討例
（ガスタービンサイクル）
第１図のフローに従つて、芳香族化合物の加圧
液相酸化プロセスの触媒成分の一つとして臭素
（Br）を使用した例について検討した。
なお、検討のための前提条件は以下の如くであ
る。
(1) 圧縮機Ｃ 断熱効率 ηc＝0.70
膨張機Ｔ 〃 ηt＝0.87
燃焼効率 nb＝0.99
機械効率 ηm＝0.98
(2) 圧力損失（サイクル総合圧力損失） 9.5％
但し、再生器Ｒ２を使用しない検討例２では
7.2％
(3) オフガス 流量 34000Nm3／ｈ
（CPOG） 圧力 16ata
温度 47℃
(4) 燃料（CCの燃料）
成分 CO、H2、CH4、N2、CO2などの混合
ガス
発熱量 2640kcal／Ｎm3
温度 80℃
圧力 14ata
(5) 膨張機Ｔ入り口条件
圧力 12ata
温度 1000℃
(5) 大気条件 ISO
検討例 １
（ガスタービンサイクル＝GT１）
第１図のフロー（管No.５〜）について検討した
結果を下記に示した。
再生器 Ｒ１（熱回収量）4.0×106kcal／ｈ
〃 Ｒ２（熱回収量）4.0×106kcal／ｈ
圧縮機(C)動力 2450kw
膨張機(T)出力 11970kw
従つて、本発明のガスタービンサイクルは、
(1) 軸端出力 9320kw
(2) 軸端熱効率 64.3％（LHV）
(3) 排気温度 99℃
であり、極めて優れたものである。
検討例 ２
（ガスタービンサイクル＝GT２）
第１図のフローにおいて、洗浄塔CA、再生器
Ｒ２を使用しないで、吸収塔ＡからのCPOGをそ
のまま再生器Ｒ１に導入する他は検討例１と同様
としたところ
(1) 軸端出力 7900kw
(2) 軸端熱効率 65.2％（LHV）
(3) 排気温度 247℃
の結果が得られた。
以上の検討結果について、CPOGのエクセルギ
ーをJIS Ｚ 9204に従つて計算し、これを評価に
組み入れた検討例１、２の評価結果を下表に示し
た。これから、検討例１の方法が、検討例２より
優れたものであることがわかる。
【表】DETAILED DESCRIPTION OF THE INVENTION The present invention relates to the effective utilization of aromatic compound oxidation process off-gases, and in particular to the effective utilization of aromatic compound oxidation process off-gases, and in particular to the high temperature corrosive element-containing organic Pressurized off-gas containing compounds is combusted in a contact combustor to turn the organic compounds into inorganic substances, and then the corrosive components in the inorganic substances are absorbed in an absorption tower to create a clean turbine blade with virtually no corrosive components. off-gas,
A method for recovering power from oxidation process exhaust gas by introducing it into the pressurized working medium gas of a gas turbine cycle and using it as part of the air that is the working medium of the gas turbine cycle, and in a preferred embodiment, As a regenerative gas turbine cycle, the clean off-gas is used for preheating by exchanging heat with the turbine exhaust gas, and two or more absorption towers are provided, and the regeneration gas turbine cycle is performed using circulation and make-up water in the latter stage absorption tower. This is done to recover heat from the low temperature section. Pressurized off-gases from pressurized liquid phase oxidation processes, such as aromatic compounds - especially p-, m-xylene, are usually passed through an aqueous absorption device for the purpose of recovery of active components such as unreacted components in the off-gas. The temperature is relatively low, usually around 50℃, and the pressure is 10℃.
~20 ata. Most of the components in the off-gas are nitrogen that did not contribute to the oxidation reaction, and the rest is carbon dioxide, which is a product of the oxidation reaction, oxygen that has not been used in the oxidation reaction, and entrained saturated water vapor from the water absorption device described above. be. In addition, the off-gas contains a small amount of organic compounds containing elements that are catalyst components for oxidation reactions, and this by-product is a high-temperature corrosive component of turbine blades, depending on the catalyst component. , for example, a compound such as bromine from 1 to
It contains about 3000ppm. Conventionally, the following methods are known as methods for recovering the pressure energy of this pressurized off-gas. First, the off-gas is preheated with an external heat source to a temperature that does not cause high-temperature corrosion of the organic compounds in the off-gas and at which the expanded off-gas is higher than the dew point, for example, approximately 300°C, and then introduced into the expander. There is a method in which the power is recovered, and then the organic compound is turned into an inorganic substance by a catalytic combustor, and then removed by an absorption device. In this method, the temperature of the off-gas is low and the flow rate is low, so the power recovered by the expander is small. Furthermore, a method has been proposed in which off-gas is directly introduced into the gas turbine cycle and used as part of the compressed air. In this method, because the corrosive components of the turbine blades are not removed, high-temperature corrosion occurs in the expander nozzle blades, combustor, etc., and special materials must be selected from the viewpoint of longevity and reliability. It also had the disadvantage of not being able to operate continuously for long periods of time, making it impractical. As a result of various studies on the above-mentioned drawbacks, the present inventors discovered a method of removing corrosive components of turbine blades in off-gas under pressure, and then using the off-gas as a working medium in a gas turbine cycle, and completed the present invention. did. The present invention will be explained below with reference to the drawings. Figure 1 shows one of the most preferred embodiments of the present invention. )
T and regenerators R1 and R2) as a heat recovery medium (regeneration medium).
In this example, pure water for cleaning is used as a regeneration medium in the low temperature section of the regeneration gas turbine cycle. In Figure 1, off-gas from the pressurized liquid phase oxidation process of aromatic compounds is preheated in preheater R through tube 1, introduced into contact combustor TC, and combusted to remove corrosive element-containing organic compounds from turbine blades. After being converted into an inorganic substance and heated, the heat is recovered in the preheater R and introduced into the absorption tower A through the pipe 4. In the absorption tower A, water containing an additive component that has excellent absorption of inorganic substances, which are corrosive components of the turbine blades, is not circulated by the pump through the pipe 21, and here, substantially the corrosion of the turbine blades is prevented. Inorganic substances, which are natural components, are absorbed and removed. Absorption tower A
The off-gas from is introduced into the cleaning tower CA through pipe 5, where impurities such as components that have not been removed sufficiently in the absorption tower A and absorption additives are removed by a pump into pipe 2.
It is removed by pure water that is circulated through 2 to 23. The off-gas, which has thus been substantially freed from the corrosive components of the turbinating blades, is mixed with a portion of the working medium air of the gas turbine cycle via the pipe 6. In Fig. 1, the off-gas from the pipe 6 is further transmitted to the compressor C, the combustor CC, and the expander (turbine).
In addition, the purified water from the cleaning tower CA is used as a regeneration medium for the regeneration gas turbine cycle consisting of the regeneration gas turbine cycle T and regenerators R1 and R2 and is preheated. It is introduced into the regenerator R2 on the lower temperature side, where it is preheated by exchanging heat with the turbine exhaust gas from the pipe 35, and then circulated through the pipe 23 to the cleaning tower CA. The present invention has been described above with reference to the drawings based on a preferred embodiment of the present invention, but the present invention is not limited to the method shown in FIG. Simply using the absorbed or clean off-gas as part of the working air air in a simple gas turbine cycle, as a regeneration medium in a regenerative gas turbine cycle, or as part of the compressed air obtained in a gas turbine cycle. A method of using air as oxidizing air in the liquid phase oxidation process, a heat recovery operation similar to that of clean off-gas is performed on some or all of the compressed air, and heat recovery is performed in the low temperature section of the regeneration gas turbine cycle using circulation and make-up water. Naturally, this also includes a method of using the resulting air/steam mixture as a regeneration medium. The method of the present invention as described above removes harmful components from an off-gas containing high-temperature corrosive element-containing organic compounds of a turbine blade from a pressurized liquid phase oxidation process of aromatic compounds without reducing the pressure.
In addition, it minimizes heat loss and is used as a part of the high-temperature working medium of the turbine, providing an extremely excellent energy-saving process and having extremely high industrial practicality. Example 1 (Production of clean off-gas) Cleaning tower (50φ×
1000L) to configure the flow paths of tubes 1 to 5,
Obtained clean off-gas. Here, the operating temperature of the catalytic combustor was 500°C. This clean off-gas (=CPOG) has a flow rate of
The temperature of the circulating water (=alkaline aqueous solution) in the washing tower was adjusted so that the flow rate was 40Nm 3 /h, the pressure was 14ata, and the temperature was 45°C. Moreover, the content of Br 2 in CPOG was less than 1 ppmV and was not included in the measurement. Study Example (Gas Turbine Cycle) According to the flow shown in Figure 1, an example was studied in which bromine (Br) was used as one of the catalyst components in a pressurized liquid phase oxidation process of aromatic compounds. The preconditions for the study are as follows. (1) Compressor C Adiabatic efficiency ηc=0.70 Expander T 〃 ηt=0.87 Combustion efficiency nb=0.99 Mechanical efficiency ηm=0.98 (2) Pressure loss (total cycle pressure loss) 9.5% However, consider not using regenerator R2 In example 2
7.2% (3) Off gas Flow rate 34000Nm 3 /h (CPOG) Pressure 16ata Temperature 47℃ (4) Fuel (CC fuel) Component Mixed gas such as CO, H 2 , CH 4 , N 2 , CO 2 Calorific value 2640kcal / Nm 3 Temperature 80℃ Pressure 14ata (5) Expander T inlet conditions Pressure 12ata Temperature 1000℃ (5) Atmospheric conditions ISO Study example 1 (Gas turbine cycle = GT1) Study the flow in Figure 1 (Pipe No. 5~) The results are shown below. Regenerator R1 (heat recovery amount) 4.0×10 6 kcal/h 〃 R2 (heat recovery amount) 4.0×10 6 kcal/h Compressor (C) power 2450kw Expander (T) output 11970kw Therefore, the gas of the present invention The turbine cycle is extremely excellent, with (1) shaft end output of 9320kw, (2) shaft end thermal efficiency of 64.3% (LHV), and (3) exhaust temperature of 99℃. Study example 2 (Gas turbine cycle = GT2) Same as study example 1 except that in the flow shown in Figure 1, CPOG from absorption tower A is directly introduced into regenerator R1 without using cleaning tower CA and regenerator R2. As a result, the following results were obtained: (1) Shaft end output 7900kw (2) Shaft end thermal efficiency 65.2% (LHV) (3) Exhaust temperature 247℃. Regarding the above study results, the exergy of CPOG was calculated according to JIS Z 9204, and the evaluation results of Study Examples 1 and 2, which were incorporated into the evaluation, are shown in the table below. From this, it can be seen that the method of Study Example 1 is superior to Study Example 2. 【table】
第１図は、本発明の動力回収方法の好ましい一
例のフローであり、図中の番号及び記号はそれぞ
れ、
Ｒ：予熱器、TC：接触燃焼器、Ａ：吸収塔、
CA：洗浄塔、Ｒ２：低温側再生器、Ｒ１：高温
側再生器、Ｃ：圧縮機、Ｔ：膨張機、CC：燃焼
器、Ｌ：負荷、および１，２，３，４，５，６，
７，２１，２２，２３，３１，３２，３３，３
４，３５，３６，３７：管を示す。
FIG. 1 is a flowchart of a preferred example of the power recovery method of the present invention, and the numbers and symbols in the diagram are respectively R: preheater, TC: contact combustor, A: absorption tower,
CA: Cleaning tower, R2: Low temperature side regenerator, R1: High temperature side regenerator, C: Compressor, T: Expander, CC: Combustor, L: Load, and 1, 2, 3, 4, 5, 6 ，
7, 21, 22, 23, 31, 32, 33, 3
4, 35, 36, 37: Indicates a tube.
Claims (1)
タービンブレードの高温腐蝕性元素含有有機化合
物を含む加圧オフガスを接触燃焼器にて燃焼さ
せ、該有機化合物を無機物としたのち、吸収塔で
該無機物中の腐蝕性成分を吸収して、実質的にタ
ービンブレード腐蝕性成分のないクリーンなオフ
ガスとし、ガスタービンサイクルの加圧作動媒体
ガス中に導入し、該ガスタービンサイクルの作動
媒体である空気の一部として用いるごとくしてな
る酸化プロセス排ガスからの動力回収法。 ２ ガスタービンサイクルが再生サイクルであ
り、該クリーンなオフガスをタービン排気と熱交
換して予熱してなるものである特許請求の範囲第
１項記載の方法。 ３ 吸収塔を二塔以上設け、後段吸収塔の循環及
び補給水で再生ガスタービンサイクルの低温部の
熱回収を行う特許請求の範囲第１項又は２項記載
の方法。[Claims] 1. Pressurized off-gas containing high-temperature corrosive element-containing organic compounds of turbine blades from a pressurized liquid phase oxidation process of aromatic compounds is combusted in a catalytic combustor to convert the organic compounds into inorganic substances. Thereafter, the corrosive components in the inorganic substances are absorbed in an absorption tower to produce a clean off-gas substantially free of components corrosive to turbine blades, and the off-gas is introduced into the pressurized working medium gas of the gas turbine cycle. A method of recovering power from the oxidation process exhaust gas, which is used as part of the air that is the working medium of the oxidation process. 2. The method according to claim 1, wherein the gas turbine cycle is a regeneration cycle, and the clean off-gas is preheated by heat exchange with turbine exhaust gas. 3. The method according to claim 1 or 2, wherein two or more absorption towers are provided, and heat recovery from the low-temperature section of the regeneration gas turbine cycle is performed using circulation in the latter absorption tower and make-up water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7637384A JPS60219421A (en) | 1984-04-16 | 1984-04-16 | Method of recovering power from exhaust gas of oxidizing process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7637384A JPS60219421A (en) | 1984-04-16 | 1984-04-16 | Method of recovering power from exhaust gas of oxidizing process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60219421A JPS60219421A (en) | 1985-11-02 |
| JPH0468453B2 true JPH0468453B2 (en) | 1992-11-02 |
Family
ID=13603537
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7637384A Granted JPS60219421A (en) | 1984-04-16 | 1984-04-16 | Method of recovering power from exhaust gas of oxidizing process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60219421A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62203929A (en) * | 1986-03-04 | 1987-09-08 | Mitsubishi Gas Chem Co Inc | Power recovery method from off-gas in oxidation reactor |
| GB0808200D0 (en) * | 2008-05-06 | 2008-06-11 | Invista Technologies Srl | Power recovery |
-
1984
- 1984-04-16 JP JP7637384A patent/JPS60219421A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60219421A (en) | 1985-11-02 |
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