JPH08155261A - Gas treatment equipment - Google Patents
Gas treatment equipmentInfo
- Publication number
- JPH08155261A JPH08155261A JP6301097A JP30109794A JPH08155261A JP H08155261 A JPH08155261 A JP H08155261A JP 6301097 A JP6301097 A JP 6301097A JP 30109794 A JP30109794 A JP 30109794A JP H08155261 A JPH08155261 A JP H08155261A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- liquid
- water
- desulfurization
- treated
- 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.)
- Granted
Links
- 239000007788 liquid Substances 0.000 claims abstract description 86
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 47
- 230000023556 desulfurization Effects 0.000 claims abstract description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000001816 cooling Methods 0.000 claims abstract description 22
- 238000010521 absorption reaction Methods 0.000 claims abstract description 17
- 238000002485 combustion reaction Methods 0.000 claims abstract description 15
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 14
- 239000011593 sulfur Substances 0.000 claims abstract description 14
- 239000007789 gas Substances 0.000 claims description 124
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 27
- 238000000354 decomposition reaction Methods 0.000 claims description 4
- 230000002528 anti-freeze Effects 0.000 description 21
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 8
- 239000003546 flue gas Substances 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- 239000000428 dust Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 239000000446 fuel Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 description 4
- 239000003638 chemical reducing agent Substances 0.000 description 4
- 230000003009 desulfurizing effect Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000012717 electrostatic precipitator Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- XULSCZPZVQIMFM-IPZQJPLYSA-N odevixibat Chemical compound C12=CC(SC)=C(OCC(=O)N[C@@H](C(=O)N[C@@H](CC)C(O)=O)C=3C=CC(O)=CC=3)C=C2S(=O)(=O)NC(CCCC)(CCCC)CN1C1=CC=CC=C1 XULSCZPZVQIMFM-IPZQJPLYSA-N 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
(57)【要約】
【目的】 脱硫処理の際の補給水を不用にする。
【構成】 燃焼機器１からの排ガス等の被処理ガス中の
硫黄分を吸収除去するガス処理装置において、前記被処
理ガスを吸収液と接触させてガス中の硫黄分を吸収液に
吸収除去させる脱硫塔９を設け、その吸収液を、被処理
ガスと接触した際にガス中の水分が凝縮し得る温度に冷
却する冷却手段１４を設ける。
(57) [Summary] [Purpose] Makes up make-up water unnecessary during desulfurization. In a gas treatment device for absorbing and removing a sulfur content in a gas to be treated such as an exhaust gas from a combustion device 1, the gas to be treated is brought into contact with an absorption liquid to absorb and remove the sulfur content in the gas into the absorption liquid. A desulfurization tower 9 is provided, and a cooling means 14 is provided for cooling the absorbed liquid to a temperature at which water in the gas can condense when brought into contact with the gas to be treated.
Description
【０００１】[0001]
【産業上の利用分野】本発明は燃焼機器からの排ガス等
の被処理ガスを精製処理するガス処理装置に関するもの
である。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gas treatment device for purifying a gas to be treated such as exhaust gas from combustion equipment.
【０００２】[0002]
【従来の技術】燃焼機器例えばボイラから排出されるガ
スは、ガス中に窒素酸化物、粉塵、硫黄酸化物等が含ま
れているため、ガス処理装置により脱硝、脱塵、脱硫な
どの精製処理をした後、大気に開放される。2. Description of the Related Art Gas discharged from combustion equipment, such as a boiler, contains nitrogen oxides, dust, sulfur oxides, etc., and is therefore purified by a gas treatment device such as denitration, dedusting and desulfurization. After that, it is opened to the atmosphere.
【０００３】ガス処理装置は、図４に示すように、脱硝
装置３０，空気予熱器（ＧＡＨ）５，電気集塵機（Ｅ
Ｐ）６，ガスガスヒータ（ＧＧＨ）３１，湿式排煙脱硫
装置３２，ガスガスヒータ（ＧＧＨ）３３等から主に構
成されており、ボイラ１からの排ガスが、例えば選択接
触還元法（ＳＣＲ）を用いた脱硝装置３０で脱硝処理さ
れた後、空気予熱器５において例えば約 370℃から約 1
30〜140 ℃に冷却される。そして、電気集塵機６で脱塵
処理され、さらにガスガスヒータ３１で例えば約90℃に
冷却された後、湿式の排煙脱硫装置３２に導かれてガス
中の硫黄分が吸収液（石灰石スラリ）に吸収除去されて
脱硫処理される。この脱硫処理後のガスがガスガスヒー
タ３３を介して例えば約50℃から約90〜100 ℃に昇温さ
れた後、煙突３から大気に開放される。As shown in FIG. 4, the gas treatment device includes a denitration device 30, an air preheater (GAH) 5, an electrostatic precipitator (E).
P) 6, a gas gas heater (GGH) 31, a wet flue gas desulfurization device 32, a gas gas heater (GGH) 33 and the like, and the exhaust gas from the boiler 1 uses, for example, a selective catalytic reduction method (SCR). After being denitrified by the denitration device 30, the air preheater 5 is, for example, about 370 ° C to about 1
It is cooled to 30-140 ℃. Then, after being dedusted by the electric dust collector 6 and further cooled by the gas gas heater 31 to, for example, about 90 ° C., it is guided to the wet flue gas desulfurization device 32 so that the sulfur content in the gas becomes an absorbing liquid (limestone slurry). It is absorbed and removed and desulfurized. The gas after the desulfurization treatment is heated from, for example, about 50 ° C. to about 90 to 100 ° C. through the gas gas heater 33, and then released from the chimney 3 to the atmosphere.
【０００４】[0004]
【発明が解決しようとする課題】ところで、前述のガス
処理装置に備えられている排煙脱硫装置は、湿式石灰石
−石膏法で脱硫処理を行うものである。すなわち、脱硫
塔内で排ガスと炭酸カルシウム等のカルシウム系の脱硫
剤を含むスラリ状の吸収液とを気液接触させ、ガス中の
硫黄酸化物を脱硫剤（吸収液）に吸収除去させて排ガス
の脱硫処理を行うものである。このため、脱硫塔では、
ガスガスヒータからの例えば約90℃の排ガスが吸収液と
気液接触して約50℃になるため、脱硫塔内での蒸発水分
が多いので、多くの補給水を脱硫塔等に供給しなければ
ならず、補給水の確保が必要になる。By the way, the flue gas desulfurization apparatus provided in the above-mentioned gas treatment apparatus performs desulfurization treatment by the wet limestone-gypsum method. That is, the exhaust gas is brought into gas-liquid contact with a slurry-like absorption liquid containing a calcium-based desulfurization agent such as calcium carbonate in the desulfurization tower, and the sulfur oxides in the gas are absorbed and removed by the desulfurization agent (absorption liquid) to remove the exhaust gas. The desulfurization treatment is performed. Therefore, in the desulfurization tower,
For example, the exhaust gas of about 90 ° C from the gas gas heater comes into contact with the absorbing liquid in a gas-liquid state to reach about 50 ° C, and the amount of water vaporized in the desulfurization tower is large. However, it is necessary to secure makeup water.
【０００５】そこで、本発明は、このような実情に鑑み
なされたものであり、その目的は、ガスの脱硫処理の際
の補給水を不用にすることができるガス処理装置を提供
することにある。Therefore, the present invention has been made in view of such circumstances, and an object of the present invention is to provide a gas treatment device which makes it unnecessary to use make-up water in the desulfurization treatment of gas. .
【０００６】[0006]
【課題を解決するための手段】本発明のガス処理装置
は、前記目的を達成するために、燃焼機器からの排ガス
等の被処理ガス中の硫黄分を吸収除去するガス処理装置
において、前記被処理ガスを吸収液と接触させてガス中
の硫黄分を吸収液に吸収除去させる脱硫塔を設け、その
吸収液を、被処理ガスと接触した際にガス中の水分が凝
縮し得るように冷却する冷却手段を設けたものである
（請求項１）。In order to achieve the above object, the gas treatment apparatus of the present invention is a gas treatment apparatus for absorbing and removing a sulfur content in a gas to be treated such as exhaust gas from a combustion device. A desulfurization tower is provided to bring the treated gas into contact with the absorbing liquid to absorb and remove the sulfur content in the gas into the absorbing liquid, and cool the absorbing liquid so that water in the gas can condense when it comes into contact with the gas to be treated. The cooling means is provided (Claim 1).
【０００７】また、燃焼機器からの排ガスを脱硝・脱硫
処理するガス処理装置において、前記排ガスを吸収液と
接触させてガス中の硫黄分を吸収液に吸収除去させる脱
硫塔を設け、その吸収液をＬＮＧと接触させて被処理ガ
スと接触した際にガス中の水分が凝縮し得るように冷却
する冷却手段を設け、その冷却手段で気化したＬＮＧ
を、窒素酸化物の分解に寄与させるべく前記燃焼機器に
供給するＬＮＧ供給手段を設けたものである（請求項
２）。Further, in a gas treatment device for denitration and desulfurization of exhaust gas from a combustion device, a desulfurization tower is provided for bringing the exhaust gas into contact with an absorption liquid to absorb and remove the sulfur content in the gas into the absorption liquid. Is provided with a LNG, and cooling means is provided for cooling so that water in the gas can be condensed when the LNG is brought into contact with the gas to be treated, and the LNG vaporized by the cooling means.
Is provided to the combustion equipment so as to contribute to the decomposition of nitrogen oxides (claim 2).
【０００８】さらに、前記吸収液は水であることが好ま
しい（請求項３）。Further, the absorbing liquid is preferably water (claim 3).
【０００９】[0009]
【作用】被処理ガス（排ガス）は、脱硫塔で吸収液と接
触してガス中の硫黄分が吸収液に吸収除去され、脱硫処
理される。この際、吸収液が冷却手段により被処理ガス
と接触した際にガス中の水分が凝縮し得る温度に冷却さ
れているため、被処理ガスと吸収液とが接触しても、脱
硫塔内で水分が蒸発することがなく、逆にガス中の水分
が凝縮する。よって、ガスの脱硫処理の際の補給水を不
用にすることが可能となる（請求項１）。In the desulfurization tower, the gas to be treated (exhaust gas) is contacted with the absorbing liquid to remove the sulfur content in the gas by the absorbing liquid and desulfurized. At this time, since the absorbing liquid is cooled by the cooling means to a temperature at which water in the gas can condense when contacting the gas to be treated, even if the gas to be treated and the absorbing liquid come into contact with each other, in the desulfurization tower The water does not evaporate, and the water in the gas condenses. Therefore, it becomes possible to make unnecessary the make-up water for the gas desulfurization treatment (Claim 1).
【００１０】また、吸収液を冷却するのにＬＮＧを用
い、この冷却により気化したＬＮＧを燃焼機器例えばボ
イラに供給することで、燃焼機器内で脱硝処理が行われ
る。すなわち、気化したＬＮＧは主成分が還元物質であ
るメタンであるため、このメタンと窒素酸化物（ＮＯ
ｘ）とが反応してＮＯｘが分解されるので、燃焼機器内
で脱硝処理が行われ、例えば選択接触還元法（ＳＣＲ）
を用いた脱硝装置を別途設ける必要がなくなる（請求項
２）。Further, LNG is used to cool the absorbing liquid, and the LNG vaporized by this cooling is supplied to the combustion equipment, for example, the boiler, so that the denitration treatment is performed in the combustion equipment. That is, since the main component of vaporized LNG is methane, which is a reducing substance, this methane and nitrogen oxides (NO
x) reacts with NOx to decompose, so denitration treatment is performed in the combustion equipment, for example, selective catalytic reduction method (SCR).
It is not necessary to separately provide a denitration device using (Claim 2).
【００１１】さらに、吸収液を冷却して脱硫塔内での脱
硫を低温で行うことにより、吸収液が水でも十分に硫黄
分を吸収することが可能となり、炭酸カルシウム等のカ
ルシウム系などの脱硫剤が不用になる（請求項３）。Further, by cooling the absorbing liquid and performing desulfurization in the desulfurization tower at a low temperature, the absorbing liquid can sufficiently absorb the sulfur content even in water, and desulfurization such as calcium carbonate such as calcium carbonate. The agent becomes unnecessary (claim 3).
【００１２】[0012]
【実施例】以下、本発明の一実施例を添付図面に基づい
て詳述する。An embodiment of the present invention will be described in detail below with reference to the accompanying drawings.
【００１３】図１において、１は燃焼機器としてのボイ
ラを示し、このボイラ１には石炭等の燃料を供給する燃
料供給ライン２が接続されている。In FIG. 1, reference numeral 1 denotes a boiler as a combustion device, and a fuel supply line 2 for supplying a fuel such as coal is connected to the boiler 1.
【００１４】ボイラ１にはボイラ１からの排ガス（被処
理ガス）を煙突３に導く排ガスライン４が接続され、こ
の排ガスライン４には、ガスの流れ方向に沿って、空気
予熱器（ＧＡＨ）５，ガス中のダスト等の粉塵を捕捉す
る電気集塵機（ＥＰ）６，第１ガスガスヒータ（ＧＧ
Ｈ）７，湿式排煙脱硫装置８の脱硫塔９，第２ガスガス
ヒータ（ＧＧＨ）１０が順次介設されている。An exhaust gas line 4 for guiding the exhaust gas (gas to be treated) from the boiler 1 to the chimney 3 is connected to the boiler 1, and an air preheater (GAH) is connected to the exhaust gas line 4 along the gas flow direction. 5, Electrostatic precipitator (EP) for capturing dust such as dust in gas 6, First gas gas heater (GG
H) 7, a desulfurization tower 9 of the wet flue gas desulfurization device 8, and a second gas gas heater (GGH) 10 are sequentially provided.
【００１５】空気予熱器５は、ボイラ１からの高温（例
えば約 370℃）の排ガスとボイラ１に供給される空気と
を間接的に熱交換させて空気を予熱すると共に排ガスを
例えば約 130〜140 ℃に冷却するものである。The air preheater 5 indirectly heat-exchanges the high-temperature (for example, about 370 ° C.) exhaust gas from the boiler 1 with the air supplied to the boiler 1 to preheat the air, and at the same time, the exhaust gas is heated to, for example, about 130- It is cooled to 140 ° C.
【００１６】第１ガスガスヒータ７は、電気集塵機６で
脱塵処理されたガスと熱交換媒体例えば水とを熱交換チ
ューブを介して間接的に熱交換して、 130〜140 ℃の排
ガスを例えば50℃まで冷却し得るように構成する。第２
ガスガスヒータ１０は、排煙脱硫装置８の脱硫塔９を介
した例えば約０℃のガスと第１ガスガスヒータ７からの
熱交換媒体（水）とを熱交換させてガスを例えば約90℃
に昇温するもので、この昇温されたガスが煙突３から大
気に開放される。その熱交換媒体である水は、第１ガス
ガスヒータ７と第２ガスガスヒータ１０との共通の熱交
換媒体であり、第１ガスガスヒータ７では排ガスを冷却
するために、第２ガスガスヒータ１０では排ガスを加熱
するために作用する。The first gas heater 7 indirectly exchanges heat between the gas dedusted by the electrostatic precipitator 6 and a heat exchange medium, such as water, through a heat exchange tube to generate exhaust gas at 130 to 140 ° C., for example. It is configured so that it can be cooled to 50 ° C. Second
The gas gas heater 10 exchanges heat between the gas of about 0 ° C. and the heat exchange medium (water) from the first gas gas heater 7 through the desulfurization tower 9 of the flue gas desulfurization device 8 to heat the gas to about 90 ° C., for example.
The heated gas is released from the chimney 3 to the atmosphere. The heat exchange medium, water, is a common heat exchange medium for the first gas gas heater 7 and the second gas gas heater 10, and the first gas gas heater 7 cools the exhaust gas. Therefore, the second gas gas heater 10 uses the exhaust gas. Acts to heat up.
【００１７】排煙脱硫装置８は、脱硫塔９内で排ガスと
吸収液である水とを気液接触させてガス中の硫黄分を水
に吸収除去させ、ガスの脱硫処理を行うものであり、水
にはエチレングリコール等の不凍液が混入されている。
脱硫塔９の内部下方には吸収液（水）を溜める液溜タン
ク１１が設けられ、この液溜タンク１１には、水を脱硫
塔９内上部のスプレーノズル（図示せず）に移送するた
めの循環ポンプ１２を有する循環ライン１３が接続され
ている。The flue gas desulfurization device 8 performs a gas desulfurization process by bringing the exhaust gas and water as an absorbing liquid into gas-liquid contact in the desulfurization tower 9 to absorb and remove the sulfur content in the gas. , Water contains antifreeze such as ethylene glycol.
A liquid storage tank 11 for storing an absorbing liquid (water) is provided below the inside of the desulfurization tower 9, and the water is transferred to a spray nozzle (not shown) in the upper part of the desulfurization tower 9 in the liquid storage tank 11. A circulation line 13 having a circulation pump 12 of is connected.
【００１８】循環ライン１３の循環ポンプ１２の上流側
には、循環液である吸収液（水）とＬＮＧとを接触させ
て、吸収液を排ガスと接触した際に排ガス中の水分が凝
縮し得る温度（所定の温度）に冷却する冷却手段である
冷却器１４が介設されている。冷却器１４は、吸収液を
ＬＮＧにより所定の温度に冷却できるものならばどのよ
うな構造のものでもよく、間接の熱交換器（例えばシェ
ルアンドチューブ型の熱交換器）でも、図２に示すよう
に、吸収液中にＬＮＧ供給ライン１５からのＬＮＧを噴
出ノズル１６から直接注入して吸収液を直接冷却する熱
交換器でもよい。吸収液を冷却する所定の温度とは、ボ
イラ１からの排ガスは約30℃以下の温度にするとガス中
に含まれる約８％の水分が凝縮するので、排ガスが約30
℃以下の温度にし得る温度であり、例えば−５〜−10℃
である。例えば、冷却器１４をＬＮＧにより吸収液が−
５℃の温度に冷却するようにする。これにより、−５℃
の吸収液がスプレーノズルから噴霧され、この噴霧吸収
液と接触した排ガスは０℃以下まで冷却され、排ガス中
の水分が凝縮する。冷却器１４には、吸収液（循環液）
である水にエチレングリコール等の不凍液を混入する不
凍液供給ライン１７が接続され、この不凍液供給ライン
１７からの不凍液の供給量（濃度）は、水が凍結しない
濃度で、例えば、ボイラからの排ガスを処理する場合に
は数 ppmで十分である。On the upstream side of the circulation pump 12 of the circulation line 13, the absorption liquid (water) which is the circulation liquid is brought into contact with LNG, and when the absorption liquid is brought into contact with the exhaust gas, water in the exhaust gas can be condensed. A cooler 14, which is a cooling means for cooling to a temperature (predetermined temperature), is provided. The cooler 14 may have any structure as long as it can cool the absorbing liquid to a predetermined temperature by LNG, and an indirect heat exchanger (for example, a shell-and-tube heat exchanger) is shown in FIG. As described above, a heat exchanger that directly cools the absorbing liquid by directly injecting LNG from the LNG supply line 15 into the absorbing liquid from the ejection nozzle 16 may be used. The predetermined temperature for cooling the absorbing liquid means that when the exhaust gas from the boiler 1 is brought to a temperature of about 30 ° C or lower, about 8% of water contained in the gas is condensed, so that the exhaust gas is about 30 ° C.
It is a temperature that can be a temperature of ℃ or less, for example -5 to -10 ℃
Is. For example, when the cooler 14 absorbs the absorption liquid by LNG,
Allow to cool to a temperature of 5 ° C. By this, -5 ℃
The absorbing solution is sprayed from the spray nozzle, and the exhaust gas in contact with the spray absorbing solution is cooled to 0 ° C. or lower, and the water content in the exhaust gas is condensed. The cooler 14 has an absorbing liquid (circulating liquid).
The antifreeze liquid supply line 17 for mixing the antifreeze liquid such as ethylene glycol into the water is connected, and the supply amount (concentration) of the antifreeze liquid from the antifreeze liquid supply line 17 is a concentration at which water does not freeze, for example, exhaust gas from a boiler. A few ppm is sufficient for processing.
【００１９】また、循環ライン１３には、図１に示すよ
うに、吸収液の一部を抜き出し排出する排出ライン１８
が接続され、この排出ライン１８から排出される液の量
を排ガス中の水分が凝縮する水分量にすることにより一
定量の吸収液を循環することが可能となる。このように
排出ライン１８から液が排出されるとこの液中に不凍液
が混入され、この不凍液の濃度は例えば数 ppmと薄いの
でこのまま排出してもよく、また排出ライン１８に不凍
液を分離回収する分離系１９を介設し、この分離回収し
た不凍液を冷却器１４に戻すようにしてもよい。すなわ
ち、分離系１９に、分離回収した不凍液を送るポンプ２
０を有する不凍液戻しライン２１を接続し、この不凍液
戻しライン２１を前記不凍液供給ライン１７に接続す
る。また、分離系１９は、不凍液を分離回収できればど
のような構成でもよく、たとえば図３に示すように、液
（Ｈ2 ＳＯ3 ）を蒸気等の加熱源で加熱すると共に、こ
の加熱により液から放散したＳＯ2 をイナートガスや空
気等のキャリアガスにより放散させる加熱器２４と、加
熱器２４からの液（Ｈ2 Ｏ＋不凍液）を導入し、この液
から不凍液のみを濃縮したり、抽出したりして回収する
回収器２５とから構成され、その回収器２５に不凍液戻
しライン２１が接続されて、回収した不凍液が冷却器１
４に戻される。Further, in the circulation line 13, as shown in FIG. 1, a discharge line 18 for extracting a part of the absorbing liquid and discharging it.
Is connected, and the amount of the liquid discharged from the discharge line 18 is set to the amount of water in which the moisture in the exhaust gas is condensed, so that a certain amount of the absorbing liquid can be circulated. When the liquid is discharged from the discharge line 18 in this manner, the antifreeze liquid is mixed into the liquid, and the concentration of the antifreeze liquid is as low as several ppm, so it may be discharged as it is. Also, the antifreeze liquid is separated and collected in the discharge line 18. A separation system 19 may be provided so that the separated antifreeze liquid is returned to the cooler 14. That is, the pump 2 that sends the separated and recovered antifreeze liquid to the separation system 19.
The antifreeze return line 21 having 0 is connected, and the antifreeze return line 21 is connected to the antifreeze supply line 17. Further, the separation system 19 may have any configuration as long as it can separate and collect the antifreeze liquid. For example, as shown in FIG. 3, the liquid (H 2 SO 3 ) is heated by a heating source such as steam, and this heating causes the liquid to be separated from the liquid. A heater 24 that diffuses the emitted SO 2 with a carrier gas such as inert gas or air, and a liquid (H 2 O + antifreeze liquid) from the heater 24 are introduced, and only the antifreeze liquid is concentrated or extracted from this liquid. The antifreeze liquid return line 21 is connected to the recovery device 25, and the recovered antifreeze liquid is collected by the cooler 1.
Returned to 4.
【００２０】その冷却器１４には、吸収液を冷却する際
に気化したＬＮＧが流入する気化ＬＮＧライン２２が接
続されている。この気化ＬＮＧライン２２は、ボイラ１
の上方に接続されてＬＮＧ供給手段２３が構成され、気
化したＬＮＧがボイラ（火炉）１の上方に吹き込まれ
て、ボイラ１の燃料の一部となると共に、窒素酸化物の
分解に寄与する還元剤として作用するようにする。The cooler 14 is connected to a vaporized LNG line 22 into which LNG vaporized when cooling the absorbing liquid flows. This vaporized LNG line 22 is connected to the boiler 1
LNG supply means 23 is configured by being connected to the upper part of the boiler 1, and the vaporized LNG is blown above the boiler (furnace) 1 to become a part of the fuel of the boiler 1 and reduction that contributes to the decomposition of nitrogen oxides. To act as an agent.
【００２１】次に本実施例の作用を述べる。Next, the operation of this embodiment will be described.
【００２２】ボイラ１からの高温例えば約 370℃の排ガ
スは、空気予熱器５で約 130〜140℃に冷却された後、
電気集塵機６で脱塵処理される。そして、第１ガスガス
ヒータ７で例えば約50℃に冷却されてから排煙脱硫装置
８の脱硫塔９に至る。脱硫塔９内の液溜タンク１１内の
吸収液（水）は、循環ポンプ１２により循環ライン１３
を介してスプレーノズルから塔９内に噴霧されて循環す
る。この循環液（吸収液）と排ガスとが気液接触してガ
ス中の硫黄分（硫黄酸化物）が吸収液に吸収除去される
（Ｈ2 Ｏ＋ＳＯ2 →Ｈ2 ＳＯ3 ）。この際、循環する吸
収液は冷却器１４でＬＮＧと接触して例えば−５℃に冷
却されるため、排ガスは吸収液と接触すると０℃以下ま
で冷却される。これにより、硫黄酸化物の低温脱硫が行
われ、吸収液が水でも十分に硫黄酸化物を吸収除去する
ことができる。このため、硫黄分を吸収するための高価
な脱硫剤、例えば炭酸カルシウム等のカルシウム系の脱
硫剤が不用になる。Exhaust gas at a high temperature, for example, about 370 ° C. from the boiler 1 is cooled to about 130 to 140 ° C. by the air preheater 5,
The dust collector 6 removes dust. Then, after being cooled to about 50 ° C. by the first gas heater 7, it reaches the desulfurization tower 9 of the flue gas desulfurization device 8. The absorption liquid (water) in the liquid storage tank 11 in the desulfurization tower 9 is circulated by the circulation pump 12 in the circulation line 13
Is sprayed from the spray nozzle into the tower 9 and circulates. The circulating liquid (absorption liquid) and the exhaust gas come into gas-liquid contact, and the sulfur content (sulfur oxide) in the gas is absorbed and removed by the absorption liquid (H 2 O + SO 2 → H 2 SO 3 ). At this time, since the circulating absorption liquid contacts the LNG in the cooler 14 and is cooled to, for example, −5 ° C., the exhaust gas is cooled to 0 ° C. or lower when it contacts the absorption liquid. As a result, low-temperature desulfurization of the sulfur oxide is performed, and the sulfur oxide can be sufficiently absorbed and removed even if the absorbing liquid is water. Therefore, an expensive desulfurizing agent for absorbing the sulfur content, for example, a calcium-based desulfurizing agent such as calcium carbonate becomes unnecessary.
【００２３】また、排ガスは吸収液によりガス中の水分
が凝縮し得る温度（30℃以下の温度）に冷却されるた
め、ガス中に含まれる水分（排ガス中には約８％の水分
が含まれている）の一部が凝縮する。このように、脱硫
塔９内ではガスと吸収液とが気液接触しても水分が蒸発
することなく、逆にガス中の水分が凝縮するので、脱硫
の際の補給水を不用にすることができる。Further, since the exhaust gas is cooled by the absorbing liquid to a temperature at which water in the gas can be condensed (a temperature of 30 ° C. or lower), the water contained in the gas (exhaust gas contains about 8% of water). Part of) is condensed. In this way, in the desulfurization tower 9, even if the gas and the absorbing liquid come into gas-liquid contact with each other, the water does not evaporate, and the water in the gas condenses, so that make-up water for desulfurization is unnecessary. You can
【００２４】脱硫処理後のガスは、第２ガスガスヒータ
１０で第１ガスガスヒータ７からの熱交換媒体（水）に
より例えば約０℃から約90〜100 ℃に昇温された後、煙
突３から大気に開放される。この際、ガス温度が約90〜
100 ℃であるので白煙が抑制される。The gas after desulfurization is heated from the temperature of about 0 ° C. to about 90 to 100 ° C. by the second gas heater 10 by the heat exchange medium (water) from the first gas heater 7, and then the gas is discharged from the stack 3. Open to the atmosphere. At this time, the gas temperature is about 90 ~
Since it is 100 ℃, white smoke is suppressed.
【００２５】脱硫処理後の吸収液は排出ライン１８によ
り排出されて他の系で処理される。なお、排出ライン１
８に分離系１９が介設されると、排出される液中の不凍
液が回収され、これが不凍液戻しライン２１を介して冷
却器１４に戻される。The desulfurized absorption liquid is discharged through the discharge line 18 and processed in another system. The discharge line 1
When the separation system 19 is installed in the column 8, the antifreeze liquid in the discharged liquid is collected and returned to the cooler 14 via the antifreeze liquid return line 21.
【００２６】冷却器１４では吸収液と接触したＬＮＧが
気化し、この気化したＬＮＧ（気化ＬＮＧ）が気化ＬＮ
Ｇライン２２に流入して、そしてボイラ（火炉）１の上
方に吹き込まれる。これにより、気化ＬＮＧは、ボイラ
１の燃料の一部となると共に、窒素酸化物の分解に寄与
する還元剤として作用する。すなわち、気化したＬＮＧ
は主成分が還元物質であるメタンであるため、このメタ
ンと窒素酸化物（ＮＯｘ）とが反応してＮＯｘが分解
（ＣＨ4 ＋４ＮＯ→２Ｎ2 ＋ＣＯ2 ＋２Ｈ2 Ｏ）される
ので、ボイラ１内で脱硝処理が行われる。これにより、
例えば選択接触還元法（ＳＣＲ）を用いた高価な触媒を
必要とする脱硝装置を別途設ける必要がなくなる。In the cooler 14, LNG in contact with the absorbing liquid is vaporized, and this vaporized LNG (vaporized LNG) is vaporized LN.
It flows into the G line 22 and is blown above the boiler (furnace) 1. As a result, the vaporized LNG becomes a part of the fuel of the boiler 1 and acts as a reducing agent that contributes to the decomposition of nitrogen oxides. That is, vaporized LNG
Since the main component is methane which is a reducing substance, this methane reacts with nitrogen oxides (NOx) to decompose NOx (CH 4 + 4NO → 2N 2 + CO 2 + 2H 2 O). Denitration process is performed. This allows
For example, it is not necessary to separately provide a denitration device that requires an expensive catalyst using the selective catalytic reduction method (SCR).
【００２７】従って、脱硫剤が不用になると共に、湿式
排煙脱硫装置８への補給水が不用になる。また、冷却に
使用したＬＮＧをボイラ１の燃料の一部として使用でき
ると共に、脱硝用の還元剤としても使用でき、脱硝装置
が不用になる。Therefore, the desulfurizing agent becomes unnecessary, and the makeup water for the wet flue gas desulfurization device 8 becomes unnecessary. Further, the LNG used for cooling can be used as a part of the fuel of the boiler 1 and also as a reducing agent for denitration, which makes the denitration device unnecessary.
【００２８】[0028]
【発明の効果】以上要するに本発明によれば、次のよう
な優れた効果を奏する。In summary, the present invention has the following excellent effects.
【００２９】(1) 請求項１の構成によれば、脱硫処理の
際の補給水を不用にできる。(1) According to the configuration of claim 1, make-up water for the desulfurization treatment can be dispensed with.
【００３０】(2) 請求項２の構成によれば、脱硫処理の
際の補給水を不用にできると共に燃焼機器内で脱硝処理
が行える。(2) According to the configuration of claim 2, make-up water for desulfurization can be dispensed with and denitration can be performed in the combustion equipment.
【００３１】(3) 請求項３の構成によれば、脱硫剤を不
用にできる。(3) According to the structure of claim 3, the desulfurizing agent can be dispensed with.
【図１】本発明の一実施例を示す構成図である。FIG. 1 is a configuration diagram showing an embodiment of the present invention.
【図２】本発明の冷却手段の一例を示す構成図である。FIG. 2 is a configuration diagram showing an example of a cooling unit of the present invention.
【図３】本発明の不凍液を分離回収する分離系の一例を
示す構成図である。FIG. 3 is a configuration diagram showing an example of a separation system for separating and recovering an antifreeze solution of the present invention.
【図４】従来のガス処理装置の一例を示す構成図であ
る。FIG. 4 is a configuration diagram showing an example of a conventional gas treatment device.
１ ボイラ（燃焼機器） ９ 脱硫塔 １４ 冷却器（冷却手段） 1 Boiler (combustion equipment) 9 Desulfurization tower 14 Cooler (cooling means)
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０１Ｄ 53/34 ＺＡＢ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Office reference number FI technical display location B01D 53/34 ZAB
Claims (3)
の硫黄分を吸収除去するガス処理装置において、前記被
処理ガスを吸収液と接触させてガス中の硫黄分を吸収液
に吸収除去させる脱硫塔を設け、その吸収液を、被処理
ガスと接触した際にガス中の水分が凝縮し得るように冷
却する冷却手段を設けたことを特徴とするガス処理装
置。1. A gas treatment device for absorbing and removing sulfur in a gas to be treated such as exhaust gas from a combustion device by bringing the gas to be treated into contact with an absorbing liquid to remove the sulfur in the gas to the absorbing liquid. A gas treatment apparatus comprising: a desulfurization tower for cooling the absorbing liquid; and cooling means for cooling the absorbed liquid so that water in the gas can be condensed when coming into contact with the gas to be treated.
するガス処理装置において、前記排ガスを吸収液と接触
させてガス中の硫黄分を吸収液に吸収除去させる脱硫塔
を設け、その吸収液をＬＮＧと接触させて被処理ガスと
接触した際にガス中の水分が凝縮し得るように冷却する
冷却手段を設け、その冷却手段で気化したＬＮＧを、窒
素酸化物の分解に寄与させるべく前記燃焼機器に供給す
るＬＮＧ供給手段を設けたことを特徴とするガス処理装
置。2. A gas treatment apparatus for denitration / desulfurization of exhaust gas from a combustion device, wherein a desulfurization tower is provided for bringing the exhaust gas into contact with an absorption liquid to absorb and remove the sulfur content in the gas into the absorption liquid. Is provided with LNG, and a cooling means is provided for cooling so as to condense water in the gas when it comes into contact with the gas to be treated, and LNG vaporized by the cooling means is contributed to the decomposition of nitrogen oxides. A gas treatment device comprising LNG supply means for supplying to a combustion device.
載のガス処理装置。3. The gas treatment device according to claim 1, wherein the absorbing liquid is water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30109794A JP3777623B2 (en) | 1994-12-05 | 1994-12-05 | Gas processing equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30109794A JP3777623B2 (en) | 1994-12-05 | 1994-12-05 | Gas processing equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08155261A true JPH08155261A (en) | 1996-06-18 |
| JP3777623B2 JP3777623B2 (en) | 2006-05-24 |
Family
ID=17892823
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP30109794A Expired - Fee Related JP3777623B2 (en) | 1994-12-05 | 1994-12-05 | Gas processing equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3777623B2 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008126154A (en) * | 2006-11-21 | 2008-06-05 | Mitsubishi Heavy Ind Ltd | Treatment method and treatment apparatus of exhaust gas |
| CN101596398B (en) | 2009-05-08 | 2012-05-23 | 朱学智 | Re-devulcanization method based on circulating fluidized bed boiler flue |
| CN107174921A (en) * | 2017-07-26 | 2017-09-19 | 江苏苏高流体机械有限公司 | One kind is used for desulfuration in furnace device |
| CN110639348A (en) * | 2018-06-26 | 2020-01-03 | 北京万信同和能源科技有限公司 | Colored smoke plume processing equipment and method |
| CN111425877A (en) * | 2020-04-22 | 2020-07-17 | 大唐环境产业集团股份有限公司 | Coal-fired power plant waste heat and water recovery system and method |
| CN115301062A (en) * | 2022-09-13 | 2022-11-08 | 重庆市渝江机械设备有限公司 | Desulfurization treatment system with pretreatment structure |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106474860A (en) * | 2015-08-25 | 2017-03-08 | 贺方昀 | Wet desulfurization flue gas processing system and processing method |
| CN216557146U (en) * | 2021-09-28 | 2022-05-17 | 中国华能集团清洁能源技术研究院有限公司 | Low-temperature flue gas desulfurization and denitrification system of rotary kiln combustion furnace of garbage power plant |
-
1994
- 1994-12-05 JP JP30109794A patent/JP3777623B2/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008126154A (en) * | 2006-11-21 | 2008-06-05 | Mitsubishi Heavy Ind Ltd | Treatment method and treatment apparatus of exhaust gas |
| CN101596398B (en) | 2009-05-08 | 2012-05-23 | 朱学智 | Re-devulcanization method based on circulating fluidized bed boiler flue |
| CN107174921A (en) * | 2017-07-26 | 2017-09-19 | 江苏苏高流体机械有限公司 | One kind is used for desulfuration in furnace device |
| CN110639348A (en) * | 2018-06-26 | 2020-01-03 | 北京万信同和能源科技有限公司 | Colored smoke plume processing equipment and method |
| CN111425877A (en) * | 2020-04-22 | 2020-07-17 | 大唐环境产业集团股份有限公司 | Coal-fired power plant waste heat and water recovery system and method |
| CN115301062A (en) * | 2022-09-13 | 2022-11-08 | 重庆市渝江机械设备有限公司 | Desulfurization treatment system with pretreatment structure |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3777623B2 (en) | 2006-05-24 |
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