JPH0326351A - Equipment and method for electrostatic flocculation - Google Patents
Equipment and method for electrostatic flocculationInfo
- Publication number
- JPH0326351A JPH0326351A JP1156682A JP15668289A JPH0326351A JP H0326351 A JPH0326351 A JP H0326351A JP 1156682 A JP1156682 A JP 1156682A JP 15668289 A JP15668289 A JP 15668289A JP H0326351 A JPH0326351 A JP H0326351A
- Authority
- JP
- Japan
- Prior art keywords
- dust
- aggregation
- electrostatic
- flue
- discharge electrode
- 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
- 238000005189 flocculation Methods 0.000 title claims abstract 3
- 230000016615 flocculation Effects 0.000 title claims abstract 3
- 238000000034 method Methods 0.000 title description 10
- 239000000428 dust Substances 0.000 claims abstract description 94
- 239000004071 soot Substances 0.000 claims abstract description 32
- 230000002776 aggregation Effects 0.000 claims description 66
- 238000004220 aggregation Methods 0.000 claims description 54
- 230000015271 coagulation Effects 0.000 claims description 18
- 238000005345 coagulation Methods 0.000 claims description 18
- 238000005054 agglomeration Methods 0.000 claims description 12
- 230000005684 electric field Effects 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 5
- 230000002195 synergetic effect Effects 0.000 claims description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 48
- 239000003546 flue gas Substances 0.000 abstract description 48
- 239000007789 gas Substances 0.000 abstract description 29
- 239000000295 fuel oil Substances 0.000 abstract description 13
- 238000001816 cooling Methods 0.000 abstract description 7
- 238000010521 absorption reaction Methods 0.000 abstract description 3
- 230000003311 flocculating effect Effects 0.000 abstract description 2
- 238000010304 firing Methods 0.000 abstract 1
- 238000006477 desulfuration reaction Methods 0.000 description 36
- 230000023556 desulfurization Effects 0.000 description 36
- 239000002245 particle Substances 0.000 description 26
- 230000000694 effects Effects 0.000 description 14
- 238000010586 diagram Methods 0.000 description 12
- 238000009833 condensation Methods 0.000 description 8
- 230000005494 condensation Effects 0.000 description 8
- 239000000446 fuel Substances 0.000 description 7
- 238000002485 combustion reaction Methods 0.000 description 6
- 230000033228 biological regulation Effects 0.000 description 5
- 238000009826 distribution Methods 0.000 description 5
- 239000012212 insulator Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 239000012718 dry electrostatic precipitator Substances 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 239000012719 wet electrostatic precipitator Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- RSWGJHLUYNHPMX-UHFFFAOYSA-N Abietic-Saeure Natural products C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- KHPCPRHQVVSZAH-HUOMCSJISA-N Rosin Natural products O(C/C=C/c1ccccc1)[C@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 KHPCPRHQVVSZAH-HUOMCSJISA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000009297 electrocoagulation Methods 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01R—MEASURING ELECTRIC VARIABLES; MEASURING MAGNETIC VARIABLES
- G01R31/00—Arrangements for testing electric properties; Arrangements for locating electric faults; Arrangements for electrical testing characterised by what is being tested not provided for elsewhere
- G01R31/50—Testing of electric apparatus, lines, cables or components for short-circuits, continuity, leakage current or incorrect line connections
- G01R31/54—Testing for continuity
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01R—MEASURING ELECTRIC VARIABLES; MEASURING MAGNETIC VARIABLES
- G01R31/00—Arrangements for testing electric properties; Arrangements for locating electric faults; Arrangements for electrical testing characterised by what is being tested not provided for elsewhere
- G01R31/50—Testing of electric apparatus, lines, cables or components for short-circuits, continuity, leakage current or incorrect line connections
- G01R31/52—Testing for short-circuits, leakage current or ground faults
Landscapes
- Physics & Mathematics (AREA)
- General Physics & Mathematics (AREA)
- Treating Waste Gases (AREA)
- Electrostatic Separation (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、重油専焼ボイラ（以下、重専ボイラという）
の排ガス処理用の排煙脱硫装置のばいじん等のダストの
除じん効率向上用として適用される静電凝集装置に関す
る。[Detailed Description of the Invention] [Industrial Field of Application] The present invention is directed to a heavy oil boiler (hereinafter referred to as a heavy oil boiler).
The present invention relates to an electrostatic coagulation device that is applied to improve the efficiency of removing dust such as soot and dust in a flue gas desulfurization device for exhaust gas treatment.
重専ボイラ・プラントにおいて、その排ガス中に含まれ
るばいじん，ＮＯＸ．ＳＯＸ等の大気への放出量を規制
値内におさめるために、脱硝装置，乾式電気集じん装置
．バグフィルタ，排煙脱硫装置，湿式電気集じん装置等
あるいはその一部を組み合せた排煙処理設備が設置され
る。上記の装置のうち、何を組み合せるかは、使用する
燃料である重油の性状，ボイラの運用方法、およびそれ
らに起因して変化するボイラ出口におけるばいじん，Ｎ
Ｏｘ ，ＳＯｘの排出量によって異なる。In heavy boiler plants, soot and NOx contained in the exhaust gas. In order to keep the amount of SOX and other substances released into the atmosphere within the regulated values, denitrification equipment and dry electrostatic precipitators are installed. Flue gas treatment equipment will be installed, including bag filters, flue gas desulfurization equipment, wet electrostatic precipitators, etc., or a combination thereof. Which of the above devices should be combined depends on the properties of the heavy oil used as fuel, the boiler operating method, and the amount of soot and nitrogen at the boiler outlet that change due to these factors.
It varies depending on the amount of Ox and SOx discharged.
重専ボイラ用の排煙処理設備としてどのような装置を組
み合せるかは、各プラントに固有の事情に応じて異るが
、一般産業用の重専ボイラで、ごく通常の性状の重油を
燃料として使用する場合には、次の様な理由から、排煙
脱硫装置のみを設置する場合が多い。こ・の場合の排煙
処理設備の全体系統図の１例を第６図に示す。The type of equipment to be combined as flue gas treatment equipment for a heavy-duty boiler depends on the unique circumstances of each plant, but a heavy-duty boiler for general industry uses heavy oil with normal properties as fuel. When used as a gas turbine, only a flue gas desulfurization device is often installed for the following reasons. An example of the overall system diagram of the flue gas treatment equipment in this case is shown in Figure 6.
《１》 脱硝装置は一般に高価な設備となる為、ボイ
ラの燃焼条件の調整（例えば燃焼時の０２を絞ること等
）によってＮＯｘの低減を図り、この方法によって規制
値以下のＮＯｘ濃度が達成できることが多い。この場合
には、特に脱硝装置を設置する必要がない。《1》 Since denitrification equipment is generally an expensive piece of equipment, it is possible to reduce NOx by adjusting the combustion conditions of the boiler (for example, by throttling the 02 during combustion), and by this method it is possible to achieve a NOx concentration below the regulation value. There are many. In this case, there is no need to particularly install a denitrification device.
（２） ＳＯｘ濃度を規制値以下に維持させるため一
般に湿式排煙脱硫装置を設置する場合が多いが、排煙脱
硫装置自体にばいじんの捕集・除じん機能が兼ね備えら
れており、例えばボイラ出口のばいじん濃度が２５０■
／Ｉ′１１′Ｎ程度以下であれば、排煙脱硫装置出口で
のばいじん濃度を５０■／ｎｉ’Ｎ程度にまで低下させ
ることが可能である。そのため排煙脱硫装置のみで十分
規制値以下のＳＯＸ及びばいじん濃度が達成できること
が多い。従ってこの場合には、煙突からの可視煙の排出
さえ問題にしなければ、特にばいじん捕集装置として乾
式ならびに湿式の電気集じん装置やバグフィルタを設置
する必要がない。(2) Wet flue gas desulfurization equipment is generally installed in order to maintain the SOx concentration below the regulatory value, but the flue gas desulfurization equipment itself also has dust collection and dust removal functions, for example, at the boiler outlet. Dust concentration is 250■
/I'11'N or less, it is possible to reduce the soot and dust concentration at the outlet of the flue gas desulfurization device to about 50/ni'N. Therefore, it is often possible to achieve SOX and soot concentrations well below the regulatory values using only flue gas desulfurization equipment. Therefore, in this case, unless visible smoke emissions from the chimney are a problem, there is no need to install dry or wet electrostatic precipitators or bag filters as particulate collection devices.
しかしながら、排煙処理設備として排煙脱硫装置のみを
設置しているプラントにおいて、排出ＮＯｘ濃度を規制
値以下に維持するためには、通常時にも増してボイラ燃
焼時の０２量を絞る等の燃焼調整が必要となる。しかし
、ボイラ燃焼時の０２量を絞ると一般に発生ばいじん量
が増加し、しかもその増加するばいじんは、いわゆる「
気相析出型」と呼ばれる粒径の非常に小さいサブミクロ
ン（１μ以下）のカーボン・スートが多い。こうしたサ
ブミクロン粒子は、排煙脱硫装置では比較的捕集されに
くいこと及び、発生ばいじんの絶対量が増加することの
ために排煙脱硫装置出口でのばいじん濃度を規制値以下
とすることが極めて困難となる場合がある。こうした事
態に対する対策としては、従来下記の方法が採用されて
いる。However, in plants where only flue gas desulfurization equipment is installed as flue gas treatment equipment, in order to maintain the exhaust NOx concentration below the regulation value, it is necessary to reduce the amount of 02 during boiler combustion even more than usual. Adjustments will be required. However, reducing the amount of 02 during boiler combustion generally increases the amount of soot and dust generated, and the increased soot and dust is
There are many carbon soots with very small particle sizes, submicron (1μ or less), which are called "vapor phase precipitation type". These submicron particles are relatively difficult to collect in flue gas desulfurization equipment, and the absolute amount of generated dust increases, so it is extremely difficult to keep the soot and dust concentration at the flue gas desulfurization equipment outlet below the regulatory value. It can be difficult. Conventionally, the following methods have been adopted as countermeasures against such situations.
（１）脱硝装置を設置（追置）する。(1) Install (additional) a denitrification device.
（２）乾式または湿式電気集じん装置やバグフィルタ等
のばいじん捕集装置を設置（追設）する。(2) Install (add) a dry or wet electrostatic precipitator, bag filter, or other dust collection device.
上記（１） （２）の対策は、いずれも非常に高価であ
り、例えば常時、通常の良い品質の重油を使用し、燃料
事情等によってやむを得ないときのみ一時的に低品質な
重油を使用する様な重専ボイラプラントでは、上記（１
） （２）の方法を採った場合、良い品質の重油を使用
している時（常時）においては過剰設備となってしまう
。また、既設プラントにおいて、これまで良質な重油を
使用してきたが、燃料事情等によって低品質な重油に燃
料転換が必要とされ５
る場合に、上記（１） （２）の方法を採りたくても、
既設プラントへの装置追設のスペース不足等により、不
可能な場合もある。Measures (1) and (2) above are both very expensive; for example, use normal high-quality heavy oil all the time, and temporarily use low-quality heavy oil only when it is unavoidable due to fuel circumstances. In heavy-duty boiler plants such as
) If method (2) is adopted, there will be excess equipment when good quality heavy oil is used (at all times). In addition, in the case where an existing plant has been using high-quality heavy oil until now, but it becomes necessary to switch to lower-quality heavy oil due to fuel circumstances, etc., we would like to adopt methods (1) and (2) above. too,
In some cases, this may not be possible due to lack of space to add equipment to an existing plant.
燃料重油品質の低下による発生ばいじんの増加量は、条
件によっても異るが、ボイラ出口でのばいじん濃度が３
５０■／ｒｒｌ’Ｎ程度にｊ曽加することが多いので、
排煙脱硫装置出口でばいじん濃度が８ ０ ＋ｎｇ ／
ｒｎ’ Ｎ 〜１ ０ ０ ｍｇ ／ ｒｒ？ Ｎ程
度になる場合が多い。従って上記（１） （２）の様な
高コストな対策を採ることなく、コンパクトかつ安価な
装置により、排煙脱硫装置でのばいじんの除じん効率を
高め、８０〜１００■／ｒｒ？Ｎの排煙脱硫装置出口ぽ
いじん量を規制値（５０■／ｒｒ？Ｎが採用されること
が多い）以下に減少させることが強く望まれている。The amount of increase in soot and dust due to deterioration in the quality of fuel oil varies depending on the conditions, but if the soot and dust concentration at the boiler outlet is 3.
Since it is often added to about 50■/rrl'N,
The soot and dust concentration at the exit of the flue gas desulfurization equipment is 80 + ng/
rn' N ~100 mg/rr? In many cases, it is around N. Therefore, without taking the high-cost measures mentioned in (1) and (2) above, the dust removal efficiency of the flue gas desulfurization equipment can be increased by using a compact and inexpensive device, and the dust removal efficiency can be increased to 80 to 100 μ/rr. It is strongly desired to reduce the amount of N dust at the exit of the flue gas desulfurization equipment to below the regulation value (50/rr?N is often adopted).
排煙脱硫装置におけるばいじん等ダストの捕集効率は、
一般に粒径が大きいほど高く、粒径の小さいもの、例え
ば１μ以下のサブミクロン粒子に対しては捕集効率が低
いことが知られている。The collection efficiency of soot and other dust in flue gas desulfurization equipment is
It is generally known that the larger the particle size, the higher the collection efficiency, and that the collection efficiency is lower for small particle sizes, for example, submicron particles of 1 μm or less.
従って、前述のように主としてサブミクロンの６
粒径の粒子が増加したことによりばいじん量の絶対値が
増加した状態に対して排煙脱硫装置のばいじん捕集効率
を向上させるためには、排煙脱硫装置の上流側で、ばい
じんを凝集・粗大化して、排煙脱硫装置に流入するばい
じんの粒径を大きくするという手段が非常に有効である
。Therefore, as mentioned above, in order to improve the dust collection efficiency of the flue gas desulfurization equipment in the situation where the absolute value of the amount of dust has increased due to the increase in the number of submicron particles, it is necessary to A very effective method is to agglomerate and coarsen the soot and dust on the upstream side of the desulfurization equipment to increase the particle size of the soot and dust that flows into the flue gas desulfurization equipment.
ばいじん等のダストを効果的に凝集・粗大化させる方法
の１つとして、静電凝集法がある。静電凝集法はさらに
次の２種類に大別される。Electrostatic coagulation is one of the methods for effectively coagulating and coarsening dust such as soot and dust. The electrostatic coagulation method is further divided into the following two types.
（１）ばいじん粒子が高電界かつコロナ電流の場を通過
する際に、電荷を帯び、かつ粒子表面上の電荷が分極さ
れ、粒子同志がクーロン力により吸引しあって凝集する
（いわゆる空間凝集と呼ばれる）方法。(1) When dust particles pass through a high electric field and corona current field, they become charged, and the charges on the particle surface are polarized, causing the particles to attract each other and aggregate due to Coulomb force (so-called spatial aggregation). called) method.
（２）電荷を帯びたばいじん粒子が、高電界場から受け
るクーロン力により、放電極に対向するアース側電極上
に移動し、同電極上において複数の粒子が互いの静電力
に加えて物理的もしくは化学的に凝集する（いわゆる電
極凝集と呼ばれる）方法。(2) Charged dust particles move onto the ground side electrode facing the discharge electrode due to the Coulomb force received from the high electric field, and multiple particles on the same electrode are physically Or a method of chemical aggregation (so-called electrode aggregation).
こうした静電凝集効果を利用して、ばいじん等のダスト
を凝集・粗大化させようという試みは従来にもいくつか
見られるが次の様な問題点を有していた。There have been several attempts to use such electrostatic aggregation effects to aggregate and coarsen dust such as soot and dust, but these have had the following problems.
（１）空間凝集効果を最大限に利用するため、凝集空間
におけるばいじん等のダストの滞留時間をなるべく長く
とり、凝集空間におけるガス流速を低速に設定すると、
いわゆる「電気集じん装置」と同様の原理により、アー
ス側電極をいわゆる「集じん電極」としてダストが付着
・堆積し、そのまま放置すると荷電障害等の原因となり
、有効な静電凝集効果が得られない。(1) In order to maximize the spatial aggregation effect, the residence time of dust such as soot and dust in the aggregation space is set as long as possible, and the gas flow velocity in the aggregation space is set to a low speed.
Based on the same principle as a so-called "electrostatic precipitator", dust adheres and accumulates on the ground side electrode as a so-called "dust-collecting electrode", and if left as is, it may cause charging problems, and an effective electrostatic coagulation effect cannot be obtained. do not have.
（２） （１）項記載の理由から、凝集空間における
ばいじん等のダストの滞留時間を長くとるということは
、凝集空間の大型化を意味するので、凝集装置そのもの
が大きなものとなり、コンパクト化、コストダウンの主
旨に反する。(2) For the reasons stated in (1), increasing the residence time of soot and other dust in the aggregation space means increasing the size of the aggregation space, which means that the aggregation device itself becomes larger, making it more compact and more compact. This goes against the purpose of reducing costs.
（３） （１）項に記載の様に、電極上にダストが堆
積する場合、これを除去する手段、例えば槌打装置や水
洗装置等が必要とされるが、このような新たな付加装置
が必要とされるのみならず、凝集装置本体の耐震性・防
食性等も考慮した材質向上の必要もあるので、全体とし
て非常に大きなコストアップになる。(3) As described in item (1), when dust accumulates on the electrode, a means to remove it, such as a hammering device or a water washing device, is required. Not only is this necessary, but it is also necessary to improve the material quality of the main body of the flocculating device, taking into account earthquake resistance, anti-corrosion, etc., resulting in a very large increase in cost overall.
（４）凝集させる粒子の種類，状態，雰囲気，温度によ
り粘着性や水分や油分の含有率が高いため、やはりアー
ス側電極への付着・堆積が著しくなり、（１）及び（３
）項の問題点がさらに激しいものとなる。(4) Depending on the type, condition, atmosphere, and temperature of the particles to be aggregated, the adhesiveness and content of moisture and oil may be high, resulting in significant adhesion and accumulation on the earth side electrode, and (1) and (3)
) The problems in section ) become even more severe.
本発明は、上記（１）〜（４）の問題点を解決したコン
バクトでかつ安価な静電凝集装置を提供することを目的
とする。An object of the present invention is to provide a compact and inexpensive electrostatic coagulation device that solves the problems (1) to (4) above.
本発明に係る静電凝集装置は、
（１）放電極（１）と凝集板（２）からなる荷電部を有
する静電凝集装置（１２）において、前記放電極（１）
は細線ワイヤあるいは複数のとげ状の突起ないしシャー
プエッジ状の棒状の高電流型放電極とし、
前記放電極（１）と凝集板（２）を電気的に絶縁すると
ともに、放電極（１）の表面と凝集板９
（２）の表面の最短間隔を８０ｃｍ以下のナロウスペー
シングとし、放電極（１）と凝集板（２）の間には高電
界で高コロナ放電電流の凝集空間を実現させる高圧電源
（１８）を接続し、排煙脱硫装置の冷却塔（１３）の上
流側の入口煙道（９）内のガス温度が１００℃以上、ガ
ス流速が１０ｍ／ｓ以上の領域に組込み、前記凝集空間
において生ずる空間凝集および前記凝集板状において生
ずる電極凝集の相乗効果により、重専ボイラから排出さ
れるばい塵等のダストの凝集粗大化を行なうことを特徴
とする。The electrostatic agglomeration device according to the present invention includes: (1) In an electrostatic aggregation device (12) having a charging section consisting of a discharge electrode (1) and an aggregation plate (2), the discharge electrode (1)
is a high current discharge electrode in the form of a thin wire or a bar with multiple barbed protrusions or sharp edges, which electrically insulates the discharge electrode (1) and the aggregation plate (2), and The shortest distance between the surface and the surface of the aggregation plate 9 (2) is a narrow spacing of 80 cm or less, and a condensation space with a high electric field and high corona discharge current is realized between the discharge electrode (1) and the aggregation plate (2). Connect a high voltage power supply (18) and install it in an area where the gas temperature in the inlet flue (9) on the upstream side of the cooling tower (13) of the flue gas desulfurization device is 100 ° C. or more and the gas flow velocity is 10 m/s or more, The present invention is characterized in that the synergistic effect of the spatial aggregation occurring in the aggregation space and the electrode aggregation occurring in the aggregation plate shape causes the aggregation and coarsening of dust such as soot and dust discharged from the heavy boiler.
（２）前記（１）記載の静電凝集装置において、重専ボ
イラから排出されるばいじんの低電気抵抗率と、ガス温
度が１００℃以上の高温であることと、ガス流速が１０
ｍ／ｓ以上の高速流であることにより、放電極および凝
集板上へのばいじん等の付着を防止し、定常的な電極の
槌打および洗浄するための装置のいずれかを省略するこ
とを特徴とする。(2) In the electrostatic coagulation device described in (1) above, the soot and dust discharged from the heavy boiler has a low electrical resistivity, the gas temperature is high at 100°C or higher, and the gas flow rate is 10°C.
The high-speed flow of m/s or more prevents the adhesion of soot and dust onto the discharge electrode and aggregation plate, and eliminates the need for regular electrode hammering or cleaning equipment. shall be.
（３）すなわち、本発明装置は、放電極およびアース側
電極（すなわち凝集板）へのダスト付着を１０
防止するため、ガス流速１０ｍ／ｓ（すなわち、通常の
排煙脱硫装置の入口煙道内ガス流速）以上とし、
電極へのダスト付着を防止するため、ガス温度は１００
℃（すなわち、通常の排煙脱硫装置の冷却塔より上流側
のガス温度）以上とする。また、適用プラントをばいじ
んの電気抵抗率の低い重専ボイラプラントに限定する。(3) That is, in order to prevent dust from adhering to the discharge electrode and the earth side electrode (i.e. agglomeration plate), the device of the present invention has a gas flow rate of 10 m/s (i.e., the gas in the inlet flue of a normal flue gas To prevent dust from adhering to the electrodes, the gas temperature was set at 100°C.
℃ (that is, the gas temperature upstream of the cooling tower of a normal flue gas desulfurization equipment) or higher. In addition, the applicable plants are limited to heavy boiler plants with low electrical resistivity of soot and dust.
そして、ガス流速が速いため、凝集空間内におけるダス
トの滞留時間が短いにもかかわらず、効果的な凝集効果
を得るために、凝集板上での平均コロナ電流密度が例え
ば５ ｍＡ／ ｒｒｔ以上、凝集空間の平均電界強度が
例えば５ｋＶ／ｃｍ以上といった大きな値に設定できる
様に、放電極と凝集板との間隔をナロウスベイシング（
８０■以下）とする。In addition, in order to obtain an effective agglomeration effect even though the residence time of the dust in the aggregation space is short due to the high gas flow rate, the average corona current density on the aggregation plate must be, for example, 5 mA/rrt or more. The distance between the discharge electrode and the agglomeration plate is narrow basing (
80■ or less).
上述の手段により、次の作用が得られる。 The above-mentioned means provide the following effects.
（１）放電極と凝集板をナロウスペイシングにするため
、従来の静電凝集装置に比べ非常に高電界かつ高コロナ
電流の凝集空間が得られる。そのた１１
め、ガス流速が速く、ダストの凝集空間内における滞留
時間が短いにもかかわらず、十分な空間凝集効果が得ら
れる。(1) Since the discharge electrode and aggregation plate are narrowly spaced, a coagulation space with a much higher electric field and higher corona current can be obtained compared to conventional electrostatic coagulation devices. Therefore, a sufficient spatial aggregation effect can be obtained even though the gas flow rate is high and the residence time of dust in the aggregation space is short.
（２）放電極と凝集板をナロウスペイシングにするため
、従来の静電凝集装置に比べて高コロナ電流が得られ、
コロナ電流の約１７２乗に比例して増大するイオン風に
よる主ガス流に直交する二次流れを大きくできる。その
ため、ダストの凝集板への移動速度が増大し、またダス
トの凝集板への衝突確率が増大し、従来より高い電極凝
集効果が得られる。(2) Because the discharge electrode and aggregation plate are narrowly spaced, a higher corona current can be obtained compared to conventional electrostatic aggregation devices.
It is possible to increase the secondary flow perpendicular to the main gas flow due to the ion wind, which increases in proportion to about the 172nd power of the corona current. Therefore, the speed at which dust moves to the aggregation plate increases, and the probability of dust colliding with the aggregation plate increases, making it possible to obtain a higher electrode aggregation effect than in the past.
（３） ガス流速が高速で、凝集板上のダストが後流
へ流され易く、ガス温度が高い為、ダストの粒着性も低
く、また対象とするダストの電気抵抗率も低いため、凝
集板に到達したダストはただちに電荷を放出し、凝集板
へ電気的に付着しようとする力もほとんどない。従って
ダストが電極へ付着・堆積することがなく、電極上の付
着ダストの洗浄手段は不要となる。(3) The gas flow rate is high, and the dust on the aggregation plate is easily flowed to the downstream, and the gas temperature is high, so the particle adhesion of the dust is low, and the electrical resistivity of the target dust is also low, so it is difficult to agglomerate. When the dust reaches the plate, it immediately releases its charge and has almost no force to electrically adhere to the aggregation plate. Therefore, dust does not adhere or accumulate on the electrodes, and there is no need for cleaning means for cleaning the dust adhering to the electrodes.
１ ２
〔実施例〕
本発明の実施例を第１図〜第４図に示す。第１図は、本
発明を適用した重専ボイラプラントの排煙処理設備の全
体系統図を示す。第２図は、本発明の静電凝集装置の構
成説明図、第３図は、同電極部の詳細説明図、第４図に
は、本発明による効果を示すグラフを示す。1 2 [Example] Examples of the present invention are shown in FIGS. 1 to 4. FIG. 1 shows an overall system diagram of flue gas treatment equipment for a heavy-duty boiler plant to which the present invention is applied. FIG. 2 is an explanatory diagram of the structure of the electrostatic condensation device of the present invention, FIG. 3 is a detailed explanatory diagram of the electrode section, and FIG. 4 is a graph showing the effects of the present invention.
第１図において、重専ボイラ１０からの排ガスは、空気
余熱器１１を経て排煙脱硫装置人口煙道９に導かれ、同
煙道内に組みこまれた静電凝集装置１２において、排ガ
ス中に含まれるばいじん等のダストを凝集・粗大化した
後、排煙脱硫装置の冷却塔１３及び吸収塔１４にてばい
じん等のダストが効果的に捕集された後、排ガスは煙突
１５から大気へ放出される。In FIG. 1, exhaust gas from a heavy-duty boiler 10 is led to an artificial flue 9 of the flue gas desulfurization device through an air preheater 11, and is added to the flue gas in an electrostatic coagulation device 12 built into the flue. After the dust such as soot and dust contained therein is aggregated and coarsened, and after the dust such as soot and dust is effectively collected in the cooling tower 13 and absorption tower 14 of the flue gas desulfurization equipment, the flue gas is released into the atmosphere from the chimney 15. be done.
静電凝集装置１２は、第２図に示すように、排煙脱硫装
置人口煙道９の一部に組み込まれており、本例の場合断
面が角状の本体ケーシング７の内部を凝集板２によって
断面が正方形状の小ダクトに流路分割されている。各小
ダクトの中心には、放１３
？極１が設置され、放電極１は放電極取付金具４により
放電極支持梁３に固定され、複数の放電極を支持した放
電極支持梁３は、碍子室５内に設置された支持碍子６を
介して、本体ケーシング７及び凝集板２とは電気的に絶
縁された上で固定されている。放電極１、放電極取付金
具４、放電極支持梁３から或るいわゆる放電極系には、
高圧電源１８により高電圧が印加される。第３図に方電
極１と、凝集板２から成る凝集部の詳細を示す。本例の
放電極１は、丸棒の周囲９０’ごとに、鋭角のトゲ状突
起を有するフラットバーを４枚取り付けた構造であるが
、例えば本例のトゲ状突起の代りに、フラットバー全体
の端部がシャープ■エッジ状に加工されているものや、
細線ワイヤ等、大きなコロナ電流を流すことのできる、
いわゆる「高電流型」の放電極であれば、第３図以外の
形状でも可能である。放電極１の先端と凝集板２（すな
わち、アース電極としても機能する）の距離Ｄｏはナロ
ウスペイシングにされているが、これは、高コロナ放電
電流を得るために不可欠なことであ１ ４
り、高コロナ電流を得る為には、少くともＤｏを８０１
Ｉｌｍ以下のナロウスペイシングとする必要がある。本
静電凝集装置１２は、排煙脱硫装置入口煙道つとガス通
過断面積がほぼ等しいので、静電空間における主ガス流
速はほぼ煙道流速に等しく約１５１Ｉｌ／ｓという高速
である。従って主ガス中に含まれるばいじん等のダスト
の凝集空間内の滞留時間は、凝集空間長さが５０ｃｍの
場合で約０．０３秒と極めて短いが、前述の如く電極間
隔がナロウスペイシングにされ、８ｋＶ／ｃｍ程度の高
電界かっ１０ｖｎＡ／ｒｒｒ程度の高コロナ電流密度が
実現されているので、十分な空間凝集効果が達成される
とともに、この高コロナ電流密度に起因して、主ガスに
直交する方向のイオン風による大きな二次流れが生じる
。そして、ばいじん等のダストの凝集板２への移動速度
が増大し、ダストの凝集板への衝突確率が増大するため
、高い電極凝集効果も得られている。しかも、前述の様
に主ガス流速が約１５ｍ／ｓという高速であるために凝
集板上のダストは後流へ流され易く、ガス温度は１００
℃以上なのでダ１５
ストの粘着性も低く、また重専ボイラの排ガス中のばい
じんの電気抵抗率が１０４Ω・印程度と非常に低抵抗で
あるので、凝集板に到達したダストはただちに電荷を放
出して凝集板へ付着しようとする電気的な力もほとんど
ないため、本実施例における放電極１および凝集板２へ
のダスト付着はまったく見られず、電極の自己クリーニ
ング機能が確認されている。従って経時的な荷電状況の
劣化もなく、長時間にわたり安定して、静電凝集装置と
しての機能を果たしている。As shown in FIG. 2, the electrostatic coagulation device 12 is incorporated into a part of the artificial flue 9 of the flue gas desulfurization device, and in this example, the inside of the main body casing 7, which has a square cross section, is covered with a coagulation plate 2. The flow path is divided into small ducts with square cross sections. In the center of each small duct is a 13? The pole 1 is installed, the discharge electrode 1 is fixed to the discharge electrode support beam 3 by the discharge electrode mounting bracket 4, and the discharge electrode support beam 3 supporting the plurality of discharge electrodes is attached to the support insulator 6 installed in the insulator chamber 5. The main body casing 7 and the aggregation plate 2 are electrically insulated and fixed via the main body casing 7 and the aggregation plate 2. A so-called discharge electrode system includes a discharge electrode 1, a discharge electrode mounting bracket 4, and a discharge electrode support beam 3.
A high voltage is applied by a high voltage power supply 18. FIG. 3 shows the details of the aggregation section consisting of the square electrode 1 and the aggregation plate 2. The discharge electrode 1 of this example has a structure in which four flat bars having acute-angled thorn-like protrusions are attached to each 90' of the circumference of a round bar. The edges are sharp ■The edges are processed into an edge shape,
Thin wire, etc., which can flow a large corona current,
As long as it is a so-called "high current type" discharge electrode, shapes other than those shown in FIG. 3 are also possible. The distance Do between the tip of the discharge electrode 1 and the aggregation plate 2 (that is, it also functions as a ground electrode) is set to narrow spacing, which is essential for obtaining a high corona discharge current. In order to obtain a high corona current, Do should be set to at least 801.
It is necessary to use narrow spacing of Ilm or less. Since the present electrostatic condensing device 12 has a gas passage cross-sectional area almost equal to that of the flue at the entrance of the flue gas desulfurization device, the main gas flow velocity in the electrostatic space is approximately equal to the flue flow velocity and is as high as about 151 Il/s. Therefore, the residence time of dust such as soot and dust contained in the main gas in the coagulation space is extremely short, approximately 0.03 seconds when the coagulation space length is 50 cm, but as mentioned above, the electrode spacing is narrow. , a high electric field of about 8 kV/cm and a high corona current density of about 10 vnA/rrr have been achieved, so that a sufficient spatial cohesion effect is achieved, and due to this high corona current density, the current density is perpendicular to the main gas. A large secondary flow is generated due to the ion wind in the direction of In addition, since the speed of movement of dust such as soot and dust to the aggregation plate 2 increases, and the probability of dust collision with the aggregation plate 2 increases, a high electrode aggregation effect is also obtained. Moreover, as mentioned above, since the main gas flow velocity is as high as about 15 m/s, the dust on the aggregation plate is easily flowed to the downstream, and the gas temperature is 100 m/s.
Since it is above 15°C, the stickiness of the dust is low, and the electrical resistivity of the dust in the exhaust gas of heavy-duty boilers is very low, around 104Ω, so the dust that reaches the aggregation plate immediately releases its charge. Since there is almost no electric force that tends to cause dust to adhere to the aggregation plate, no dust was observed to adhere to the discharge electrode 1 and the aggregation plate 2 in this example, confirming the self-cleaning function of the electrodes. Therefore, there is no deterioration of the charging state over time, and the device stably functions as an electrostatic agglomeration device over a long period of time.
第４図は、本実施例における排煙脱硫装置の冷却塔の直
前でアンダーセン・スタック●サンプラにより測定した
流入ダストの粒径分布をいわゆるロジン●ラムラー線図
に表したもので、横軸がダストの粒子径、縦軸がダスト
の累積分布割合を示す。第４図中Ａで示した曲線は、本
実施例の静電凝集装置を荷電しない場合、すなわち静電
凝集が行われない場合のダスト粒径分布を示しており、
Ｂで示した曲線は、本実施例の静電凝集装置を荷電した
場合（ ８ ｋＶ／ ｃｍ， １ ０ ＩＩＩＡ／
ｒｆ）すなわち静１６
電凝集が行われている場合のダスト粒径分布を示してい
る。Ｂの曲線の方がＡの曲線より全体に右側に位置して
おり、静電凝集効果によりダストが凝集・粗大化され、
粒径が大きくなったことがわかる。特に、１μｎ以下の
サブクミロン粒子に注目すると、曲線Ａの場合２０％以
上がサブミクロン粒子であったのに対して、曲線Ｂの場
合のサブミクロン粒子は７％程度であるので、サブミク
ロン粒子を１＃以上の粒径に凝集・粗大化させることに
対して、本静電凝集装置が非常に有効であることを示し
ている。Figure 4 shows the particle size distribution of the inflowing dust measured by an Andersen stack sampler just before the cooling tower of the flue gas desulfurization equipment in this example in a so-called rosin Rammler diagram, where the horizontal axis represents the dust. The particle size of , and the vertical axis indicates the cumulative distribution ratio of dust. The curve indicated by A in FIG. 4 shows the dust particle size distribution when the electrostatic agglomeration device of this example is not charged, that is, when electrostatic aggregation is not performed.
The curve shown by B shows the case where the electrostatic condensation device of this example is charged (8 kV/cm, 10 IIIA/
rf), that is, the dust particle size distribution when electrostatic 16 electrocoagulation is performed. The curve B is located on the right side of the curve A as a whole, and the dust is aggregated and coarsened due to the electrostatic agglomeration effect.
It can be seen that the particle size has increased. In particular, if we focus on submicron particles of 1 μn or less, more than 20% of them in curve A are submicron particles, while about 7% of them in curve B are submicron particles. This shows that the present electrostatic agglomeration device is very effective in aggregating and coarsening particles to a particle size of 1 # or more.
第５図に、本発明の静電凝集装置による、重専ボイラ用
排煙脱硫装置の出口ダスト濃度の低減例を示す。縦軸は
出口ダスト濃度を示し、横軸は本発明の静電凝集装置の
比コロナ電力すなわち荷電圧とコロナ電流密度の積を示
す。FIG. 5 shows an example of reducing the dust concentration at the exit of a flue gas desulfurization device for a heavy-duty boiler using the electrostatic coagulation device of the present invention. The vertical axis shows the exit dust concentration, and the horizontal axis shows the specific corona power of the electrostatic coagulation device of the present invention, that is, the product of the charging voltage and the corona current density.
本発明の静電凝集装置を設置しない場合（すなわち無荷
電の場合）には、排煙脱硫装置入口ダスト濃度約３５０
■／ ｍ’ Ｎに対する出口ダスト濃度は約１００■／
ｒｎ’ Ｎあったが、本発明装置を使用１７
すると、比較的低品質の重油を燃料とし、０２を絞った
ボイラ燃焼を実施しているため、本発明の静電凝集装置
に高電圧を印加するに従い、排煙脱硫装置に流入するダ
ストの粒径が凝集・粗大化されて大きくなる。その結果
排煙脱硫装置におけるダストの捕集効率が増大し、出口
のダスト濃度が低減し、比コロナ電力４００Ｗ／ｒｒｒ
においてはダスト濃度を４０■／ｍ３Ｎ以下にすること
ができた。When the electrostatic condensation device of the present invention is not installed (that is, when it is uncharged), the dust concentration at the inlet of the flue gas desulfurization device is approximately 350.
■／The outlet dust concentration for m'N is approximately 100■/
rn' N, but when using the device of the present invention, relatively low-quality heavy oil is used as fuel and boiler combustion with reduced 02 is performed, so high voltage is applied to the electrostatic condensation device of the present invention. As the temperature increases, the particle size of the dust flowing into the flue gas desulfurization equipment becomes larger due to agglomeration and coarsening. As a result, the dust collection efficiency in the flue gas desulfurization equipment increases, the dust concentration at the outlet decreases, and the specific corona power reaches 400W/rrr.
In this case, it was possible to reduce the dust concentration to 40 .mu./m3N or less.
すなわち、規制値５０■／ｒ１１′Ｎよりも十分に近い
値にできた。In other words, the value was sufficiently close to the regulation value of 50/r11'N.
本発明は、前述のように構或されているので、以下に記
載するような効果を奏する。Since the present invention is constructed as described above, it produces the effects described below.
（１）重専ボイラプラントにおける排煙脱硫装置の入口
煙道内に組み込み、コンパク１・でかつ比較的安価に排
ガス中のばいじん等のダストを静電凝集・粗大化するこ
とが可能になったさ排煙脱硫装置におけるダストの捕集
・除去効率が向上する。(1) By incorporating it into the inlet flue of the flue gas desulfurization equipment in a heavy boiler plant, it has become possible to electrostatically coagulate and coarsen dust such as soot and dust in flue gas in a compact and relatively inexpensive manner. Dust collection and removal efficiency in flue gas desulfurization equipment is improved.
（２）低品質な重油を燃料として使用し、脱硝装置を設
けることなく発生ＮＯｘを抑えるべくボイ１８
ラの燃焼調整を実施するためばいじん発生量が非常に多
い場合にも、乾式または湿式電気集じん装置やバグフィ
ルタ等のばいじん捕集用の専用装置を設置することなく
、主としてＳＯｘ対策用として設置する排煙脱硫装置の
みによって、ばいじん等ダストの排出濃度を規制値以下
にすることができる。(2) Low-quality heavy oil is used as fuel, and the combustion adjustment of the boiler 18 is carried out to suppress the generated NOx without installing a denitrification device. Without installing a dedicated device for dust collection such as a dust device or bag filter, it is possible to reduce the emission concentration of dust such as soot to below the regulation value only by using a flue gas desulfurization device installed mainly for SOx countermeasures.
第１図は、本発明の実施例に係る排煙処理設備の全体系
統図、第２図は、本発明の静電凝集装置の構成説明図、
第３図は本茜明の静電凝集装置の電極部の詳細説明図、
第４図は排煙脱硫装置冷却塔入口におけるダストの粒径
分布図、第５図は排煙脱硫装置出口におけるばいじん濃
度と静電凝集装置の比コロナ電力の関係を示す図、第６
図は、従来の排煙処理設備の全体系統図の１例を示す図
である。
１・・・放電極、２・・・凝集板（アース側電極）、３
・・・放電極支持梁、４・・・放電極取付金具、５・・
・碍子室、６・・・支持碍子、７・・・本体ケーシング
、１９
８・・・点検用マンホール、９・・・排煙脱硫装置入口
煙道、１０・・・ボイラ、１１・・・空気余熱器、１２
・・・静電凝集装置、１３・・・排煙脱硫装置冷却塔、
１４・・・排煙脱硫装置吸収塔、１５・・・煙突、１６
・・・空気供給ライン、１７・・・燃料供給ライン、ａ
・・・主ガス流入方向、１８・・・高圧電源。FIG. 1 is an overall system diagram of flue gas treatment equipment according to an embodiment of the present invention, and FIG. 2 is an explanatory diagram of the configuration of an electrostatic condensation device of the present invention.
Figure 3 is a detailed explanatory diagram of the electrode part of Akane Moto's electrostatic condensation device.
Figure 4 is a particle size distribution diagram of dust at the inlet of the cooling tower in the flue gas desulfurization equipment, Figure 5 is a diagram showing the relationship between the dust concentration at the outlet of the flue gas desulfurization equipment and the specific corona power of the electrostatic coagulation equipment, and Figure 6
The figure is a diagram showing an example of an overall system diagram of a conventional flue gas treatment facility. 1... Discharge electrode, 2... Coagulation plate (earth side electrode), 3
...Discharge electrode support beam, 4...Discharge electrode mounting bracket, 5...
・Insulator chamber, 6... Support insulator, 7... Main body casing, 19 8... Inspection manhole, 9... Flue gas desulfurization equipment inlet flue, 10... Boiler, 11... Air Preheater, 12
... Electrostatic condensation device, 13 ... Flue gas desulfurization device cooling tower,
14... Flue gas desulfurization equipment absorption tower, 15... Chimney, 16
...Air supply line, 17...Fuel supply line, a
...Main gas inflow direction, 18...High voltage power supply.
Claims (2)
する静電凝集装置（１２）において、前記放電極（１）
は細線ワイヤあるいは複数のとげ状の突起ないしシャー
プエッジ状の棒状の高電流型放電極とし、 前記放電極（１）と凝集板（２）を電気的に絶縁すると
ともに、放電極（１）の表面と凝集板（２）の表面の最
短間隔を８０ｃｍ以下のナロウスペーシングとし、放電
極（１）と凝集板（２）の間には高電界で高コロナ放電
電流の凝集空間を実現させる高圧電源（１８）を接続し
、排煙脱硫装置の冷却塔（１３）の上流側の入口煙道（
９）内のガス温度が１００℃以上、ガス流速が１０ｍ／
ｓ以上の領域に組込み、前記凝集空間において生ずる空
間凝集および前記凝集板状において生ずる電極凝集の相
乗効果により、重専ボイラから排出されるばい塵等のダ
ストの凝集粗大化を行なうことを特徴とする静電凝集装
置。(1) In an electrostatic agglomeration device (12) having a charging section consisting of a discharge electrode (1) and an aggregation plate (2), the discharge electrode (1)
is a high current discharge electrode in the form of a thin wire or a bar with multiple barbed protrusions or sharp edges, which electrically insulates the discharge electrode (1) and the aggregation plate (2), and The shortest distance between the surface and the surface of the aggregation plate (2) is narrow spacing of 80 cm or less, and a high voltage is applied between the discharge electrode (1) and the aggregation plate (2) to realize a cohesion space with a high electric field and a high corona discharge current. Connect the power supply (18) and connect the inlet flue (
9) The gas temperature inside is 100℃ or more, and the gas flow velocity is 10m/
It is incorporated in an area of s or more, and the synergistic effect of the spatial aggregation occurring in the aggregation space and the electrode aggregation occurring in the aggregation plate shape causes the agglomeration and coarsening of dust such as soot and dust discharged from the heavy boiler. Electrostatic flocculation device.
率と、ガス温度が１００℃以上の高温であることと、ガ
ス流速が１０ｍ／ｓ以上の高速流であることにより、放
電極および凝集板上へのばいじん等の付着を防止し、定
常的な電極の槌打および洗浄するための装置のいずれか
を省略することを特徴とする請求項（１）記載の静電凝
集装置。(2) Due to the low electrical resistivity of the soot and dust discharged from heavy boilers, the high gas temperature of 100°C or higher, and the high-speed gas flow of 10 m/s or higher, discharge electrodes and agglomeration are possible. The electrostatic coagulation device according to claim 1, characterized in that any device for preventing dust and the like from adhering to the plate and for regularly hammering and cleaning the electrodes is omitted.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15668289A JP2659805B2 (en) | 1989-06-21 | 1989-06-21 | Electrostatic coagulation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15668289A JP2659805B2 (en) | 1989-06-21 | 1989-06-21 | Electrostatic coagulation device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0326351A true JPH0326351A (en) | 1991-02-04 |
| JP2659805B2 JP2659805B2 (en) | 1997-09-30 |
Family
ID=15633022
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15668289A Expired - Fee Related JP2659805B2 (en) | 1989-06-21 | 1989-06-21 | Electrostatic coagulation device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2659805B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5070811A (en) * | 1988-09-27 | 1991-12-10 | Albert Feuerstein | Apparatus for applying dielectric or metallic materials |
| CN102962135A (en) * | 2012-09-26 | 2013-03-13 | 山东国舜建设集团有限公司 | Wet-type sintering desulfurization flue gas deep purification device |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106669349B (en) * | 2017-02-23 | 2019-06-04 | 浙江彩蝶实业有限公司 | Tenter frame exhaust cleaning treatment system |
-
1989
- 1989-06-21 JP JP15668289A patent/JP2659805B2/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5070811A (en) * | 1988-09-27 | 1991-12-10 | Albert Feuerstein | Apparatus for applying dielectric or metallic materials |
| CN102962135A (en) * | 2012-09-26 | 2013-03-13 | 山东国舜建设集团有限公司 | Wet-type sintering desulfurization flue gas deep purification device |
| CN102962135B (en) * | 2012-09-26 | 2015-08-05 | 山东国舜建设集团有限公司 | Wet type sintering desulfuration flue gas device for deep cleaning |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2659805B2 (en) | 1997-09-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Yang et al. | Highly efficient removal of sulfuric acid aerosol by a combined wet electrostatic precipitator | |
| RU2262386C2 (en) | Method and a device for agglomeration of particles | |
| CN109127136B (en) | Ultra-high-efficiency low-temperature electric dust removal device based on multi-field agglomeration | |
| US5147423A (en) | Corona electrode for electrically charging aerosol particles | |
| US4449159A (en) | Focusing electrodes for high-intensity ionizer stage of electrostatic precipitator | |
| JPH0456646B2 (en) | ||
| CN108325314B (en) | Particle concentration electric turbulence condensation device for PM2.5 removal | |
| JPH0326351A (en) | Equipment and method for electrostatic flocculation | |
| CN111068451B (en) | Device and method for efficiently removing fine particulate matters through temperature and humidity regulation | |
| JP2607680B2 (en) | Electric precipitator and operating method thereof | |
| JP2007107399A (en) | Exhaust emission control device for internal combustion engine | |
| JP6827864B2 (en) | Coagulation device and exhaust gas treatment device equipped with this | |
| JP6953605B2 (en) | Electrostatic precipitator | |
| Lagarias | Discharge electrodes and electrostatic precipitators | |
| CN203448182U (en) | Electric dust remover | |
| JP3376338B2 (en) | Helical screw type high efficiency dust charging device | |
| Dalmon | Electrostatic precipitators for large power station boilers | |
| JP3388842B2 (en) | Conduction filter | |
| CN205650338U (en) | Shuan dian district micronic dust processing apparatus | |
| US9574586B2 (en) | System and method for an electrostatic bypass | |
| Darby | Criteria for designing electrostatic precipitators | |
| KR102298965B1 (en) | Electric and magnetic dust collector | |
| JPH02217711A (en) | Catching fly ash from flue gas of coal burning boiler | |
| KR102402795B1 (en) | Electric and magnetic dust collector having distributed switching ionizer | |
| Chauke et al. | Effect of high frequency power supplies on the electrostatic precipitator collection efficiency as compared to conventional transformer rectifiers |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| S531 | Written request for registration of change of domicile |
Free format text: JAPANESE INTERMEDIATE CODE: R313531 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| S111 | Request for change of ownership or part of ownership |
Free format text: JAPANESE INTERMEDIATE CODE: R313111 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090606 Year of fee payment: 12 |
|
| LAPS | Cancellation because of no payment of annual fees |