JPH08246816A - Generation method due to burning exhaust gas - Google Patents
Generation method due to burning exhaust gasInfo
- Publication number
- JPH08246816A JPH08246816A JP7051450A JP5145095A JPH08246816A JP H08246816 A JPH08246816 A JP H08246816A JP 7051450 A JP7051450 A JP 7051450A JP 5145095 A JP5145095 A JP 5145095A JP H08246816 A JPH08246816 A JP H08246816A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- steam
- generator
- condenser
- absorber
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
Landscapes
- Engine Equipment That Uses Special Cycles (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、都市ゴミ、都市下水の
汚泥、産業有機物を含む廃棄物、産業固形廃棄物などの
廃棄物を焼却してその排ガスにより発電する方法に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for incinerating waste such as municipal waste, sludge of municipal sewage, waste containing industrial organic substances, industrial solid waste, etc., and generating power from the exhaust gas.
【０００２】[0002]
【従来の技術】この種の、廃棄物はストーカー炉、流動
層、あるいは高速流動層、移動式焼却炉等によって焼却
されているが、水分を多く含む固形廃棄物はそのまま通
常の燃焼空気（熱交換により高温としたものあるいは常
温のもの）を用いて燃焼を行っている。このため、蒸発
した水分は利用されるこなく、排ガスとともに排気され
ている。2. Description of the Related Art This kind of waste is incinerated in a stalker furnace, a fluidized bed, a high-speed fluidized bed, a mobile incinerator, etc., but solid waste containing a large amount of water is used as it is in normal combustion air (heat Combustion is carried out using the ones that have been heated to a high temperature or those that are at room temperature. Therefore, the evaporated water is not used but is exhausted together with the exhaust gas.
【０００３】通常、廃棄物自体は４５〜７０％程度の大
量の水分を持っており、その排ガス中の水分のもってい
る熱量は、排ガス中の有害物質を除去洗浄するための最
終段階に設けられている湿式のスクラバーにおける洗浄
液に移行することにより棄てられた後、排ガスが大気中
に放散されるか、再加熱されて白煙の発生の防止が図ら
れながら大気中に棄てられている。Usually, the waste itself has a large amount of water of about 45 to 70%, and the heat quantity of the water in the exhaust gas is provided at the final stage for removing and cleaning harmful substances in the exhaust gas. After being discarded by being transferred to the cleaning liquid in the wet scrubber, the exhaust gas is either released into the atmosphere or is reheated and is discarded into the atmosphere while preventing the generation of white smoke.
【０００４】廃棄物に由来する水分のもっている熱量を
利用する方法として、本発明者らが先に提案した特開平
５−３０６８１３号公報に示されているように、燃焼空
気中の水分を増湿させることにより、排ガス中の水分を
高温で凝縮させ（８０〜８５℃で凝縮を始め、６０〜７
５℃で凝縮を終了させる）、排ガス中の水分の熱量を顕
熱として回収できる。As a method of utilizing the amount of heat of water derived from waste, as disclosed in Japanese Patent Laid-Open No. 306813/1993 proposed by the present inventors, the water content in combustion air is increased. By moistening, the moisture in the exhaust gas is condensed at a high temperature (condensation starts at 80 to 85 ° C,
Condensation is completed at 5 ° C.), and the calorific value of water in the exhaust gas can be recovered as sensible heat.
【０００５】従来のヒートポンプでは、駆動熱源と吸熱
熱源は別々の熱源を用いることが多い。一般的な発生
器、凝縮器、蒸発器、吸収器の４つの基本機器よりなる
吸収式冷凍機においては、吸収器および凝縮器より回収
される熱量の温度は、発生器と蒸発器の中間の温度であ
ることは知られている。In the conventional heat pump, the driving heat source and the endothermic heat source often use different heat sources. In an absorption chiller consisting of four basic devices, a general generator, a condenser, an evaporator, and an absorber, the temperature of the amount of heat recovered from the absorber and the condenser is between the generator and the evaporator. It is known to be temperature.
【０００６】したがって、吸収器および凝縮器Ｃの温度
を上げるためには、高温で発生器を運転させる必要があ
り、このためにリチューム−水とは異なった腐食性のな
い二作動流体が求められている。一方、蒸発器において
は、６０〜１００℃程度の吸熱熱源が要求されている。Therefore, in order to raise the temperature of the absorber and the condenser C, it is necessary to operate the generator at a high temperature, which requires a non-corrosive two working fluid different from lithium-water. ing. On the other hand, in the evaporator, an endothermic heat source of about 60 to 100 ° C. is required.
【０００７】[0007]
【発明が解決しようとする課題】一般に、廃棄物を燃焼
するにあたっては、その付属の廃熱ボイラーにおいて、
低温腐食を防止するために排ガス中の酸露点より高い温
度で運転し、かつ高温腐食を考慮してある温度以下で運
転しなければならない点の制限がある。Generally, in burning waste, in the attached waste heat boiler,
In order to prevent low temperature corrosion, there is a limitation in that it must be operated at a temperature higher than the acid dew point in the exhaust gas and must be operated at a temperature below a certain temperature in consideration of high temperature corrosion.
【０００８】このためにボイラーの蒸発圧力は高くしな
ければいけないし、一方、このような排ガスからは管壁
温度が非常に上昇するスーパーヒータの設置が無理とさ
れている。このために廃棄物ゴミ発電においては、効率
良く発電するためには、廃棄物の廃熱ボイラーより発生
した蒸気を別の熱源に加温する方法、すなわちガスター
ビンの排ガスによって加温する方法があり、また別の燃
料を用いて加温する方法がある。For this reason, the evaporation pressure of the boiler must be raised, and on the other hand, it is impossible to install a super heater which causes the temperature of the tube wall to rise extremely from such exhaust gas. For this reason, in the power generation of waste trash, there is a method of heating the steam generated from the waste heat boiler of the waste to another heat source, that is, a method of heating by the exhaust gas of the gas turbine, in order to generate power efficiently. There is also a method of heating with another fuel.
【０００９】しかし、前者の方法では、多額の設備費が
必要であり、また大型プラントでないと経済的でなく、
小型のゴミ処理発電プラントには適さない。後者の方法
においては、新しい燃料を外部より供給する必要がある
とともに、元来、大量の熱量を持っている廃棄物処理工
場に付設することは設計上好ましくない。However, the former method requires a large amount of equipment cost and is not economical unless it is a large plant.
Not suitable for small garbage disposal power plants. In the latter method, fresh fuel needs to be supplied from the outside, and it is originally not preferable to attach it to a waste treatment plant that has a large amount of heat.
【００１０】したがって、本発明の課題は、小型のゴミ
処理発電プラントとして適しており、かつ排ガス中の水
分がもっている熱量を効率よく発電により利用すること
により回収することにある。[0010] Therefore, an object of the present invention is to be suitable as a small-sized waste treatment power generation plant, and to recover the amount of heat of moisture in exhaust gas by efficiently utilizing the power generation.
【００１１】[0011]
【課題を解決するための手段】上記課題は、発生器、凝
縮器、蒸発器および吸収器により吸収式ヒートポンプを
構成し、水分を含む廃棄物を焼却炉に投入し、増湿され
た燃焼空気を用いて焼却し、その排ガスを、二作動体の
駆動熱源として前記発生器に導いて、蒸気を発生させて
これを凝縮器に導くとともに、前記発生器を通った排ガ
スを湿式処理により洗浄処理し、このガスを前記吸収器
へ送り吸熱熱源として利用し、前記吸収器での発生蒸気
と前記凝縮器での発生蒸気を蒸気タービンに導いて発電
を行うことで解決できる。Means for Solving the Problems The above problem is that an absorption heat pump is constituted by a generator, a condenser, an evaporator, and an absorber, and waste containing water is put into an incinerator to obtain humidified combustion air. Incinerating the exhaust gas, and guiding the exhaust gas to the generator as a heat source for driving the two-acting body to generate steam to guide it to the condenser, and the exhaust gas passing through the generator is washed by a wet process. Then, this gas is sent to the absorber to be used as an endothermic heat source, and the generated steam in the absorber and the generated steam in the condenser are guided to a steam turbine for power generation.
【００１２】前記蒸気タービンに蒸気を供給する前に、
その蒸気を外部熱源によりスーパーヒートした後、発電
を行うことが望ましい。この外部熱源として、焼却排ガ
スのもっている熱量を利用することができる。Before supplying steam to the steam turbine,
It is desirable to generate power after superheating the steam with an external heat source. As the external heat source, the amount of heat of the incineration exhaust gas can be used.
【００１３】前記焼却炉としては、注水して温度を制御
している炉であるときに本発明が好適に適用される。The present invention is preferably applied when the incinerator is a furnace in which water is poured to control the temperature.
【００１４】前記発生蒸気の一部を前記発電に、残部を
工業用蒸気および冷暖房用蒸気のいずれか一つに用いる
ことができる。A part of the generated steam can be used for the power generation, and the rest can be used for any one of industrial steam and cooling / heating steam.
【００１５】前記吸収器を通った排ガスを、前記増湿時
において燃焼空気の加温に用いるのが熱利用の点で好適
である。It is preferable in terms of heat utilization to use the exhaust gas that has passed through the absorber for heating the combustion air during the humidification.
【００１６】[0016]
【作用】図１に本発明のシステムフローシートを示す。
１は発生器、２は凝縮器、３は蒸発器、４は吸収器であ
り、これらを基本機器として吸収式ヒートポンプが構成
されている。FIG. 1 shows a system flow sheet of the present invention.
Reference numeral 1 is a generator, 2 is a condenser, 3 is an evaporator, and 4 is an absorber, and an absorption heat pump is configured with these as basic devices.
【００１７】他方で、廃棄物Ｍは焼却炉４０に供給さ
れ、これに対して増湿器５０を経て増湿された燃焼空気
が供給されて、燃料４１の下で、燃焼が行われる。この
焼却炉の形式は流動層であったり、ロストルを持った炉
であったり適宜の形式が用いられる。On the other hand, the waste M is supplied to the incinerator 40, to which the combustion air that has been humidified through the humidifier 50 is supplied, and combustion is performed under the fuel 41. The type of the incinerator may be a fluidized bed, a furnace with a rustle, or an appropriate type.
【００１８】焼却炉４０からの排ガスは、発生器１の加
熱器１ａに導かれて、発生器に蓄えられている濃厚塩類
を蒸発させる。蒸発したベーパーは、経路２１を経て凝
縮器２の再過熱部２ｂを通り、凝縮器２で発生している
蒸気と熱交換しながら、凝縮部２ａで凝縮する。同時
に、凝縮器２にある純水は蒸発されて、経路２２を経て
スーパーヒータ７を経て蒸気タービン８に導かれる。The exhaust gas from the incinerator 40 is guided to the heater 1a of the generator 1 to evaporate the concentrated salts stored in the generator. The vaporized vapor passes through the path 21 and passes through the reheating section 2b of the condenser 2 and exchanges heat with the vapor generated in the condenser 2 and is condensed in the condenser section 2a. At the same time, the pure water in the condenser 2 is evaporated and introduced into the steam turbine 8 via the route 22 and the super heater 7.
【００１９】凝縮器２で凝縮した水は、熱交換器６にお
いて、これに経路２３を経て流通されるタービン８のコ
ンデンセートと熱交換されて、蒸発器３に供給される。The water condensed in the condenser 2 is heat-exchanged in the heat exchanger 6 with the condensate of the turbine 8 which flows through the path 23, and is supplied to the evaporator 3.
【００２０】上述の発生器１の加熱器１ａを通った排ガ
スは、経路２４を経て湿式スクラバー１１に導かれ、こ
こで外部から水が供給されて増湿された後、経路２５を
経て蒸発器３の加熱器３ａに供給される。蒸発器３で
は、加熱器３ａによりコンデンセートを蒸発し、蒸発し
たベーパーを経路２６を経て、発生器１から経路２７を
経てくる濃厚塩と合流点２８で混合して吸収器４に導
く。The exhaust gas that has passed through the heater 1a of the generator 1 is guided to the wet scrubber 11 via the path 24, where water is supplied from the outside to increase the humidity, and then via the path 25 to the evaporator. 3 to the heater 3a. In the evaporator 3, the condensate is evaporated by the heater 3 a, and the evaporated vapor is mixed with the concentrated salt flowing from the generator 1 through the path 27 at the confluence point 28 and guided to the absorber 4.
【００２１】吸収器４では蒸発ベーパーを完全に凝縮さ
せ、凝縮液はポンプ１１により経路２９を経て熱交換器
５を通して、希薄液として発生器１に送る。熱交換器５
では希薄液と濃厚液との熱交換を図る。In the absorber 4, the evaporative vapor is completely condensed, and the condensed liquid is sent to the generator 1 as a dilute liquid through the heat exchanger 5 via the path 29 by the pump 11. Heat exchanger 5
Then, heat exchange between the dilute liquid and the concentrated liquid is attempted.
【００２２】吸収器４の凝縮器４ａ内においては、純粋
な水のベーパーと濃厚塩が合流点２８で混合されるため
に、沸点上昇を生じ、このために高温の加熱源となる。
そこで、蒸気タービン８のコンデンサー１０からのコン
デンセートを循環ポンプ１２により経路３０を通して吸
収器４に供給し、コンデンセートを蒸発し、経路３１を
通して、前記の凝縮器２から移行するベーパーと合流し
て、スーパーヒータ７に供給する。In the condenser 4a of the absorber 4, the pure water vapor and the concentrated salt are mixed at the confluence 28, so that the boiling point rises, and this serves as a high temperature heating source.
Therefore, the condensate from the condenser 10 of the steam turbine 8 is supplied to the absorber 4 through the path 30 by the circulation pump 12 to evaporate the condensate, and joins the vapor that is transferred from the condenser 2 through the path 31 to obtain the supercondensate. Supply to the heater 7.
【００２３】スーパーヒータ７では外部から燃料Ｆを供
給し、混合ベーパーをスーパーヒートしてこれを蒸気タ
ービン８に送り、エンタルピー落差を利用して発電機９
で発電を行う。操作条件によっては、スーパーヒータ７
を省略することができる。In the super heater 7, the fuel F is supplied from the outside, the mixed vapor is superheated and sent to the steam turbine 8, and the generator 9 is utilized by utilizing the enthalpy head.
To generate electricity. Depending on the operating conditions, the super heater 7
Can be omitted.
【００２４】蒸気タービン８の排気はコンデンサー１０
で凝縮し、このコンデンセートはそれぞれ前述の経路２
３，３０を通して凝縮器２および吸収器４の蒸発側に供
給させて、蒸発操作を行う。The exhaust of the steam turbine 8 is a condenser 10
Condensate is condensed by the
It is supplied to the evaporation side of the condenser 2 and the absorber 4 through 3, 30 to perform the evaporation operation.
【００２５】蒸発器３の加熱器３ａを出た排ガスは、経
路３２を経て給気送風機５１によって増湿器５０に送
り、送風機５２で送られる燃焼用空気の加温を行う。こ
こに増湿器５０では、冷却塔５３からのコンデンセート
を循環ポンプ５４により増湿器５０に供給し、このコン
デンセートを蒸発させて燃焼空気に水分を与える。増湿
器５０を通った排ガスは冷却塔５３に送られて、直接冷
却、あるいは間接冷却する。最終的な排ガスは冷却塔５
３の上部より大気中に拡散される。その前に、白煙防止
のための加熱器等を取り付けるのが好適である。The exhaust gas discharged from the heater 3a of the evaporator 3 is sent to the humidifier 50 by the supply air blower 51 via the path 32, and the combustion air sent by the blower 52 is heated. Here, in the humidifier 50, the condensate from the cooling tower 53 is supplied to the humidifier 50 by the circulation pump 54, and the condensate is evaporated to give water to the combustion air. The exhaust gas that has passed through the humidifier 50 is sent to the cooling tower 53 and is directly or indirectly cooled. Final exhaust gas is cooling tower 5
It is diffused into the atmosphere from the upper part of 3. Before that, it is preferable to attach a heater or the like for preventing white smoke.
【００２６】以上のように、本発明に従って、増湿器５
０を用いて増湿空気を燃焼用空気として用いることによ
り、蒸発器３の加熱温度が高くなり、大量の凝縮熱を少
ない温度差で（温度降下量で）蒸発器３内の作動流体に
伝熱できる。As described above, according to the present invention, the humidifier 5
By using the humidified air as combustion air by using 0, the heating temperature of the evaporator 3 becomes high, and a large amount of heat of condensation is transferred to the working fluid in the evaporator 3 with a small temperature difference (amount of temperature drop). I can heat up.
【００２７】[0027]
【実施例】前記の例において、操作条件などについて付
言する。本発明におけるヒートポンプの二作動体として
は、高温溶融無機塩と水の系が望ましいが、その他の組
合せも用いることができる。本発明に好適に用いられる
濃厚塩としては、リチュームブロマイド−水系を代表的
に用いることができるが、そのほか、硝酸カリおよび硝
酸ナトリウムの混合塩の水溶液、あるいはリチューム硝
酸と硝酸カリと硝酸ソーダの混合塩の水溶液なども用い
ることができる。EXAMPLES In the above example, the operating conditions and the like will be additionally mentioned. As the two-acting body of the heat pump in the present invention, a system of high temperature molten inorganic salt and water is desirable, but other combinations can be used. As the concentrated salt preferably used in the present invention, a lithium bromide-water system can be representatively used. An aqueous solution of salt or the like can also be used.
【００２８】焼却炉４０の排ガスにより蒸気ヒートポン
プの発生器１を駆動して用い、発生器１よりの排ガスを
湿式処理をし、高温になったガスを蒸発器１の加熱部に
導入する。これによって、通常では４５〜５０℃で露点
になる排ガスを８０℃付近で凝縮が始まるようにし、排
ガスの持っている多くの熱量を凝縮操作の下で、蒸発器
に熱量を与えることにより吸収器および凝縮器を加温さ
せることができる。The generator 1 of the steam heat pump is driven by the exhaust gas of the incinerator 40, the exhaust gas from the generator 1 is wet-processed, and the hot gas is introduced into the heating portion of the evaporator 1. As a result, the exhaust gas, which normally has a dew point of 45 to 50 ° C., starts to condense at around 80 ° C., and a large amount of heat of the exhaust gas is given to the evaporator under the condensing operation. And the condenser can be warmed.
【００２９】発生器１の加熱器の温度、すなわち排ガス
の入口温度は８００℃前後で出口温度は３００ないし４
５０℃とし、高温腐食および酸露点によるチューブの腐
食を避けるのが望ましい。湿式スクラバー１１での洗浄
処理においては、供給される排ガスの水分および増湿空
気の度合いによっても違うが、その出口ガス温度は、７
５〜８３℃前後であり、これが蒸発器３に供給されて凝
縮を始め、蒸発器３からの出口の温度は６５〜７５℃前
後である。この温度は比較的低温であるので、発生器１
へと同じ程度の熱量をここで供給することができる。し
たがって、この温度のベーパーが吸収器４に導かれてコ
ンデンスするために、同様の熱量が蒸気となってタービ
ンに供給される。The temperature of the heater of the generator 1, that is, the exhaust gas inlet temperature is around 800 ° C. and the outlet temperature is 300 to 4
It is desirable to set the temperature to 50 ° C. to avoid high temperature corrosion and tube corrosion due to acid dew point. In the cleaning process with the wet scrubber 11, the outlet gas temperature is 7 depending on the moisture content of the exhaust gas supplied and the degree of humidified air.
The temperature is around 5 to 83 ° C, which is supplied to the evaporator 3 to start condensation, and the temperature at the outlet from the evaporator 3 is around 65 to 75 ° C. Since this temperature is relatively low, the generator 1
The same amount of heat can be supplied here. Therefore, since the vapor of this temperature is guided to the absorber 4 to be condensed, the same amount of heat becomes steam and is supplied to the turbine.
【００３０】凝縮器２および吸収器４の蒸発部の圧力
は、１〜３kg／ｆcm2 程度が好ましい。また、発生器１
の濃厚塩の温度は２２０〜２６０℃前後が好ましい。ま
た、蒸発器３の圧力は０．５kg／ｆcm2 前後が最適であ
る。The pressure in the evaporators of the condenser 2 and the absorber 4 is preferably about 1 to 3 kg / fcm 2 . Also, the generator 1
The temperature of the concentrated salt is preferably 220 to 260 ° C. The pressure of the evaporator 3 is optimally around 0.5 kg / fcm 2 .
【００３１】以上のようにして低圧蒸気ではあるが、適
切な過熱度ベーパーを得ることによって低圧の蒸気ター
ビン８を十分駆動することができる。As described above, the low-pressure steam turbine 8 can be sufficiently driven by obtaining an appropriate superheat degree vapor.
【００３２】[0032]
【実施例】本発明の効果を図１に従う実施例により説明
する。９，９００Ｎm3／hrの湿度４５％、温度２５℃の
空気を誘引ファンで直径１．２m 、伝熱面積３５０m2の
増湿器の下部より供給し、冷却塔より発生するドレンを
供給し、温度７０℃の飽和空気を得て、これを焼却炉に
供給した。EXAMPLES The effects of the present invention will be described with reference to an example according to FIG. Air of 9,900 Nm 3 / hr with a humidity of 45% and a temperature of 25 ° C. was supplied by an induction fan from the bottom of the humidifier with a diameter of 1.2 m and a heat transfer area of 350 m 2 , and the drain generated from the cooling tower was supplied. Saturated air with a temperature of 70 ° C. was obtained and fed to the incinerator.
【００３３】発熱量２，０００kcal／kgの廃棄物は流動
焼却炉に２．７Ton ／hrの割合で供給されて焼却が行わ
れ、燃焼排ガス温度として８４０〜８５０℃で運転され
た。Waste having a calorific value of 2,000 kcal / kg was supplied to a fluidized incinerator at a rate of 2.7 Ton / hr for incineration, and the combustion exhaust gas temperature was operated at 840 to 850 ° C.
【００３４】燃焼排ガス量は１３，３００kg／hrであ
り、これが本発明の発生器を構成する、伝熱面積１５０
m2の煙管型ボイラーに供給された。ここでは、入口温度
８４０〜８５０℃、出口温度４４０〜４５０℃で運転を
した。ボイラー内部にはトータル塩濃度９０％、そのう
ち硝酸ナトリウム１９％、硝酸カリウム２８％、硝酸リ
チューム５３％の濃厚塩を２．３kg／ｆcm2 Abで２２７
℃で蒸発を行い、発生したベーパーは伝熱面積２５０m2
の凝縮器に供給し、缶外にはボイラー水が沸騰し、操作
圧力２．３kg／ｆcm2 Ab、蒸発量は３．８Ton ／hrであ
る。The amount of combustion exhaust gas is 13,300 kg / hr, which constitutes the generator of the present invention.
Supplied to a smoke tube boiler of m 2 . Here, the operation was performed at an inlet temperature of 840 to 850 ° C and an outlet temperature of 440 to 450 ° C. 90% total salt concentration, of which 19% sodium nitrate, 28% potassium nitrate, 53% nitrate nitrate, concentrated salt of 227 at 2.3 kg / fcm 2 Ab
Evaporate at ℃, the generated vapor has a heat transfer area of 250m 2
Boiler water boils outside the can, the operating pressure is 2.3 kg / fcm 2 Ab, and the evaporation amount is 3.8 Ton / hr.
【００３５】次いでこの排ガスは、直径２．４m ×高さ
１０m 湿式スクラバーを通して洗浄処理された後、加熱
器の伝熱面積１５０m2の横型多管式の蒸発器に供給され
た。Next, this exhaust gas was washed through a wet scrubber having a diameter of 2.4 m and a height of 10 m, and then fed to a horizontal multi-tube evaporator having a heat transfer area of 150 m 2 of the heater.
【００３６】蒸発器の運転は入口温度８１〜８２℃、出
口温度７２℃とされた。一方、蒸発器の蒸発側は０．５
kg／ｆcm2 Abの圧力下で、凝縮器のコンデンセートを蒸
発した。蒸発器からのベーパーは、発生器の濃厚塩と混
合されて、温度１３５℃となって吸収器の加熱器の内部
で凝縮された。The evaporator was operated at an inlet temperature of 81 to 82 ° C and an outlet temperature of 72 ° C. On the other hand, the evaporation side of the evaporator is 0.5
The condensate of the condenser was evaporated under a pressure of kg / fcm 2 Ab. The vapor from the evaporator was mixed with the concentrated salt of the generator to a temperature of 135 ° C and condensed inside the heater of the absorber.
【００３７】この吸収器の外部は、蒸発側となってお
り、蒸気タービン排気のコンデンセートが供給され、こ
れを３．９Ton ／hrの割合で蒸発させて、スーパーヒー
タ７に送られた。一方、ここで得られた凝縮液すなわち
希薄溶液は、ポンプにより熱交換器を経て発生器に返さ
れ、前記の操作が繰り返えされた。The outside of this absorber is on the evaporation side, and the condensate of the steam turbine exhaust was supplied, and this was evaporated at a rate of 3.9 Ton / hr and sent to the super heater 7. On the other hand, the condensate obtained here, that is, the dilute solution, was returned to the generator via the heat exchanger by the pump, and the above operation was repeated.
【００３８】この吸収器での発生蒸気と前記凝縮器から
の発生した蒸気を合流させて、灯油を燃料とする４５m2
のスーパーヒータにより温度を３００℃とし、３段の蒸
気タービンに供給し、それに付属している発電機によっ
て発電を行った。その際、排気蒸気は２５０m2のコンデ
ンサーによって０．０７kg／ｆcm2 の真空下で運転し
た。発電機では１，０８０kwの発電量を得ることができ
た。The steam generated in this absorber and the steam generated in the condenser are merged, and 45 m 2 using kerosene as fuel
The temperature was raised to 300 ° C. by the super heater of No. 3 and supplied to a three-stage steam turbine, and power was generated by the generator attached to it. At that time, the exhaust steam was operated under a vacuum of 0.07 kg / fcm 2 with a condenser of 250 m 2 . With the generator, we were able to obtain a power output of 1,080 kw.
【００３９】[0039]
【発明の効果】本発明によれば、発電熱効率として約１
４．３％であり、通常の小型ゴミ処理発電プラントでの
発電量と比較してきわめて高い。水分および有害物質を
多く含む廃棄物を増湿燃焼をし、そのガスを再生器に供
給し、出口の高温ガスを湿式処理し、それをさらに蒸発
器に入れることにより従来よりも約２倍の蒸気発生量を
得て、これをスーパーヒートすることにより低圧蒸気で
はあるが、有効な発電を行わせることができる。この発
電量は通常のボイラーの２倍であり、したがって、発電
量も約２倍となる。According to the present invention, the thermal efficiency of power generation is about 1
This is 4.3%, which is extremely high compared to the amount of power generated by a normal small-sized waste treatment power plant. The waste containing a lot of water and harmful substances is humidified and burned, the gas is supplied to the regenerator, the hot gas at the outlet is wet-processed, and it is further put in the evaporator, so that it is about twice as much as before. By obtaining the steam generation amount and superheating this, it is possible to generate effective power though it is low pressure steam. The amount of power generation is twice that of a normal boiler, and therefore the amount of power generation is also about double.
【００４０】なお、本発明は小型の２００Ton ／day 程
度までの大きさの焼却炉に付設することにより優れた利
点がもたらされる。The present invention provides excellent advantages by being attached to a small incinerator having a size of up to about 200 Ton / day.
【図１】本発明の構成例を示すフローシートである。FIG. 1 is a flow sheet showing a configuration example of the present invention.
１…発生器、１ａ…加熱器、２…凝縮器、２ｂ…再過熱
器、３…蒸発器、３ａ…加熱器、４…吸収器、５，６…
熱交換器、７…スーパーヒータ、８…蒸気タービン、９
…発電機、１０…コンデンサー、１１…湿式スクラバ
ー、４０…焼却炉、５０…増湿器。1 ... Generator, 1a ... Heater, 2 ... Condenser, 2b ... Reheater, 3 ... Evaporator, 3a ... Heater, 4 ... Absorber, 5, 6 ...
Heat exchanger, 7 ... Super heater, 8 ... Steam turbine, 9
... generator, 10 ... condenser, 11 ... wet scrubber, 40 ... incinerator, 50 ... humidifier.
Claims (6)
り吸収式ヒートポンプを構成し、 水分を含む廃棄物を焼却炉に投入し、増湿された燃焼空
気を用いて焼却し、 その排ガスを、二作動体の駆動熱源として前記発生器に
導いて、蒸気を発生させてこれを凝縮器に導くととも
に、前記発生器を通った排ガスを湿式処理により洗浄処
理し、このガスを前記吸収器へ送り吸熱熱源として利用
し、 前記吸収器での発生蒸気と前記凝縮器での発生蒸気を蒸
気タービンに導いて発電を行うことを特徴とする焼却排
ガスによる発電方法。1. An absorption heat pump comprising a generator, a condenser, an evaporator and an absorber. Waste containing water is put into an incinerator and incinerated using humidified combustion air. Is introduced into the generator as a driving heat source for the two-actuator to generate steam and guide it to the condenser, and the exhaust gas passing through the generator is washed by a wet process, and the gas is absorbed into the absorber. Is used as an endothermic heat source, and is used as an endothermic heat source to guide the steam generated in the absorber and the steam generated in the condenser to a steam turbine to generate electric power.
その蒸気を外部熱源によりスーパーヒートした後、発電
を行う請求項１記載の焼却排ガスによる発電方法。2. Before supplying steam to the steam turbine,
The power generation method using incineration exhaust gas according to claim 1, wherein the steam is superheated by an external heat source and then power is generated.
求項１記載の焼却排ガスによる発電方法。3. The power generation method using incineration exhaust gas according to claim 1, wherein incineration exhaust gas is used as the external heat source.
る炉である請求項１記載の焼却排ガスによる発電方法。4. The power generation method using incinerator exhaust gas according to claim 1, wherein the incinerator is a furnace in which water is injected to control the temperature.
工業用蒸気および冷暖房用蒸気のいずれか一つに用いる
請求項１記載の焼却排ガスによる発電方法。5. The power generation method using incineration exhaust gas according to claim 1, wherein a part of the generated steam is used for the power generation and the rest is used for any one of industrial steam and cooling / heating steam.
において燃焼空気の加温に用いる請求項１記載の焼却排
ガスによる発電方法。6. The power generation method using incineration exhaust gas according to claim 1, wherein the exhaust gas that has passed through the absorber is used for heating combustion air during the humidification.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7051450A JPH08246816A (en) | 1995-03-10 | 1995-03-10 | Generation method due to burning exhaust gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7051450A JPH08246816A (en) | 1995-03-10 | 1995-03-10 | Generation method due to burning exhaust gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH08246816A true JPH08246816A (en) | 1996-09-24 |
Family
ID=12887277
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7051450A Pending JPH08246816A (en) | 1995-03-10 | 1995-03-10 | Generation method due to burning exhaust gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH08246816A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105257353A (en) * | 2015-10-13 | 2016-01-20 | 雷衍章 | Absorption type circulation system and method |
| CN106352590A (en) * | 2016-06-15 | 2017-01-25 | 李华玉 | Combined heating and power system |
| CN106440469A (en) * | 2016-05-30 | 2017-02-22 | 李华玉 | Combined heating and power system |
| CN106440467A (en) * | 2016-05-30 | 2017-02-22 | 李华玉 | Heat and power combined supply system |
| CN106440468A (en) * | 2016-06-15 | 2017-02-22 | 李华玉 | Combined heating and power system |
| CN106524560A (en) * | 2016-06-15 | 2017-03-22 | 李华玉 | Heat-power combined supply system |
-
1995
- 1995-03-10 JP JP7051450A patent/JPH08246816A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105257353A (en) * | 2015-10-13 | 2016-01-20 | 雷衍章 | Absorption type circulation system and method |
| CN106440469A (en) * | 2016-05-30 | 2017-02-22 | 李华玉 | Combined heating and power system |
| CN106440467A (en) * | 2016-05-30 | 2017-02-22 | 李华玉 | Heat and power combined supply system |
| CN106440469B (en) * | 2016-05-30 | 2020-01-31 | 李华玉 | Combined heat and power system |
| CN106440467B (en) * | 2016-05-30 | 2020-05-01 | 李华玉 | Combined heat and power system |
| CN106352590A (en) * | 2016-06-15 | 2017-01-25 | 李华玉 | Combined heating and power system |
| CN106440468A (en) * | 2016-06-15 | 2017-02-22 | 李华玉 | Combined heating and power system |
| CN106524560A (en) * | 2016-06-15 | 2017-03-22 | 李华玉 | Heat-power combined supply system |
| CN106440468B (en) * | 2016-06-15 | 2020-03-17 | 李华玉 | Combined heat and power system |
| CN106524560B (en) * | 2016-06-15 | 2020-05-01 | 李华玉 | Combined heat and power system |
| CN106352590B (en) * | 2016-06-15 | 2020-06-16 | 李华玉 | Combined heat and power system |
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