JPH0372333B2 - - Google Patents
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- Publication number
- JPH0372333B2 JPH0372333B2 JP58002271A JP227183A JPH0372333B2 JP H0372333 B2 JPH0372333 B2 JP H0372333B2 JP 58002271 A JP58002271 A JP 58002271A JP 227183 A JP227183 A JP 227183A JP H0372333 B2 JPH0372333 B2 JP H0372333B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- heat exchanger
- adsorbent
- sulfur oxides
- desorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- Treating Waste Gases (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Description
【発明の詳細な説明】
本発明は硫黄酸化物の脱離方法に関し、特に乾
式脱硫黄装置の脱離塔において吸着剤を高温に加
熱して硫黄酸化物を脱着させる方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for desorbing sulfur oxides, and more particularly to a method for desorbing sulfur oxides by heating an adsorbent to a high temperature in a desorption tower of a dry desulfurization apparatus.
排ガス中の硫黄酸化物を半成コークス、活性炭
のような吸着剤に吸着後、脱離させ、この脱離し
た硫黄酸化物を気相下で還元して単体硫黄を凝縮
分離し、さらに残りのガスを例えばクラウス反応
に供して単体硫黄を回収する乾式脱硫装置は、石
灰スラリーなどを用いる湿式脱硫装置に比較し
て、多量の用水を必要とせず、また脱硫処理後の
排ガスの再加熱が不要であり、かつ排水が発生し
ない等の利点があり、注目されている。しかしこ
のような脱硫装置においては、二酸化硫黄の脱離
塔および還元塔などで高温操作が必要となり、そ
の安全対策が問題となる。 Sulfur oxides in exhaust gas are adsorbed and desorbed by adsorbents such as semi-formed coke and activated carbon, and the desorbed sulfur oxides are reduced in the gas phase to condense and separate elemental sulfur. Dry desulfurization equipment, which recovers elemental sulfur by subjecting gas to the Claus reaction, does not require large amounts of water compared to wet desulfurization equipment that uses lime slurry, and does not require reheating of exhaust gas after desulfurization treatment. It is attracting attention because of its advantages such as not generating wastewater. However, such desulfurization equipment requires high-temperature operation in the sulfur dioxide desorption tower, reduction tower, etc., and safety measures are a problem.
従来の典型的な乾式脱硫装置の系統図を第１図
に示す。図において、硫黄酸化物（代表例として
SO2）を含む排ガスは、導管８により吸着塔１に
導かれ、塔内に充填された半成コークス等によ
り、吸着、脱硫された後、清浄ガスとなつて導管
９から排出される。一方、SO2を吸着した吸着剤
は導管１０を通つて脱離塔２の加熱部２Ａに供給
され、ここで熱交換器１３に導入される脱離用加
熱ガスにより間接加熱され、SO2分を脱離して吸
着剤が再生される。再生吸着剤は、脱離塔２内の
下部で冷却水の流通する導管１２により間接冷却
された後、導管１１を通り、再び吸着塔１に循環
される。脱離されたSO2ガスは、SO2還元塔３に
より還元剤である炭素剤１５と反応して、硫黄ガ
スを生成し、この硫黄ガスは硫黄凝縮器４で冷却
されて回収され、他の反応生成物である硫化水
素、硫化カルボニルおよび未反応のSO2ガスは熱
交換器５を経てクラウス反応器６で硫黄に変換さ
れ、硫黄凝縮器４で硫黄が回収される。 A system diagram of a typical conventional dry desulfurization equipment is shown in Figure 1. In the figure, sulfur oxides (as a typical example
The exhaust gas containing SO 2 ) is led to the adsorption tower 1 through a conduit 8 , where it is adsorbed and desulfurized by semi-formed coke or the like filled in the tower, and then discharged through a conduit 9 as clean gas. On the other hand, the adsorbent that has adsorbed SO 2 is supplied to the heating section 2A of the desorption tower 2 through the conduit 10, where it is indirectly heated by the heating gas for desorption introduced into the heat exchanger 13, and the SO 2 is desorbed and the adsorbent is regenerated. The regenerated adsorbent is indirectly cooled at the lower part of the desorption tower 2 through a conduit 12 through which cooling water flows, and then circulated through the conduit 11 to the adsorption tower 1 again. The desorbed SO 2 gas reacts with the carbon agent 15, which is a reducing agent, in the SO 2 reduction tower 3 to generate sulfur gas, which is cooled and recovered in the sulfur condenser 4 and used in other The reaction products, hydrogen sulfide, carbonyl sulfide, and unreacted SO 2 gas, pass through a heat exchanger 5 and are converted into sulfur in a Claus reactor 6, and the sulfur is recovered in a sulfur condenser 4.
上記脱離塔２においては、塔内の熱交換器外に
上方から炭素質吸着剤が供給され、移動層を形成
しながら下方に移動する間に熱交換器１３内を通
る700〜800℃の高温ガス（通常は燃焼排ガス）に
より400℃程度に加熱され、吸着剤から硫黄酸化
物が脱着される。 In the desorption column 2, the carbonaceous adsorbent is supplied from above outside the heat exchanger in the column, and while moving downward while forming a moving bed, the carbonaceous adsorbent passes through the heat exchanger 13 at a temperature of 700 to 800°C. It is heated to around 400°C by high-temperature gas (usually combustion exhaust gas), and sulfur oxides are desorbed from the adsorbent.
しかしながら、上記従来の脱着方法において
は、熱交換器内の加熱ガスが高温高圧であり、万
一、ガス漏れを生じたときにガス中の酸素により
炭素質吸着剤が燃焼を開始し、危険であるのみな
らず、吸着剤の酸化、焼損が著しいという欠点が
ある。 However, in the conventional desorption method described above, the heated gas in the heat exchanger is at high temperature and high pressure, and in the event of a gas leak, the carbonaceous adsorbent will start burning due to the oxygen in the gas, which can be dangerous. In addition, there is a drawback that the adsorbent is significantly oxidized and burnt out.
本発明の目的は、上記従来技術に鑑み、熱交換
器内のガス漏れを防止し、また万一ガス漏れを生
じた場合でも炭素質吸着剤の自燃を生じない硫黄
酸化物の脱離方法を提供することにある。 In view of the above prior art, an object of the present invention is to provide a method for desorbing sulfur oxides that prevents gas leakage in a heat exchanger and does not cause self-combustion of the carbonaceous adsorbent even if gas leakage occurs. It is about providing.
本発明は、高温ガスが流通する熱交換器を内蔵
する脱離塔内に硫黄酸化物を吸着した炭素質吸着
剤を供給し、間接加熱により前記吸着剤から硫黄
酸化物を脱離する方法において、熱交換器を通る
高温ガスの圧力を炭素質吸着剤側よりも負圧と
し、かつ該ガス中の酸素濃度を１％以下としたこ
とを特徴とする。 The present invention provides a method for supplying a carbonaceous adsorbent adsorbing sulfur oxides into a desorption tower having a built-in heat exchanger through which high-temperature gas flows, and desorbing sulfur oxides from the adsorbent by indirect heating. , the pressure of the high-temperature gas passing through the heat exchanger is set to be lower than that of the carbonaceous adsorbent side, and the oxygen concentration in the gas is set to 1% or less.
本発明において、熱交換器内の加熱ガスの圧力
を負圧としたのは、万一ガス漏れがあつても熱交
換器内の高温ガスが炭素質吸着剤側に容易に流出
しないようにうするためである。このような圧力
としては300mmH2O以下が好ましい。また上記高
温ガス中の酸素濃度は、１％（vol％）以下が適
当である。該酸素濃度が１％を越えると、ガス漏
れを生じた場合に管外の炭素質吸着剤と酸素が反
応して吸着剤の燃焼または燃損を生じるおそれが
ある。 In the present invention, the pressure of the heated gas in the heat exchanger is set to negative pressure to prevent the high temperature gas in the heat exchanger from easily flowing out to the carbonaceous adsorbent side even if there is a gas leak. This is to do so. Such a pressure is preferably 300 mmH 2 O or less. Further, the oxygen concentration in the high temperature gas is suitably 1% (vol%) or less. If the oxygen concentration exceeds 1%, there is a risk that in the event of gas leakage, the carbonaceous adsorbent outside the tube and oxygen will react, resulting in combustion or burnout of the adsorbent.
本発明において、熱交換器内の高温ガス中の酸
素濃度を１％以下にするには、たとえば石炭、重
質油等を低酸素状態で燃焼させるか、または燃焼
排ガス中の酸素を粉状活性炭等と接触させて強制
的にO2を吸収除去させる方法が用いられる。 In the present invention, in order to reduce the oxygen concentration in the high-temperature gas in the heat exchanger to 1% or less, for example, coal, heavy oil, etc. can be burned in a low-oxygen state, or oxygen in the combustion exhaust gas can be reduced to powdered activated carbon. A method is used in which O 2 is forcibly absorbed and removed by contacting with a substance such as the like.
上記熱交換器は、炭素質吸着剤の加熱および移
動を均一にするために、例えば千鳥状に配列する
ことが好ましい。 The heat exchangers are preferably arranged in a staggered manner, for example, in order to uniformly heat and move the carbonaceous adsorbent.
以下、本発明を図面によりさらに詳細に説明す
る。 Hereinafter, the present invention will be explained in more detail with reference to the drawings.
第２図は、本発明の一実施例を示す脱離塔の加
熱部２Ａの断面図である。脱離塔加熱部２Ａ内に
は、一対のヘツダ２０，２２間を多数の熱交換器
２４で連結した熱交換ユニツトが多段に配設さ
れ、各ユニツトのヘツダ２０，２２はさらに垂直
の連結パイプ２６で上下一体に連結されている。 FIG. 2 is a sectional view of a heating section 2A of a desorption column showing an embodiment of the present invention. In the desorption tower heating section 2A, heat exchange units in which a pair of headers 20 and 22 are connected by a large number of heat exchangers 24 are arranged in multiple stages, and the headers 20 and 22 of each unit are further connected to a vertical connecting pipe. The upper and lower parts are integrally connected at 26.
上記構成の脱離塔において、塔内には上方から
炭素質吸着剤（半成コークス等）が供給され、移
動層を形成しながら下方に移動する間に、熱交換
器２４内を通る700〜800℃の燃焼排ガスにより吸
着剤は400℃程度に加熱され、硫黄酸化物が脱着
される。この場合、上記燃焼排ガスの圧力は熱交
換器外よりも低い300mmH2O以下に保持され、ま
たその酸素濃度は１％以下に調整される。 In the desorption tower having the above configuration, carbonaceous adsorbent (semi-formed coke, etc.) is supplied into the tower from above, and while moving downward while forming a moving bed, it passes through the heat exchanger 24 The adsorbent is heated to approximately 400°C by the combustion exhaust gas at 800°C, and sulfur oxides are desorbed. In this case, the pressure of the combustion exhaust gas is maintained at 300 mmH 2 O or less, which is lower than that outside the heat exchanger, and the oxygen concentration is adjusted to 1% or less.
上記実施例によれば、熱交換器２４に万一ガス
漏れを生じた場合でも、外部より負圧になつてい
るのでガスが熱交換器外に容易に流出せず、また
ガス中の酸素濃度が低いので少量ガスが露出して
も熱交換器外の炭素質吸着剤と反応して燃焼を開
始するまでには至らず、燃焼の危険を避けること
ができる。なお、上記実施例において、脱離塔２
は加熱部２Ａと冷却部に分けた構成としたが、こ
れは加熱部のみとし、冷却部は別個に設けてもよ
い。 According to the above embodiment, even if a gas leak occurs in the heat exchanger 24, the gas does not easily leak out of the heat exchanger because the pressure is negative from the outside, and the oxygen concentration in the gas Since the gas is low, even if a small amount of gas is exposed, it will not react with the carbonaceous adsorbent outside the heat exchanger and start combustion, thereby avoiding the danger of combustion. In addition, in the above embodiment, the desorption tower 2
Although the configuration is divided into the heating section 2A and the cooling section, this may be only the heating section and the cooling section may be provided separately.
以上、本発明によれば、乾式脱硫装置における
脱離塔の加熱ガスの圧力を所定値以下とし、かつ
その酸素濃度を１％以下とすることにより、万一
ガス漏れを生じた場合の炭素質吸着剤の燃焼の危
険、焼損等を防止し、装置の安全性および経済性
を高めることができる。 As described above, according to the present invention, by setting the pressure of the heated gas in the desorption tower in the dry desulfurization equipment to a predetermined value or less and the oxygen concentration to 1% or less, carbon It is possible to prevent the danger of combustion of the adsorbent, burnout, etc., and improve the safety and economic efficiency of the device.
第１図は、乾式脱硫装置の系統図、第２図は、
本発明に用いる脱離塔の加熱部の断面図である。
１……吸着塔、２……脱離塔、２Ａ……脱離塔
加熱部、３……SO2還元塔、４……硫黄凝縮器、
５……熱交換器、６……クラウス反応器、２０，
２２……ヘツダ、２４……熱交換器、２６……連
結パイプ。
Figure 1 is a system diagram of the dry desulfurization equipment, Figure 2 is:
FIG. 2 is a sectional view of a heating section of a desorption tower used in the present invention. 1... Adsorption tower, 2... Desorption tower, 2A... Desorption tower heating section, 3... SO 2 reduction tower, 4... Sulfur condenser,
5... Heat exchanger, 6... Claus reactor, 20,
22... Header, 24... Heat exchanger, 26... Connection pipe.
Claims (1)
塔内に硫黄酸化物を吸着した炭素質吸着剤を供給
し、間接加熱により前記吸着剤から硫黄酸化物を
脱離する方法において、熱交換器を通る高温ガス
の圧力を炭素質吸着剤側よりも負圧とし、かつ該
ガス中の酸素濃度を１％以下としたことを特徴と
する硫黄酸化物の脱離方法。 ２ 特許請求の範囲第１項において、熱交換器内
のガス圧が300mmH2O以下であることを特徴とす
る硫黄酸化物の脱離方法。[Claims] 1. A carbonaceous adsorbent adsorbing sulfur oxides is supplied into a desorption tower containing a heat exchanger through which high-temperature gas flows, and sulfur oxides are desorbed from the adsorbent by indirect heating. A method for desorption of sulfur oxides, characterized in that the pressure of the high-temperature gas passing through the heat exchanger is set to a negative pressure compared to the side of the carbonaceous adsorbent, and the oxygen concentration in the gas is set to 1% or less. . 2. The method for desorbing sulfur oxides according to claim 1, characterized in that the gas pressure within the heat exchanger is 300 mmH 2 O or less.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58002271A JPS59127630A (en) | 1983-01-12 | 1983-01-12 | Desorption of sulfur oxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58002271A JPS59127630A (en) | 1983-01-12 | 1983-01-12 | Desorption of sulfur oxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59127630A JPS59127630A (en) | 1984-07-23 |
| JPH0372333B2 true JPH0372333B2 (en) | 1991-11-18 |
Family
ID=11524703
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58002271A Granted JPS59127630A (en) | 1983-01-12 | 1983-01-12 | Desorption of sulfur oxide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59127630A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2843705B1 (en) * | 2002-08-21 | 2005-07-22 | Conservatoire Nat Arts | METHOD AND DEVICE FOR REGENERATING AN ADSORBENT |
| CN108509664A (en) * | 2017-02-24 | 2018-09-07 | 中国平煤神马能源化工集团有限责任公司 | It is a kind of based on negative pressure adjusted and controlled coal mine gas pumping method |
-
1983
- 1983-01-12 JP JP58002271A patent/JPS59127630A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59127630A (en) | 1984-07-23 |
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