JPH063285B2 - Boiler equipment - Google Patents
Boiler equipmentInfo
- Publication number
- JPH063285B2 JPH063285B2 JP59178070A JP17807084A JPH063285B2 JP H063285 B2 JPH063285 B2 JP H063285B2 JP 59178070 A JP59178070 A JP 59178070A JP 17807084 A JP17807084 A JP 17807084A JP H063285 B2 JPH063285 B2 JP H063285B2
- Authority
- JP
- Japan
- Prior art keywords
- air preheater
- air
- boiler
- temperature
- high temperature
- 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 - Fee Related
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000000446 fuel Substances 0.000 claims description 8
- 238000002485 combustion reaction Methods 0.000 claims description 6
- 239000000567 combustion gas Substances 0.000 description 21
- 239000007789 gas Substances 0.000 description 13
- 238000011084 recovery Methods 0.000 description 9
- 239000002737 fuel gas Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Landscapes
- Air Supply (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明はボイラ装置、更に詳細には排熱回収ボイラ装置
の改良に関する。Description: TECHNICAL FIELD The present invention relates to a boiler device, and more particularly, to improvement of an exhaust heat recovery boiler device.
工場プロセスの過程で発生する副生ガスの種類に、低カ
ロリガスのものが可成りあり、従来もこれらをボイラの
燃料として有効に利用して来た。その１例として第３図
を参照すると、01はボイラ、０２は空気予熱器、０３は
誘引通風機、０４は煙突であり、これらは煙道０５によ
り連通され、燃焼ガスはボイラ０１から誘引通風機０３
により煙突から排出される。一方燃焼用空気は押込通風
機０６により空気予熱器０２に送られ、その出口空気は
バーナ風箱０７に至り、ボイラ０１の炉内に供給され
る。そして押込通風機０６からバーナ風箱０７に至るま
では風道０８により連通されている。また燃料ガスは燃
料ガス管０９によりＵ字水封器010を経てバーナ風箱０
７内のバーナ011に連通されている。ボイラ給水は、給
水ポンプ012により給水配管013を通じて気水ドラム014
に給水されている。The type of by-product gas generated in the process of the factory process can be low calorie gas, and these have been used effectively as fuel for boilers in the past. As an example, referring to FIG. 3, 01 is a boiler, 02 is an air preheater, 03 is an induced draft fan, 04 is a chimney, and these are communicated by a flue 05, and the combustion gas is drawn from the boiler 01 to the draft draft. Machine 03
Is discharged from the chimney by. On the other hand, the combustion air is sent to the air preheater 02 by the forced draft fan 06, and its outlet air reaches the burner wind box 07 and is supplied into the furnace of the boiler 01. An air passage 08 connects the forced draft fan 06 to the burner wind box 07. Further, the fuel gas is passed through the U-shaped water sealer 010 through the fuel gas pipe 09 and the burner wind box 0
It communicates with burner 011 in 7. Boiler water is supplied by the water supply pump 012 through the water supply pipe 013 to the steam drum 014.
Is supplied with water.
上記の低カロリーガスの代表的な例は製鉄所の高炉ガス
であり、表−１に示すように、燃料ガス中の一酸化炭素
ＣＯを２０〜２５％含有するので、空気による燃料用酸
素の供給が少なくてよい反面、不活性ガスである窒素N2
および炭酸ガスCO2を合わせて７０〜７５％含有するの
で、表−２に示すように、天然ガス、重油に比べて燃料
発熱量が低く、燃焼生成ガス量が非常に多い。このこと
は、ボイラからの排熱回収を計る空気予熱器の設計に関
し重要な条件である。A typical example of the above low-calorie gas is blast furnace gas of an iron mill, and as shown in Table 1, it contains 20 to 25% of carbon monoxide CO in the fuel gas. Nitrogen N 2 which is an inert gas, while the supply may be small
Further, since 70 to 75% of carbon dioxide CO 2 is contained in total, as shown in Table 2, the calorific value of fuel is lower than that of natural gas and heavy oil, and the amount of combustion product gas is very large. This is an important condition for designing an air preheater that measures exhaust heat recovery from a boiler.
ところで，ボイラ・ユニットの高効率化による省エネル
ギ指向に対し、重油、天然ガスあるいは石炭などのよう
な燃料を用いる場合は、空気予熱器の伝熱面積が増加す
れば、それ相当の熱回収が可能で、ボイラ効率も上昇す
るが、高炉ガスのように燃焼ガス量が多大で、加熱側保
有熱量が大きく、被加熱側の空気量が少ない場合は、空
気の温度が上昇し易く、出口空気温度が燃焼ガス温度に
接近して温度差が飽和するので、熱交換量に限界が生
じ、空気予熱器の伝熱面をいくら増加させても、ボイラ
効率の上昇が期待できない状態が生じる。下記はその１
例である。即ち第４図において， ＧＣ＝空気予熱器を通過する燃焼ガス量 ＝305,000kg／Ｈ ＡＣ＝空気予熱器を通過する空気量 ＝126,000kg／Ｈ tg1＝空気予熱器入口燃焼ガス温度 ＝３８８℃ tg2＝空気予熱器出口燃焼ガス温度 ＝２５６℃ Cpg＝燃焼ガスの比熱 ＝0.26Kcalkg・℃ ta1＝空気予熱器入口空気温度＝１０℃ ta2＝空気予熱器出口空気温度＝350℃ Cpa＝空気の比熱 ＝0.245Kcal／kg・℃ Δt1＝空気予熱器高温側におけるガスと空気 の温度差 ＝３８℃ Δt2＝空気予熱器低温側におけるガスと空気 の温度差 ＝246℃ という条件を与えると、空気予熱器の必要伝熱面積（Ｈ
・Ｓ）は 但し，Ｑ＝空気予熱器の熱交換量 ＝ＧＣ×（tgi−tgo）Cpg ＝ＡＣ×（tao−tai）Cpa ＝10,500,000Kcal／Ｈ Ｋ＝熱伝達係数＝２５Kcal／m2h℃ そこで、空気予熱器の伝熱面積を増加して燃焼ガスの排
熱回収量を増加させ、ボイラの熱効率を２％向上させよ
うとする場合の例を下記に示す。ここでボイラの熱効率
を２％向上させるためには、上述のtg2を256℃から226
℃とする必要があるから tg1＝338℃ tg2＝226℃ Ｑ＝ＧＣ（tg1−tg2）Cpg ＝305,000×（388−226）×0.26 ＝12,850,000Kcal 上記の計算から、空気予熱器の高温側において、加熱側
の燃焼ガス温度よりも被加熱側の空気温度が高くならな
いと熱収支的にバランスしないことを示し、実際上この
よな熱交換はありえない。 By the way, in the case of using fuel such as heavy oil, natural gas, or coal, in order to save energy by improving the efficiency of the boiler unit, if the heat transfer area of the air preheater is increased, a corresponding heat recovery can be achieved. Although the boiler efficiency is also increased, if the combustion gas amount is large like blast furnace gas, the heating side has a large amount of heat, and the heated side has a small amount of air, the temperature of the air tends to rise and the outlet air Since the temperature approaches the combustion gas temperature and the temperature difference is saturated, the amount of heat exchange is limited, and no matter how much the heat transfer surface of the air preheater is increased, the boiler efficiency cannot be expected to increase. Below is part 1
Here is an example. That is, in FIG. 4, GC = combustion gas amount passing through the air preheater = 305,000 kg / H AC = air amount passing through the air preheater = 126,000 kg / H t g1 = air preheater inlet combustion gas temperature = 388 ° C. t g2 = air preheater outlet combustion gas temperature = 256 ° C C pg = combustion gas specific heat = 0.26Kcalkg · ° C t a1 = air preheater inlet air temperature = 10 ° C t a2 = air preheater outlet air temperature = 350 ° C pa = specific heat of air = 0.245Kcal / kg · ° C Δt 1 = temperature difference between gas and air on the high temperature side of the air preheater = 38 ° C Δt 2 = temperature difference between gas and air on the low temperature side of the air preheater = 246 ° C , The required heat transfer area of the air preheater (H
・ S) However, Q = amount of heat exchange air preheater = GC × (t gi -t go ) C pg = AC × (t ao -t ai) C pa = 10,500,000Kcal / H K = heat transfer coefficient = 25 Kcal / m 2 h ℃ Therefore, an example in which the heat transfer area of the air preheater is increased to increase the exhaust heat recovery amount of the combustion gas and the thermal efficiency of the boiler is improved by 2% is shown below. Here, in order to improve the thermal efficiency of the boiler by 2%, the above-mentioned t g2 is changed from 256 ° C to 226
T g1 = 338 ° C. t g2 = 226 ° C. Q = GC (t g1 −t g2 ) C pg = 305,000 × (388−226) × 0.26 = 1,850,000 Kcal From the above calculation, it is shown that on the high temperature side of the air preheater, the heat balance will not be balanced unless the air temperature on the heated side becomes higher than the combustion gas temperature on the heating side, and such heat exchange is practically impossible. .
それゆえ、空気予熱器の熱交換はΔt1＞０，Δt2＞０で
なければならず、上記計算の場合，理論上の空気温度の
最高値tao(MaX)は388℃で、必要伝熱面積ＨＳ＝∞とな
る。この場合でもtgo＝241℃でボイラ効率は約１．０％
が限度である。Therefore, the heat exchange of the air preheater must be Δt 1 > 0 and Δt 2 > 0. In the above calculation, the theoretical maximum air temperature t ao (MaX) is 388 ° C, The thermal area HS = ∞. Even in this case, the boiler efficiency is about 1.0% at t go = 241 ° C.
Is the limit.
即ち、加熱側の燃焼ガス量が多大で、被加熱側の空気量
が比較的少量の条件の場合は、ボイラ効率の向上には限
界があり、且つこの限界内であっても僅かな効率向上の
ためにも空気予熱器が超大形となり、不経済な設備とな
る。That is, when the amount of combustion gas on the heating side is large and the amount of air on the heated side is relatively small, there is a limit to the improvement of boiler efficiency, and even within this limit, a slight improvement in efficiency is achieved. Because of this, the air preheater becomes super-large and uneconomical.
本発明は上記の高炉ガスなどの低カロリガス焚ボイラの
熱効率改善を目的とするものである。The present invention is intended to improve the thermal efficiency of a low calorie gas fired boiler such as the above blast furnace gas.
すなわち、本発明は、低カロリーガスを燃料とするボイ
ラーに於いて、空気予熱器を高温部と低温部に分割し、
低温部空気予熱器出口の熱空気により、ボイラ給水を加
熱することにより、空気温度を低下させ、高温部空気予
熱器における燃焼ガス温度と空気温度との温度差を大き
くすることにより、空気予熱器の熱交換率を向上させて
燃焼ガスの排熱を多く回収し、ボイラ効率の向上を計っ
たことを特徴とするボイラ装置にある。That is, the present invention, in a boiler that uses low-calorie gas as a fuel, divides the air preheater into a high temperature part and a low temperature part,
By heating the boiler feed water with hot air at the low temperature part air preheater outlet, the air temperature is lowered, and by increasing the temperature difference between the combustion gas temperature and the air temperature in the high temperature part air preheater, the air preheater is increased. The boiler device is characterized in that the heat exchange rate is improved, a large amount of exhaust heat of combustion gas is recovered, and the boiler efficiency is improved.
以下、本発明を添付図面第１図および第２図に例示した
その好適な実施例について詳述する。The present invention will now be described in detail with reference to its preferred embodiments illustrated in FIGS. 1 and 2 of the accompanying drawings.
第１図において、１はボイラ、２は高温空気予熱器、３
は低温空気予熱器、４は誘引通風機、５は煙突であり、
これらは煙道６により連通され、燃焼ガスはボイラ１か
ら誘引通風機４により煙突５に排出される。一方、燃焼
用空気は押込通風機７により低温空気予熱機３に送ら
れ、その出口空気は空気式ボイラ給水加熱器８を経て高
温空気予熱器２を通り、バーナ風箱９に至り、ボイラ１
の炉内に供給される。そして、押込通風機７からバーナ
風箱９に至るまでは風道１０により連通されている。ま
た、燃料ガスは燃料供給管１１によりＵ字形水封器１２
を経てバーナ１３に至る。In FIG. 1, 1 is a boiler, 2 is a high temperature air preheater, 3
Is a low temperature air preheater, 4 is a draft fan, 5 is a chimney,
These are communicated by a flue 6, and the combustion gas is discharged from the boiler 1 to a chimney 5 by an induced draft fan 4. On the other hand, the combustion air is sent to the low temperature air preheater 3 by the forced draft fan 7, and the outlet air thereof passes through the air boiler feedwater heater 8 and the high temperature air preheater 2 to reach the burner wind box 9 to reach the boiler 1
Is fed into the furnace. An air passage 10 connects the forced draft fan 7 to the burner air box 9. Further, the fuel gas is supplied to the U-shaped water sealer 12 through the fuel supply pipe 11.
To the burner 13.
ボイラ給水は、給水ポンプ１４により給水配管１５を通
じ、空気式ボイラ給水加熱器８を経て気水ドラム１６に
給水される。Boiler feed water is fed to a steam / water drum 16 by a feed pump 14 through a feed pipe 15 and an air type boiler feed heater 8.
上記第１図に図示のボイラ全体の作用を略述すれば下記
のとおりである。The operation of the entire boiler shown in FIG. 1 is as follows.
(1)燃焼用空気は押込通風機７により、低温空気予熱器
３に送られ、ボイラ１からの燃焼ガスの排熱を回収しな
がら燃焼空気の予熱を行なう。(1) Combustion air is sent to the low temperature air preheater 3 by the forced draft fan 7, and the combustion air is preheated while recovering the exhaust heat of the combustion gas from the boiler 1.
(2)低温空気予熱器３で予熱された空気は、空気式ボイ
ラ給水加熱器８において、ボイラ給水を加熱する。(2) The air preheated by the low temperature air preheater 3 heats the boiler feed water in the pneumatic boiler feed water heater 8.
(3)空気式ボイラ給水加熱器８を出た空気は再び高温空
気予熱器２でボイラ排熱を回収し高温空気となってバー
ナ風箱９に至る。(3) The air discharged from the air type boiler feed water heater 8 recovers the exhaust heat of the boiler again by the high temperature air preheater 2 and becomes high temperature air and reaches the burner wind box 9.
上記の従来の空気予熱器によるボイラ排熱の熱回収は前
述の第４図において説明したように、ボイラ排熱の回収
量には限界があり、ボイラ熱効率の大幅な向上が期待で
きない。As described above with reference to FIG. 4, the heat recovery of the boiler exhaust heat by the conventional air preheater has a limit in the amount of recovery of the boiler exhaust heat, and a significant improvement in boiler thermal efficiency cannot be expected.
本発明のボイラ装置は、上記構成、作用のものであり、
空気予熱器を高温部空気予熱器と低温部空気予熱器とに
分割し、低温空気予熱器３と高温空気予熱器２の間に空
気式ボイラ給水加熱器８を設けて、空気の熱量をボイラ
給水に転化し、高温空気通熱器２の入口空気温度を下げ
ているので、高温空気予熱器２におけるボイラ排ガスの
熱回収効率が向上しボイラ効率が上昇する。The boiler device of the present invention has the above-mentioned configuration and operation,
The air preheater is divided into a high temperature part air preheater and a low temperature part air preheater, and an air type boiler feedwater heater 8 is provided between the low temperature air preheater 3 and the high temperature air preheater 2 to change the heat quantity of the air to the boiler. Since the temperature of the inlet air of the high-temperature air heat exchanger 2 is lowered by converting to feed water, the heat recovery efficiency of the boiler exhaust gas in the high-temperature air preheater 2 is improved and the boiler efficiency is increased.
以下、前述の第４図における従来の場合と比較し、本発
明の場合のボイラ効率の向上度合を具体的に説明する。Hereinafter, the degree of improvement in boiler efficiency in the case of the present invention will be specifically described in comparison with the conventional case shown in FIG.
第２図において、ボイラ効率を２％向上させる場合 ＧＣ＝高温空気予熱器２と低温空気予熱器３ を通過する燃焼ガス量 ＝305,000×（１−0.02）＝298,900kg／Ｈ ＡＣ＝高温空気予熱器２と低温空気予熱器３ を通過する空気量 ＝126,000×（１-0.02）＝123,480kg／Ｈ ＦＷ＝ボイラ給水量 ＝130,000kg／Ｈ とする。In Fig. 2, in the case of improving the boiler efficiency by 2% GC = amount of combustion gas passing through the high temperature air preheater 2 and the low temperature air preheater 3 = 305,000 x (1-0.02) = 298,900kg / H AC = high temperature air preheat The amount of air passing through the unit 2 and the low-temperature air preheater 3 = 126,000 x (1-0.02) = 123,480 kg / H FW = boiler feed water amount = 130,000 kg / H.
(1)高温空気予熱器の設計 tg1＝高温空気予熱器入口燃焼ガス温度 ＝388℃ tg2＝高温空気予熱器出口燃焼ガス温度 ＝330℃ では、 Ｑ１＝高温空気予熱器の熱交換量 ＝ＧＣ×（tg1−tg2）×Cpg ＝298,900×（388−330）×0.26 ＝4,507,000Kcal／Ｈ となる。(1) Design of high temperature air preheater t g1 = high temperature air preheater inlet combustion gas temperature = 388 ° C t g2 = high temperature air preheater outlet combustion gas temperature = 330 ° C, Q 1 = heat exchange amount of high temperature air preheater = GC × (t g1 -t g2 ) a × C pg = 298,900 × (388-330 ) × 0.26 = 4,507,000Kcal / H.
また， ta4＝高温空気予熱器出口空気温度 ＝350℃ Δtm1＝高温空気予熱器の対数平均温度差 ＝７２℃ K1＝高温空気予熱器の熱伝達係数 ＝25Kcal／m2h℃ では， (2)低温空気予熱器の設計 tg3＝低温空気予熱器入口燃焼ガス温度 ＝330℃ tg4＝低温空気予熱器出口燃焼ガス温度 ＝226℃（ボイラ効率２％向上させる時 の排ガス温度）では、 Ｑ２＝低温空気予熱器の熱交換量 ＝GC×（tg3−tg4）×Cpg ＝298,900×（330−226）×0.260 ＝8,082,000Kcal／Ｈ となる。In addition, ta4 = high temperature air preheater outlet air temperature = 350 ° C Δt m1 = logarithmic mean temperature difference of high temperature air preheater = 72 ° C K 1 = heat transfer coefficient of high temperature air preheater = 25 Kcal / m 2 h ℃, (2) Design of low temperature air preheater t g3 = low temperature air preheater inlet combustion gas temperature = 330 ° C t g4 = low temperature air preheater outlet combustion gas temperature = 226 ° C (exhaust gas temperature when improving boiler efficiency by 2%) , Q 2 = heat exchange amount of the low temperature air preheater = GC × (t g3 −t g4 ) × C pg = 298,900 × (330−226) × 0.260 = 8,082,000 Kcal / H.
また， ta1＝低温空気予熱器の入口空気温度 ＝１０℃ Δtm2＝低温空気予熱器の対数平均温度差 ＝115゜C Ｋ２＝低温空気予熱器の熱伝達係数 ＝25Kcal／m2h℃ では， (3)空気式ボイラ給水加熱器の設計 Ｑｗ＝空気式ボイラ給水加熱器の熱交換量 ＝AC×（ta2−ta3）×Cpa ＝123,480×（277−201）×0.245 ＝2,299,000Kcal／Ｈ となり， tw1＝空気式ボイラ給水加熱器の入口燃料ガ ス温度 ＝140℃ Δtm(W)＝空気式ボイラ給水加熱器の対数平均温 度差 ＝85℃ Ｋ（ｗ）＝空気式ボイラ給水加熱器の熱伝達係数 ＝35Kcal／m2h℃ では， Ｈ・Ｓ（ｗ）＝空気式ボイラ給水加熱器の必要伝熱面 積 ＝773m2 となる。Also, t a1 = inlet air temperature of low temperature air preheater = 10 ° C Δt m2 = Logarithmic mean temperature difference of low temperature air preheater = 115 ° C K 2 = Heat transfer coefficient of low temperature air preheater = 25 Kcal / m 2 h ℃, (3) pneumatic boiler feedwater heater design Q w = amount of heat exchange air boiler feedwater heater = AC × (t a2 -t a3 ) × C pa = 123,480 × (277-201) × 0.245 = 2,299,000Kcal / H, t w1 = pneumatic boiler feed water heater inlet fuel gas temperature = 140 ° C Δt m (W) = logarithmic mean temperature difference of air boiler feedwater heater = 85 ℃ K (w) = heat transfer coefficient of air boiler feedwater heater = 35Kcal / m 2 h ℃, H ・ S (w ) = Required heat transfer surface area of the air boiler feedwater heater = 773m 2 .
以上のように、従来の空気予熱器の必要伝熱面積3,780m
2に比べて約１．４倍（高温空気予熱器の必要伝熱面積
2,500m2＋低温空気予熱器の必要伝熱面積2,810m2＝5,31
0m2）の空気予熱器と773m2の空気式ボイラ給水加熱器を
設置すれば，ボイラ効率は約２％向上させることができ
る。As described above, the required heat transfer area of the conventional air preheater is 3,780m.
Approximately 1.4 times compared to 2 (required heat transfer area of high temperature air preheater
2,500m 2 + required heat transfer area of low temperature air preheater 2,810m 2 = 5,31
If a 0 m 2 ) air preheater and a 773 m 2 air boiler feedwater heater are installed, the boiler efficiency can be improved by about 2%.
このように、ボイラの燃料量が２％節減できることは、
上記設備費を短時間の中に原価償却するのに充分であ
り、十分採算が合うものである。In this way, it is possible to reduce the amount of fuel in the boiler by 2%.
It is sufficient to depreciate the above equipment cost in a short time, and it is profitable.
第１図は本発明の排熱回収ボイラ装置の系統図、第２図
は第１図における燃焼ガスと空気が高温空気予熱器と低
温空気予熱器で熱交換され、更に空気式ボイラ給水加熱
器で空気とボイラ給水が熱交換される時に熱収支の状態
図、第３図は従来の排熱回収ボイラ装置の系統図、第４
図は第３図における燃焼ガスと空気が空気予熱器で熱交
換される時の状態と熱収支を示す状態図である。 １…ボイラ，２…高温空気予熱器，３…低温空気予熱
器，４…誘引通風機，５…煙突，６…煙道，７…押込通
風機，８…空気式ボイラ給水加熱器，９…バーナ風箱，
１０…風道，１１…燃料供給管，１２…Ｕ字形水封器，
１３…バーナ，１４…給水ポンプ，１５…給水配管，１
６…気水ドラム。FIG. 1 is a system diagram of an exhaust heat recovery boiler device of the present invention, and FIG. 2 is heat exchange of combustion gas and air in FIG. 1 by a high temperature air preheater and a low temperature air preheater, and further an air type boiler feed water heater. Fig. 3 is a state diagram of heat balance when heat is exchanged between air and boiler feed water. Fig. 3 is a system diagram of a conventional exhaust heat recovery boiler device.
The figure is a state diagram showing the state and heat balance when the combustion gas and air in FIG. 3 are heat-exchanged by the air preheater. 1 ... Boiler, 2 ... High temperature air preheater, 3 ... Low temperature air preheater, 4 ... Induction draft fan, 5 ... Chimney, 6 ... Flue, 7 ... Push draft fan, 8 ... Pneumatic boiler feed water heater, 9 ... Burner box,
10 ... Wind passage, 11 ... Fuel supply pipe, 12 ... U-shaped water seal,
13 ... Burner, 14 ... Water supply pump, 15 ... Water supply pipe, 1
6 ... Steam drum.
Claims (1)
予熱器を高温部空気予熱器と低温部空気予熱器とに分割
し、当該ボイラの排ガスを前記高温部空気予熱器、低温
部空気予熱器の順に導く煙道と、燃焼用空気を前記低温
部空気予熱器、高温部空気予熱器の順に導く風道とを設
け、前記低温部空気予熱器と前記高温部空気予熱器とを
連通する前記風道に空気式ボイラ給水加熱器を介装した
ことを特徴とするボイラ装置。1. An air preheater for a boiler that uses low-calorie gas as a fuel is divided into a high temperature part air preheater and a low temperature part air preheater, and exhaust gas of the boiler is heated to the high temperature part air preheater and the low temperature part air preheater. A flue leading in the order of the air conditioner, and an air passage leading the combustion air in the order of the low temperature part air preheater and the high temperature part air preheater to connect the low temperature part air preheater and the high temperature part air preheater. A boiler apparatus, wherein an air type boiler feed water heater is provided in the air passage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59178070A JPH063285B2 (en) | 1984-08-27 | 1984-08-27 | Boiler equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59178070A JPH063285B2 (en) | 1984-08-27 | 1984-08-27 | Boiler equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6155503A JPS6155503A (en) | 1986-03-20 |
| JPH063285B2 true JPH063285B2 (en) | 1994-01-12 |
Family
ID=16042087
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59178070A Expired - Fee Related JPH063285B2 (en) | 1984-08-27 | 1984-08-27 | Boiler equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH063285B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103836609B (en) * | 2013-12-04 | 2016-05-04 | 成信绿集成股份有限公司 | A kind of emission-reducing system of boiler of power plant exhaust gas dust |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5338454B2 (en) * | 1973-01-16 | 1978-10-16 | ||
| JPS5989901A (en) * | 1982-11-15 | 1984-05-24 | 三菱重工業株式会社 | Boiler device |
-
1984
- 1984-08-27 JP JP59178070A patent/JPH063285B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6155503A (en) | 1986-03-20 |
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