JPH0194920A - Method for treating waste liquid in flue gas treatment apparatus - Google Patents
Method for treating waste liquid in flue gas treatment apparatusInfo
- Publication number
- JPH0194920A JPH0194920A JP62249999A JP24999987A JPH0194920A JP H0194920 A JPH0194920 A JP H0194920A JP 62249999 A JP62249999 A JP 62249999A JP 24999987 A JP24999987 A JP 24999987A JP H0194920 A JPH0194920 A JP H0194920A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- liquid
- cooling tower
- gas
- flue gas
- 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
- 239000007788 liquid Substances 0.000 title claims abstract description 73
- 238000011282 treatment Methods 0.000 title claims abstract description 24
- 239000002699 waste material Substances 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title abstract description 10
- 239000003546 flue gas Substances 0.000 title abstract description 10
- 238000001816 cooling Methods 0.000 claims abstract description 50
- 239000000428 dust Substances 0.000 claims abstract description 38
- 238000010521 absorption reaction Methods 0.000 claims abstract description 36
- 239000004071 soot Substances 0.000 claims abstract description 20
- 239000002351 wastewater Substances 0.000 claims description 16
- 239000007787 solid Substances 0.000 claims description 13
- 150000002366 halogen compounds Chemical class 0.000 claims description 9
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 121
- 239000002002 slurry Substances 0.000 abstract description 20
- 229910052602 gypsum Inorganic materials 0.000 abstract description 17
- 239000010440 gypsum Substances 0.000 abstract description 17
- 239000000463 material Substances 0.000 abstract description 5
- 239000003513 alkali Substances 0.000 abstract 1
- 239000003153 chemical reaction reagent Substances 0.000 abstract 1
- 150000004820 halides Chemical class 0.000 abstract 1
- 230000003472 neutralizing effect Effects 0.000 abstract 1
- 239000011343 solid material Substances 0.000 abstract 1
- 238000005406 washing Methods 0.000 abstract 1
- 238000006386 neutralization reaction Methods 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 15
- 238000004140 cleaning Methods 0.000 description 9
- 230000007423 decrease Effects 0.000 description 9
- 239000012530 fluid Substances 0.000 description 9
- 238000005260 corrosion Methods 0.000 description 8
- 230000007797 corrosion Effects 0.000 description 8
- 238000003303 reheating Methods 0.000 description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 7
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 7
- 235000011116 calcium hydroxide Nutrition 0.000 description 7
- 239000000920 calcium hydroxide Substances 0.000 description 7
- 230000008021 deposition Effects 0.000 description 7
- 230000003647 oxidation Effects 0.000 description 7
- 238000007254 oxidation reaction Methods 0.000 description 7
- 235000019738 Limestone Nutrition 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 239000006028 limestone Substances 0.000 description 6
- 230000002265 prevention Effects 0.000 description 6
- 229910052736 halogen Inorganic materials 0.000 description 5
- 150000002367 halogens Chemical class 0.000 description 5
- 239000000779 smoke Substances 0.000 description 5
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 4
- 235000010261 calcium sulphite Nutrition 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 150000004679 hydroxides Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は排液を効率よく蒸発乾燥ができ、しかもガス−
ガスヒータ以外の再加熱装置を必要としない湿式排ガス
処理装置の排液の処理方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention enables efficient evaporative drying of waste liquid, and moreover,
The present invention relates to a method for treating waste liquid from a wet exhaust gas treatment device that does not require a reheating device other than a gas heater.
第２図は、従来の石炭焚きボイラ排ガスの排ガス処理装
置からの排液処理の１例の工程図である。FIG. 2 is a process diagram of an example of waste liquid treatment from a conventional coal-fired boiler exhaust gas treatment device.
第２図において１石炭焚きボイラ１から排ガス２を乾式
集じん装置３に導き排ガス中に含まれているばいじんを
固形物４として系外に排出する。次いで、ばいじんの大
部分が除去された排ガス５をガス・ガスヒータおに導き
、吸収塔８からの浄化排ガス９と熱交換させた後、冷却
塔６に導き、ばいじんとハロゲン化合物を殆んど除去し
た後ライン７により吸収塔８に導き亜硫酸ガス（ＳＯ２
）を除去する。吸収塔８からの浄化排ガス９は、ガスガ
スヒータおで加熱された後、再加熱装置襲で再び加熱さ
れ、ライン四を通って煙突刃より大気中に放出される。In FIG. 2, exhaust gas 2 is introduced from a coal-fired boiler 1 to a dry dust collector 3, and the soot and dust contained in the exhaust gas is discharged as solid matter 4 to the outside of the system. Next, the flue gas 5 from which most of the soot and dust has been removed is led to a gas heater, where it is exchanged with the purified flue gas 9 from the absorption tower 8, and then led to the cooling tower 6, where most of the soot and halogen compounds are removed. After that, the line 7 leads to the absorption tower 8 where sulfur dioxide gas (SO2
) to remove. The purified exhaust gas 9 from the absorption tower 8 is heated in a gas heater, then heated again in a reheating device, and is discharged into the atmosphere through a chimney blade through a line 4.
冷却塔６においてはポンプ１０により洗浄液を循環ライ
ン１１を通して循環スプレーさせ排ガス５を洗浄し、ば
いじんとハロゲン化合物を捕集すると共に排ガスの増湿
冷却を行なう。また蒸発水を補うために補給水１２を冷
却塔６に供給する。更に排ガス５から捕集されたばいじ
んやハロゲン化合物等が蓄積している冷却塔循環液の一
部を循環ライン１１より分岐し、ライン１３を通して中
和槽５へ送る。吸収塔８では排ガス中に含まれているＳ
Ｏ□は、循環ライン１７を通して吸収塔８内に循環スプ
レーされている石灰石又は消石灰を含むスラリー液と接
触し吸収され亜硫酸カルシウムとなる。生成した亜硫酸
カルシウムを含むスラリー液はポンプ１４に・よって循
環され、その一部はライン１５を経て酸化塔１６に送ら
れ、空気酸化によって−石膏スラリーとなる。酸化塔１
６からの石膏スラリー液はライン１８を通り、固液分離
器１９に送られ【。In the cooling tower 6, a pump 10 circulates and sprays a cleaning liquid through a circulation line 11 to clean the exhaust gas 5, collect soot and halogen compounds, and humidify and cool the exhaust gas. Also, makeup water 12 is supplied to the cooling tower 6 to supplement evaporated water. Furthermore, a part of the cooling tower circulation liquid in which soot, halogen compounds, etc. collected from the exhaust gas 5 are accumulated is branched from the circulation line 11 and sent to the neutralization tank 5 through the line 13. In the absorption tower 8, S contained in the exhaust gas is
O□ comes into contact with a slurry liquid containing limestone or slaked lime that is circulated and sprayed into the absorption tower 8 through the circulation line 17, and is absorbed and becomes calcium sulfite. The produced slurry liquid containing calcium sulfite is circulated by a pump 14, and a part of it is sent to an oxidation tower 16 through a line 15, where it is turned into a gypsum slurry by air oxidation. Oxidation tower 1
The gypsum slurry liquid from 6 passes through line 18 and is sent to solid-liquid separator 19.
副生石膏頭と炉液（吸収系排水）２１に分離され。Separated into by-product gypsum head and furnace liquid (absorption system wastewater) 21.
炉液２１の大部分は石灰石又は消石灰ｎと混合されて吸
収塔８に戻される。一方、炉液４の一部は。Most of the furnace liquid 21 is mixed with limestone or slaked lime and returned to the absorption tower 8. On the other hand, a part of the furnace liquid 4.
可溶性不純物の系内への蓄積防止のためにライン久より
中和槽６に供給される。中和槽５では、ライン冴より消
石灰あるいは石灰石が供給され、ライン１３より供給さ
れる冷却塔６循環液の一部と。In order to prevent soluble impurities from accumulating in the system, it is supplied to the neutralization tank 6 from the line. In the neutralization tank 5, slaked lime or limestone is supplied from the line 13, and a part of the circulating liquid from the cooling tower 6 is supplied from the line 13.
ライン久より供給される炉液２１の一部に含まれている
溶解金属の水酸化物及び石膏が生成する。中和槽５より
ライン怒を通りて上記の水酸化物９石膏及び排ガスから
捕集したばいじんを含んだスラリー液を乾式集じん装置
３の上流に設置された蒸発装置ｎに全量供給する。蒸発
装置Ｉではラインかよりのスラリー液が２流体ノズルよ
り噴霧され小さな液滴となる。七〇液滴と排ガス２が蒸
発装置τで混合され液滴は蒸発される。液滴のうち。Hydroxide and gypsum of dissolved metals contained in a portion of the furnace liquid 21 supplied from the line are generated. The slurry liquid containing the above-mentioned hydroxide 9 gypsum and soot and dust collected from the exhaust gas is supplied in its entirety from the neutralization tank 5 through a line to an evaporator n installed upstream of the dry dust collector 3. In the evaporator I, the slurry liquid from the line is sprayed from a two-fluid nozzle to form small droplets. 70 Droplets and exhaust gas 2 are mixed in the evaporator τ, and the droplets are evaporated. Out of droplets.
乾燥されない固形物は、付着物となるが、付着物堆積防
止装置３１により付着物！として排出される。Solids that are not dried become deposits, but the deposit prevention device 31 removes the deposits! It is discharged as.
乾燥された固形物は排ガス２中のばいじんとともに乾式
集じん装置３により固形物４として捕集され排出される
。The dried solids are collected together with soot and dust in the exhaust gas 2 by a dry dust collector 3 as solids 4 and discharged.
このような従来の排液処理方法にはつぎのような問題点
がある。Such conventional waste liquid treatment methods have the following problems.
（１） 吸収系排水を冷却塔排水とともに中和処理し
て乾式集じん装置の上流に噴霧していたので。(1) The absorption system wastewater was neutralized together with the cooling tower wastewater and then sprayed upstream of the dry dust collector.
噴霧量が冷却排水のみより増加する。その結果排ガス温
度の低下が激しく、ガスガスヒータで熱回収後頁に再加
熱を行なわないと排ガス温度が低く、白煙が発生するた
め煙突より直接大気中に放出できない。The amount of spray increases compared to cooling wastewater alone. As a result, the temperature of the exhaust gas drops sharply, and unless the exhaust gas is reheated after the heat is recovered using a gas heater, the exhaust gas temperature will be too low and white smoke will be generated, so it cannot be released directly into the atmosphere from the chimney.
（２）吸収系排水及び冷却塔排水の全量なスラＩＪ−液
として２流体ノズルより噴霧すると、液滴が蒸発した後
の付着物が堆積するため、堆積を防止するための付着物
堆積防止装置が不可欠である。(2) When the entire volume of absorption system wastewater and cooling tower wastewater is sprayed as a slug IJ liquid from a two-fluid nozzle, deposits will accumulate after the droplets have evaporated, so a deposit deposition prevention device is installed to prevent deposition. is essential.
（３）多量の冷却塔補給水が必要である。(3) A large amount of cooling tower makeup water is required.
（４）ハロゲンによる腐食（ノズル、冷却塔、配管等の
腐食）及び懸濁物による配管、ノズルの摩耗並びに閉塞
が起りやすい。(4) Corrosion caused by halogen (corrosion of nozzles, cooling towers, piping, etc.) and abrasion and clogging of piping and nozzles caused by suspended matter are likely to occur.
本発明はかかる事情に鑑みなされたもので。The present invention was made in view of such circumstances.
（１）煙突入口排ガス温度を所定の温度とするのに。(1) To set the flue gas temperature at the smoke inlet to a predetermined temperature.
ガスガスヒータ以外の再加熱装置を不要とする。Eliminates the need for reheating devices other than gas gas heaters.
（２）乾式集じん装置の上流において、排ガス中に噴霧
される排液を効率よく蒸発、乾燥出来るようにする。(2) Upstream of the dry dust collector, the waste liquid sprayed into the exhaust gas can be efficiently evaporated and dried.
（３）吸収系排水を冷却塔の補給水として使用可能とす
る。(3) Absorption system wastewater can be used as make-up water for cooling towers.
（４） 付着物堆積防止装置を極力無くするようにす
る。(4) Eliminate deposit deposition prevention devices as much as possible.
（５） ハロゲンによる腐食並びに、懸濁物による摩
耗及び閉塞を少くする
ことを特徴とする湿式排ガス処理装置の排液の処理方法
を提供することを目的としたものである。(5) It is an object of the present invention to provide a method for treating waste liquid from a wet exhaust gas treatment device, which is characterized by reducing corrosion caused by halogens and wear and clogging caused by suspended matter.
以上の従来の技術の問題点を解決するために鋭意研究を
重ねた結果、乾式集じん装置の上流に注入する排液量を
、前記乾式集じん装置の上流に注入した時の排ガス温度
の低下を４℃〜８℃になるように調整することによりそ
の目的を達成することを見出し、その知見に基づいて本
発明をなすに至ったものである。As a result of intensive research to solve the above-mentioned problems with the conventional technology, we have found that the amount of waste fluid injected upstream of the dry dust collector reduces the exhaust gas temperature when it is injected upstream of the dry dust collector. The inventors have discovered that the objective can be achieved by adjusting the temperature to 4°C to 8°C, and based on this knowledge, the present invention has been developed.
すなわち本発明はボイラ等の排ガスを乾式集じん装置に
導き排ガス中に含まれているばいじんを除去して湿式排
ガス処理装置に送り前記湿式排ガス処理装置の冷却塔で
排ガス中はばいじんとハロゲン化合物を捕集するととも
に排ガスを冷却した後、吸収塔に導き排ガス中の硫黄酸
化物を除去する排ガス処理装置において、吸収系排水を
前記吸収塔及び前記冷却塔及び前記冷却塔に供給し、か
つ前記冷却塔の循環液の１部を抜き出し、前記乾式集じ
ん装置の上流に、排ガス温度の低下が４℃〜８℃の範囲
内に留まるようにボイラ等の負荷信号または排ガス流量
信号により流入量を制御して注入し蒸発させ、この乾燥
固形物を前記乾式集じん装置で捕集することを特徴とす
る排ガス処理装置における排液の処理方法を提案するも
のである。That is, the present invention introduces exhaust gas from a boiler, etc. to a dry type dust collector, removes the soot and dust contained in the exhaust gas, and sends it to a wet type exhaust gas treatment device, where the cooling tower of the wet type exhaust gas treatment device removes soot and halogen compounds from the exhaust gas. In an exhaust gas treatment device that collects and cools the exhaust gas and then introduces it to an absorption tower to remove sulfur oxides in the exhaust gas, the absorption system wastewater is supplied to the absorption tower, the cooling tower, and the cooling tower, and the cooling A part of the circulating liquid of the tower is extracted and the inflow amount is controlled by the load signal of the boiler etc. or the exhaust gas flow rate signal so that the decrease in exhaust gas temperature remains within the range of 4°C to 8°C. The present invention proposes a method for treating waste liquid in an exhaust gas treatment apparatus, characterized in that the dry solids are injected and evaporated, and the dry solids are collected by the dry dust collector.
本発明の方法においては、湿式排ガス処理装置からの排
液量を、前記乾式集じん装置の上流に注入した時の排ガ
ス温度の低下を４〜８℃になるように調整する。In the method of the present invention, the amount of waste liquid from the wet exhaust gas treatment device is adjusted so that the temperature of the exhaust gas decreases by 4 to 8° C. when injected upstream of the dry dust collector.
なお排ガス温度の低下を４〜８℃の範囲にとどめる理由
は次のとおりである。The reason why the exhaust gas temperature is kept within the range of 4 to 8°C is as follows.
（１） 排ガス温度の低下を８℃以上にすると、乾式
集じん装置の上流に注入する液量が多くなって煙道的付
着物が多くなり、又温度の低下が大きいためガス・ガス
ヒータのみの熱回収だけでは煙突入口ガス温度を所定の
温度に保持できなくなり、別途排ガス温度を上昇させる
手段が必要となる。(1) If the exhaust gas temperature decreases to 8℃ or more, the amount of liquid injected upstream of the dry dust collector will increase, resulting in more deposits in the flue, and since the temperature decrease will be large, it will be necessary to use only gas and gas heaters. Heat recovery alone cannot maintain the smoke inlet gas temperature at a predetermined temperature, and a separate means for raising the exhaust gas temperature is required.
（２）排ガス温度の低下を、４℃以下にすると冷却塔循
環液の抜き出し量が少なすぎて排液を濃縮しすぎるので
、排液中のＣＪ？濃度が極端たとえば２０，０００ ｐ
ｐｍ以上となり、材料の腐食又、懸濁物濃度が極端たと
えば１０俤以上になり材料の摩耗がはげしくなる。(2) If the exhaust gas temperature is lowered to 4°C or less, the amount of cooling tower circulating fluid withdrawn will be too small and the effluent will be too concentrated. If the concentration is extreme, e.g. 20,000p
pm or more, corrosion of the material or concentration of suspended solids becomes extreme, for example, 10 yen or more, resulting in severe wear of the material.
排ガス温度の低下を４〜８℃にするには、排ガス量（ｍ
”Ｎ／Ｈ）に対する液量（Ｉｍ ） の割合は。In order to reduce the exhaust gas temperature by 4 to 8℃, the exhaust gas amount (m
What is the ratio of liquid volume (Im) to N/H)?
！２〜４．４ Ｘ １０″″３（１部ｍ３Ｎ ）になる
が−このＪ：５に冷却塔排水を抜き出し、冷却塔内に吸
収系排水を供給しても、冷却塔循環液内に含まれている
ハロゲン化合物やばいじんの作用により冷却塔における
石膏スケールの生成が抑制され２石膏スケールによるト
ラブルが発生しないので吸収系排水な冷却塔への補給水
として活用することができる。! 2 to 4.4 x 10''''3 (1 part m3N) - Even if the cooling tower wastewater is extracted at this J:5 and the absorption system wastewater is supplied into the cooling tower, the amount of water contained in the cooling tower circulating fluid will be The formation of gypsum scale in the cooling tower is suppressed by the action of the halogen compounds and dust contained therein, and troubles caused by gypsum scale do not occur, so it can be used as make-up water for the cooling tower, which is absorption system wastewater.
また、この排ガス量に対する液量の割合が増加すると、
蒸発塔内の付着物が増加し、液量の割合が減少すると、
液中のハロゲン濃度たとえばＣＪ 。Also, as the ratio of liquid volume to exhaust gas volume increases,
When the deposits in the evaporation tower increase and the liquid volume ratio decreases,
The halogen concentration in the liquid, for example CJ.
Ｆ及び懸濁物濃度が増加し、冷却塔における材料の腐食
、摩耗及び、上述した石膏スケールが発生する。F and suspended solids concentrations increase, leading to material corrosion, wear and the aforementioned gypsum scale in the cooling tower.
また、上述のように、排ガス流量に応じて排ガス中に噴
霧される排液量も増減するので、排液の噴霧による排ガ
スの温度低下は一定となる。したがってボイラー等の負
荷が低下して排ガス量が減少しても、噴霧される排液量
が少くなり排液の噴霧による排ガスの温度低下は小さく
なるので、ガス−ガスヒータでの熱回収だけで、煙突よ
り大気中に放出する排ガス温度を所定の温度に保つ事が
可能となりスチームガスヒータ等の外部熱源による再加
熱装置は不要となる。Further, as described above, since the amount of waste liquid sprayed into the exhaust gas also increases or decreases depending on the flow rate of the exhaust gas, the temperature drop of the exhaust gas due to spraying of the waste liquid remains constant. Therefore, even if the load on the boiler etc. decreases and the amount of exhaust gas decreases, the amount of waste liquid sprayed will decrease and the temperature drop in the exhaust gas due to the spray of waste liquid will be small, so heat recovery by the gas-gas heater alone will reduce the amount of waste gas sprayed. It is possible to maintain the temperature of the exhaust gas discharged into the atmosphere from the chimney at a predetermined temperature, making it unnecessary to use a reheating device using an external heat source such as a steam gas heater.
さらに、排ガスから運ばれるバロゲン及びフライアッシ
為等が排液中に含まれる濃度は、排ガスに対する噴霧す
る液量を一定にする事により一定となるので、ノズル配
管の腐食及び摩耗、閉塞がなくなる。 −
〔実施例〕
次に本発明の１実施例を第１図を用いて詳細に説明する
。Furthermore, the concentration of balogens, fly ash, etc. carried from the exhaust gas in the waste liquid becomes constant by keeping the amount of liquid sprayed against the exhaust gas constant, so corrosion, wear, and clogging of the nozzle piping are eliminated. - [Example] Next, an example of the present invention will be described in detail with reference to FIG.
第１図は本発明の方法の１実施例の工程図である。FIG. 1 is a process diagram of one embodiment of the method of the present invention.
第１図において、符号１〜２７及びＩは第、２図と全く
同様である。図示のように吸収塔８と煙突Ｉとの間には
、ライン９とガスガスヒータおだけで第２図で示した再
加熱装置部及びライン四はない。In FIG. 1, symbols 1 to 27 and I are completely the same as in FIGS. As shown, between the absorption tower 8 and the chimney I, there is only a line 9 and a gas heater, and there is no reheating device section or line 4 shown in FIG. 2.
又蒸発装置ごと乾式集じん装置３との間には付着物堆積
防止装置３１はない。第１図では固液分離器１９で副生
石膏加と炉液２１に分離し、Ｆ液量１は吸収塔８及びラ
イン父を通して冷却塔６に供給されており、中和槽５に
は供給しない。Further, there is no deposit deposition prevention device 31 between the evaporator and the dry dust collector 3. In Fig. 1, the solid-liquid separator 19 separates the by-product gypsum and the furnace liquid 21, and the F liquid amount 1 is supplied to the cooling tower 6 through the absorption tower 8 and the line head, and is not supplied to the neutralization tank 5. .
第１図において石炭焚きボイラ１から排ガス２を乾式集
じん装置３に導き排ガス中に含まれているばいじんを固
形物４として系外に排出する。次いでばいじんの大部分
が除去された排ガス５を。In FIG. 1, exhaust gas 2 is introduced from a coal-fired boiler 1 to a dry dust collector 3, and the soot and dust contained in the exhaust gas is discharged as solid matter 4 to the outside of the system. Next, the exhaust gas 5 from which most of the soot and dust has been removed.
ガスガスヒータおに導き、吸収塔からの浄化排ガス９と
熱交換させた後、冷却塔６に導き、ばいじんとハロゲン
化合物を殆んど除去して、ライン７を通して吸収塔８に
導き、Ｓ０２を除去する。吸収塔８からの浄化排ガス９
は再びガスガスヒータお゛で加熱された後煙突Ｉより大
気中に放出される。After passing through a gas heater and exchanging heat with the purified exhaust gas 9 from the absorption tower, it is led into a cooling tower 6 to remove most of the soot and halogen compounds, and then into an absorption tower 8 through a line 7 to remove S02. do. Purified exhaust gas 9 from absorption tower 8
After being heated again by the gas heater O, it is released into the atmosphere from the chimney I.
冷却塔６では、ポンプＩＯＫより洗浄液を循環ライン１
１を通してスプレーさせ排ガス５を洗浄し、ばいじんと
ハロゲン化合物を捕集すると共に排ガスの増湿冷却を行
なう。また蒸発水を補うために。In the cooling tower 6, the cleaning liquid is circulated from the pump IOK to the circulation line 1.
1 to clean the exhaust gas 5, collect soot and halogen compounds, and humidify and cool the exhaust gas. Also to compensate for evaporated water.
補給水１２及び石膏スラリーを固液分離した炉液（吸収
系排水）をラインＵを通して冷却塔に供給する。更に、
排ガス５から捕集されたばいじんやハロゲン化合物など
が蓄積している冷却塔循環液の一部を、循環ライン１１
より１分岐し、ライン１３を通して中和槽６へ送る。吸
収塔８では排ガス中に含まれているＳ０２は循環ライン
１７を通って吸収塔８で循環スプレーされる石灰石又は
消石灰を含むスラリー液に接触吸収され亜硫酸カルシウ
ムとなり生成亜硫酸カルシウムを含むスラリー液は。Makeup water 12 and furnace liquid (absorption system wastewater) obtained by solid-liquid separation of gypsum slurry are supplied to the cooling tower through line U. Furthermore,
A portion of the cooling tower circulating fluid in which soot and halogen compounds collected from the exhaust gas 5 are collected is transferred to the circulation line 11.
It is branched into one branch and sent to the neutralization tank 6 through a line 13. In the absorption tower 8, S02 contained in the exhaust gas passes through the circulation line 17 and is absorbed in contact with a slurry containing limestone or slaked lime that is circulated and sprayed in the absorption tower 8 to become calcium sulfite, and the slurry containing calcium sulfite is produced.
ポンプ１４によって循環され、その一部はライン１５を
経て酸化塔１６に送られ、空気酸化によって石膏スラリ
ーとなる。酸化塔１６からの石膏スラリー液はライン１
８を通り、固液分離器１９に送られて、副生石膏印とｐ
液量１に分離され、Ｐ液量１の大部分は。It is circulated by a pump 14, and a part of it is sent to an oxidation tower 16 via a line 15, where it is turned into gypsum slurry by air oxidation. Gypsum slurry liquid from oxidation tower 16 is in line 1
8, is sent to the solid-liquid separator 19, and the by-product plaster stamp and p
It is separated into liquid volume 1, and most of the P liquid volume 1 is.
石灰石、又は消石灰ηと混合されて吸収塔８に戻される
。一方、Ｐ液量１の一部は可溶性不純物蓄積防止のため
に、ラインあより冷却塔７へ供給される。It is mixed with limestone or slaked lime η and returned to the absorption tower 8. On the other hand, a part of the P liquid amount 1 is supplied to the cooling tower 7 through the line in order to prevent accumulation of soluble impurities.
ボイラー負荷信号又は排ガス流量の信号３９を調節計４
０により外力信号とし、調節弁４１で冷却塔抜出し液の
流量を調整して冷却塔循環液の一部をライン１３を通し
て中和槽６に送る。The boiler load signal or exhaust gas flow rate signal 39 is sent to the controller 4.
0 as an external force signal, the control valve 41 adjusts the flow rate of the cooling tower withdrawn liquid, and a part of the cooling tower circulating liquid is sent to the neutralization tank 6 through the line 13.
また、ツイン冴より消石灰あるいは石灰石等のアルカリ
剤が中和槽５に供給され、冷却塔循環液中の溶解金属の
水酸化物及び石膏が生成される。In addition, an alkaline agent such as slaked lime or limestone is supplied from the twin sae to the neutralization tank 5, and hydroxides of dissolved metals and gypsum in the cooling tower circulating fluid are generated.
中和槽５より２インあを通って上記水酸化物。The above hydroxide passes through a 2-inch tank from neutralization tank 5.
石膏及び排ガスから捕集されたばいじんを含んだスラリ
ーが乾式集じん装置３の上流に設置された蒸発装置ｎに
全量供給される。The entire slurry containing gypsum and soot and dust collected from the exhaust gas is supplied to an evaporator n installed upstream of the dry dust collector 3.
蒸発装置τでは、ライン加より供給されたスラリーが、
２流体ノズルより噴霧され、小さな液滴となる。その液
滴と排ガス２とが蒸発装置ｎで混合され、液滴−蒸発乾
燥され、生成した固形物は下流の乾式集じん装置３で排
ガス２中のばいじんとともに固形物４として捕集排出さ
れる。In the evaporator τ, the slurry supplied from the line is
It is sprayed from a two-fluid nozzle and becomes small droplets. The droplets and exhaust gas 2 are mixed in an evaporator n, and the droplets are evaporated to dryness, and the generated solids are collected and discharged as solids 4 together with the soot and dust in the exhaust gas 2 in a downstream dry dust collector 3. .
以上詳細に説明したように本実施例の方法によれば９次
の効果を奏することができる。As described above in detail, the method of this embodiment can produce the ninth-order effect.
（１） 排ガス中に噴霧する液量な調整することによ
り、排ガスの温度低下は小さり、シたがってガスガスヒ
ータでの熱回収だけで煙突入口ガス温度を所定の温度に
保持できるので別途再加熱装置は不要となる。(1) By adjusting the amount of liquid sprayed into the exhaust gas, the temperature drop in the exhaust gas is small, and the smoke inlet gas temperature can be maintained at a specified temperature simply by recovering heat with the gas heater, so it can be reheated separately. No equipment is required.
（２）冷却塔の補給水として吸収系排水が使用できるの
で、系外から供給する補給水を低減できる。(2) Absorption system wastewater can be used as make-up water for the cooling tower, so the amount of make-up water supplied from outside the system can be reduced.
（３）効率よく液滴が蒸発されるため付着物が少なくな
り、付着物堆積防止装置が不要となる。(3) Since the droplets are efficiently evaporated, the amount of deposits is reduced, and a device for preventing deposition of deposits is not required.
（４）ハロゲン濃度をある濃度レベル（５０００〜２０
．０００ ｐｐｌ’）に保つことにより、材料の腐食が
少なくなる。(4) Change the halogen concentration to a certain concentration level (5000 to 20
．． 000 ppl') reduces material corrosion.
（５）ｓ濁り濃度をある濃度レベル（１０１以下）にす
ることにより、ノズル配管の摩耗及び閉塞がなくなる。(5) By setting the s turbidity concentration to a certain concentration level (101 or less), wear and clogging of the nozzle piping are eliminated.
以上の作用として石炭焚きボイラからの排ガスを処理す
る場合について説明したが、油焚きボイラからの排ガス
を処理する場合についても同様のことができる。Although the above operation has been described for the case where exhaust gas from a coal-fired boiler is treated, the same effect can be applied to the case where exhaust gas from an oil-fired boiler is treated.
次にパイロットプラントにより行なった比較例及び本発
明の実験例について説明する。Next, a comparative example and an experimental example of the present invention conducted using a pilot plant will be explained.
比較例
石炭焚排ガス４，０ＯＯＮ−４を処理する第２図の態様
のノぞイロットプラントにより従来法の確認を実施した
。排ガス２の性状を第１表に示す。Comparative Example The conventional method was confirmed using a Nozoirot plant of the embodiment shown in FIG. 2, which processes 4,0 OON-4 of coal-fired exhaust gas. The properties of exhaust gas 2 are shown in Table 1.
冷却塔６の洗浄液１１をライン１３から連続的に加１／
Ｈで中和槽部に供給した。その時の洗浄液の液性状を第
２表に示す。The cleaning liquid 11 of the cooling tower 6 is continuously added from the line 13.
H was supplied to the neutralization tank section. Table 2 shows the liquid properties of the cleaning liquid at that time.
第 ２ 表 冷却塔洗浄液の液性状
石膏分離Ｆ液２１の一部をラインｎから連続的に１２
ｌＡで中和槽５に供給した。その時の炉液の液性状を第
３表に示す。Table 2 Liquid properties of cooling tower cleaning fluid A portion of the gypsum separated F solution 21 was continuously supplied from line n to 12
1A was supplied to the neutralization tank 5. Table 3 shows the properties of the furnace liquid at that time.
第 ３ 宍 石膏分離ｐ液性状
中和槽６にて冷却塔６かもの洗浄液１３と石膏分離Ｆ液
ｎを攪拌混合しながらＣａ （ＯＨ）２ 粉末冴を加
え、中和スラリーの、Ｈを７〜１２平均１１になるよう
に添加した。Ｃａ （ＯＨ）２粉末の平均供給量は６０
０９βであった。 中和槽６の中和スラリーをライン加
から３２！βで内径３５０叫φの円形ダクト内のほぼ中
心に設げた空気を利用した２流体ノズルから空気を約ｓ
Ｎｍ”７Ｈ吸き込みながら排ガス２中に噴霧した。排
ガス２はガス温度が１５０℃で水分７．８ Ｖｏ１＊の
未飽和ガスであり、３２１Ａで噴霧された中和スラ９２
６は蒸発して、排ガス温度は１３５℃〜１２０℃テ水分
＆８〜９．８ Ｖｏ１％ トナ７）。この排ガスを乾式
集じん装置３に導いた後、ガスガスヒータに導いた。こ
の場合の各部の温度は次の通りであった。ガスガスヒー
タ未処理出口排ガス温度は９０℃〜８０℃、冷却塔出口
ガス温度は５０’Ｃ〜４８℃、吸収塔出ロガス温度は５
０℃〜４８℃、及び吸収塔を出てガスガスヒータに導い
たガスのガスガスヒータ出口温度は、９０℃〜８３℃、
また冷却塔補給水は平均１８８Ｊ／Ｈであった。また付
着物堆積防止装置より排出される付着物は平均４ ｋｇ
／Ｈであった。ガスガスヒータを出たガスは、スチーム
ガスヒータにより９５℃にした後、 煙突より大気中に
放出した。Part 3 While stirring and mixing the cleaning liquid 13 of the cooling tower 6 and the gypsum separation F liquid n in the neutralization tank 6, add Ca (OH)2 powder and reduce the H of the neutralized slurry to 7. -12 It was added so that it was 11 on average. The average supply amount of Ca(OH)2 powder is 60
It was 09β. Add neutralized slurry from neutralization tank 6 to line 32! Approximately s
It was sprayed into the exhaust gas 2 while inhaling Nm"7H. The exhaust gas 2 was an unsaturated gas with a gas temperature of 150°C and a moisture content of 7.8 Vo1*, and the neutralized slurry 92 was sprayed at 321A.
6 is evaporated, and the exhaust gas temperature is 135°C to 120°C, moisture & 8 to 9.8 Vo1% Tona 7). This exhaust gas was led to a dry dust collector 3 and then to a gas heater. The temperatures of each part in this case were as follows. Gas gas heater untreated outlet exhaust gas temperature is 90°C to 80°C, cooling tower outlet gas temperature is 50'C to 48°C, absorption tower output log gas temperature is 5.
0°C to 48°C, and the gas gas heater outlet temperature of the gas that exits the absorption tower and is led to the gas gas heater is 90°C to 83°C,
Furthermore, the average amount of cooling tower make-up water was 188 J/H. Also, the average amount of deposits discharged from the deposit accumulation prevention device is 4 kg.
/H. The gas leaving the gas heater was heated to 95°C using a steam gas heater and then released into the atmosphere through the chimney.
本発明の実験例
石炭焚き排ガス４，０００ Ｎｍ”／’Ｈな処理する第
１図の態様のパイロットプラントより本発明を実施した
。排ガス２の性状は第１表と同じである。吸収系排水を
２イン諷を通して１２ ＩＡｌ、 冷却塔に供給した
。液組成は第３表と同じである。Experimental example of the present invention The present invention was carried out using a pilot plant of the embodiment shown in Fig. 1, which treats coal-fired exhaust gas at 4,000 Nm''/'H.The properties of the exhaust gas 2 are the same as in Table 1.Absorption system wastewater 12 IAl was fed to the cooling tower through a 2-inch tube.The liquid composition is the same as in Table 3.
冷却塔６の洗浄液を排ガス４，０００ Ｎｍ”／Ｈに見
合った量８Ｊ／Ｈをライン１３から連続的に中和槽６に
供給し、中和槽５では攪拌混合しながらＣａ （ＯＨ）
２粉末Ｕを加え、中和スラリーの、Ｈを＆Ｏになるよう
に添加した。その時の洗浄液の液性状を第４表に示す。The cleaning liquid from the cooling tower 6 was continuously supplied from the line 13 to the neutralization tank 6 in an amount of 8 J/H corresponding to the exhaust gas of 4,000 Nm"/H, and in the neutralization tank 5, Ca (OH) was added while stirring and mixing.
2 powder U was added, and H of the neutralized slurry was added so that it became &O. Table 4 shows the liquid properties of the cleaning liquid at that time.
以下余白
第 ４ 表 本実施例冷却塔洗浄液の液性状排ガス２の
温度は１５０℃の水分７，３ＶＯ１％の未飽和であり、
Ｉｌｌ／Ｈのスラリーが噴霧された後の排ガス温度は１
４６℃で＆１■■となった。この排ガスを乾式集じん装
置３に導いた後、ガスガスヒータおに導いた。この場合
の各部の温度は下記のとおりであった。Table 4: The temperature of the liquid exhaust gas 2, which is the cooling tower cleaning liquid of this example, is 150°C, and the water content is 7.3 VO 1%, which is unsaturated.
The exhaust gas temperature after the slurry of Ill/H is sprayed is 1
It became &1■■ at 46°C. This exhaust gas was led to a dry dust collector 3 and then to a gas heater. The temperatures of each part in this case were as follows.
ガスガスヒータ未処理出口排ガス温度は９０℃。Gas gas heater untreated outlet exhaust gas temperature is 90°C.
冷却塔出口ガス温度は５０℃、吸収塔出口ガス温度は５
０℃及びガスガスヒータ処理出口排ガス温度は、９５℃
また冷却塔補給水は平均１７６Ｊ／Ｈであった。そして
蒸発装置には付着物は皆きであった。Cooling tower outlet gas temperature is 50℃, absorption tower outlet gas temperature is 50℃.
0℃ and gas gas heater processing outlet exhaust gas temperature is 95℃
Also, the average amount of cooling tower make-up water was 176 J/H. There was no deposit on the evaporator.
ガスガスヒータを出たガスは再加熱を必要とせず９５℃
で煙突より大へ中に放出された。The gas leaving the gas heater does not require reheating and reaches 95℃.
It was ejected into the chimney.
なお９本発明の方法は１石炭焚排ガス処理装置に適用出
来るだけでよく、油焚、イトコーク焚。Note that the method of the present invention can only be applied to one coal-fired exhaust gas treatment device, such as oil-fired or itocoke-fired.
オリノコタール焚等の排ガス処理装置についても適用可
能である。It is also applicable to exhaust gas treatment equipment such as Orinoco tar firing.
本発明の方法によれば次の効果を奏することができる。 According to the method of the present invention, the following effects can be achieved.
（１） 排ガス中に噴霧する液量な調整することによ
り、排ガスの温度低下は小さく、シたがってガスガスヒ
ータでの熱回収だけで煙突入口ガス温度を所定の温度に
保持できるので別途再加熱装置は不要となる。(1) By adjusting the amount of liquid sprayed into the exhaust gas, the temperature drop in the exhaust gas is small. Therefore, the smoke inlet gas temperature can be maintained at a predetermined temperature simply by recovering heat with the gas heater, so a separate reheating device is required. becomes unnecessary.
（２）冷却塔の補給水として吸収系排水が使用できるの
で、系外から供給する補給水を低減できる。(2) Absorption system wastewater can be used as make-up water for the cooling tower, so the amount of make-up water supplied from outside the system can be reduced.
（３）効率よく液滴が蒸発されるため付着物が少なくな
り、付着物堆積防止装置が不要となる。(3) Since the droplets are efficiently evaporated, the amount of deposits is reduced, and a device for preventing deposition of deposits is not required.
（４）ハロゲン濃度及び懸濁物濃度をある濃度レベルに
することにより９機器の腐食、配管の摩耗及び閉塞がな
くなる。(4) By setting the halogen concentration and suspended solids concentration to a certain level, corrosion of 9 equipment, wear and clogging of pipes will be eliminated.
第１図は本発明の１実施例の排ガス処理装置からの排液
処理の工程図、第２図は従来の石炭焚きボイラ排ガスの
排ガス処理装置からの排液処理の１例の工程図である。
１・・・ボイラ、３・・・乾式集じん装置、６・・・冷
却塔。
８・・・吸収塔、１６・・・酸化塔、１９・・・固液分
離器。
ご・・・蒸発装置、２８・・・再加熱装置、３０・・・
煙突。
３１・・・付着物堆積防止装置、３３・・・ガスガスヒ
ータ。
３９・・・濃度検出器、 ４０・・・調節計、４１・・
・調節弁。FIG. 1 is a process diagram of a waste liquid treatment from an exhaust gas treatment device according to an embodiment of the present invention, and FIG. 2 is a process diagram of an example of a waste liquid treatment from a conventional coal-fired boiler exhaust gas treatment device. . 1... Boiler, 3... Dry dust collector, 6... Cooling tower. 8: Absorption tower, 16: Oxidation tower, 19: Solid-liquid separator. .. Evaporation device, 28.. Reheating device, 30..
chimney. 31... Deposit deposition prevention device, 33... Gas gas heater. 39...Concentration detector, 40...Controller, 41...
·Control valve.
Claims (1)
まれているばいじんを除去して湿式排ガス処理装置に送
り前記湿式排ガス処理装置の冷却塔で排ガス中のばいじ
んとハロゲン化合物を捕集するとともに排ガスを冷却し
た後、吸収塔に導き排ガス中の硫黄酸化物を除去する排
ガス処理装置において、吸収系排水を前記吸収塔及び前
記冷却塔に供給し、かつ前記冷却塔の循環液の１部を抜
き出し、前記乾式集じん装置の上流に、排ガス温度の低
下が４℃〜８℃の範囲内に留まるようにボイラ等の負荷
信号または排ガス流量信号により流入量を制御して注入
し蒸発させ、この乾燥固形物を前記乾式集じん装置で捕
集することを特徴とする排ガス処理装置における排液の
処理方法。Exhaust gas from a boiler, etc. is guided to a dry type dust collector to remove the soot and dust contained in the exhaust gas, and then sent to a wet type exhaust gas treatment device where the soot and halogen compounds in the exhaust gas are collected in the cooling tower of the wet type exhaust gas treatment device. In an exhaust gas treatment device that cools the exhaust gas and then leads it to an absorption tower to remove sulfur oxides in the exhaust gas, the absorption system wastewater is supplied to the absorption tower and the cooling tower, and a part of the circulating liquid of the cooling tower is The inflow amount is controlled by the load signal of the boiler or the exhaust gas flow rate signal so that the drop in exhaust gas temperature remains within the range of 4°C to 8°C, and the inflow is injected into the upstream of the dry dust collector and evaporated. A method for treating waste liquid in an exhaust gas treatment device, characterized in that dry solids are collected by the dry dust collector.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62249999A JPH0194920A (en) | 1987-10-05 | 1987-10-05 | Method for treating waste liquid in flue gas treatment apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62249999A JPH0194920A (en) | 1987-10-05 | 1987-10-05 | Method for treating waste liquid in flue gas treatment apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0194920A true JPH0194920A (en) | 1989-04-13 |
Family
ID=17201338
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62249999A Pending JPH0194920A (en) | 1987-10-05 | 1987-10-05 | Method for treating waste liquid in flue gas treatment apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0194920A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100050790A1 (en) * | 2008-08-29 | 2010-03-04 | Horiba, Ltd. | Stack-gas measuring apparatus and stack-gas measuring method |
| WO2012128257A1 (en) * | 2011-03-22 | 2012-09-27 | 三菱重工業株式会社 | Exhaust gas processing system and method, spray-drying device and method for dehydrated filtrate from desulfurization wastewater |
| WO2012128330A1 (en) * | 2011-03-24 | 2012-09-27 | 三菱重工業株式会社 | Spray-drying device for dehydrated filtrate from desulfurization wastewater, exhaust gas treatment system and method |
| CN108607297A (en) * | 2016-12-12 | 2018-10-02 | 河北昊凯环保科技有限公司 | Recycle fluidized bed dry flue gas desulfurization system |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61181519A (en) * | 1985-02-08 | 1986-08-14 | Mitsubishi Heavy Ind Ltd | Treatment of waste liquid in waste gas treating apparatus |
-
1987
- 1987-10-05 JP JP62249999A patent/JPH0194920A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61181519A (en) * | 1985-02-08 | 1986-08-14 | Mitsubishi Heavy Ind Ltd | Treatment of waste liquid in waste gas treating apparatus |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100050790A1 (en) * | 2008-08-29 | 2010-03-04 | Horiba, Ltd. | Stack-gas measuring apparatus and stack-gas measuring method |
| US8276469B2 (en) * | 2008-08-29 | 2012-10-02 | Horiba, Ltd. | Stack-gas measuring apparatus and stack-gas measuring method |
| EP2159564A3 (en) * | 2008-08-29 | 2014-02-26 | Horiba, Ltd. | Stack-gas measuring apparatus and stack-gas measuring method |
| WO2012128257A1 (en) * | 2011-03-22 | 2012-09-27 | 三菱重工業株式会社 | Exhaust gas processing system and method, spray-drying device and method for dehydrated filtrate from desulfurization wastewater |
| US8715402B2 (en) | 2011-03-22 | 2014-05-06 | Mitsubishi Heavy Industries, Ltd. | Air pollution control system and air pollution control method, spray drying device of dewatering filtration fluid from desulfurization discharged water, and method thereof |
| US8883107B2 (en) | 2011-03-22 | 2014-11-11 | Mitsubishi Heavy Industries, Ltd. | Air pollution control system, air pollution control method, spray drying device of dewatering filtration fluid from desulfurization discharged water, and method thereof |
| US9409117B2 (en) | 2011-03-22 | 2016-08-09 | Mitsubishi Hitachi Power Systems, Ltd. | Air pollution control system, air pollution control method, spray drying device of dewatering filtration fluid from desulfurization discharged water, and method thereof |
| WO2012128330A1 (en) * | 2011-03-24 | 2012-09-27 | 三菱重工業株式会社 | Spray-drying device for dehydrated filtrate from desulfurization wastewater, exhaust gas treatment system and method |
| US9555341B2 (en) | 2011-03-24 | 2017-01-31 | Mitsubishi Power Systems, Ltd. | Spray-drying device for dehydrated filtrate from desulfurization wastewater, air pollution control system and flue gas treatment method |
| CN108607297A (en) * | 2016-12-12 | 2018-10-02 | 河北昊凯环保科技有限公司 | Recycle fluidized bed dry flue gas desulfurization system |
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