JPH0214083B2 - - Google Patents
Info
- Publication number
- JPH0214083B2 JPH0214083B2 JP56157452A JP15745281A JPH0214083B2 JP H0214083 B2 JPH0214083 B2 JP H0214083B2 JP 56157452 A JP56157452 A JP 56157452A JP 15745281 A JP15745281 A JP 15745281A JP H0214083 B2 JPH0214083 B2 JP H0214083B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- sulfur
- claus reactor
- temperature
- claus
- 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
Links
- 239000007789 gas Substances 0.000 claims description 29
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 22
- 238000006477 desulfuration reaction Methods 0.000 claims description 11
- 230000023556 desulfurization Effects 0.000 claims description 11
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 10
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 claims description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 description 16
- 239000011593 sulfur Substances 0.000 description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000003795 desorption Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 3
- 229910052815 sulfur oxide Inorganic materials 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Description
【発明の詳細な説明】
本発明は乾式脱硫装置に係り、特にクラウス反
応器を用いて単体硫黄を回収する乾式脱硫装置に
関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a dry desulfurization apparatus, and more particularly to a dry desulfurization apparatus for recovering elemental sulfur using a Claus reactor.
排ガス中の硫黄酸化物を活性炭のような吸着剤
に吸着後脱離させ、さらに該硫黄酸化物を還元し
て得た単体硫黄を凝縮分離し、さらに残りのガス
を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、石灰石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、その熱の有効利用が問題となる。 The sulfur oxides in the exhaust gas are adsorbed onto an adsorbent such as activated carbon and then desorbed, the sulfur oxides are further reduced to condense and separate the elemental sulfur, and the remaining gas is subjected to the Claus reaction to produce elemental sulfur. Compared to wet desulfurization equipment that uses limestone slurry, dry desulfurization equipment that recovers carbon dioxide does not require large amounts of water, does not require reheating of flue gas after desulfurization treatment, and does not generate waste water. It has advantages and is attracting attention. However, in such a desulfurization apparatus, high-temperature operation is required in the sulfur dioxide desorption tower, reduction tower, etc., and effective use of the heat becomes a problem.
すなわち、第１図は、従来の典型的な乾式脱硫
装置の系統図であるが、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、活性炭により脱硫される。次いでSO2
を吸着した活性炭は脱離塔２に供給され、ここで
導管１３から導入された脱離用加熱用ガスにより
加熱され、SO2分を脱離して活性炭が再生され
る。再生活性炭は、冷却水の流通する導管１２に
より冷却され、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
る炭素分と約500〜800℃で反応し、硫黄ガスおよ
び硫化水素と末反応のSO2ガス、また一部が硫化
カニボニルになり、硫黄ガスは硫黄凝縮器４で
120〜170℃に冷却されて回収され、硫化水素、硫
化カルボニルおよびSO2ガスはクラウス反応器６
で約200〜300℃の温度で硫黄に変換され、硫黄凝
縮器４でさらに硫黄が回収される。 That is, FIG. 1 is a system diagram of a typical conventional dry desulfurization apparatus, in which exhaust gas containing sulfur oxides (typically SO 2 ) is passed through a conduit 8 to an adsorption tower 1.
and is desulfurized using activated carbon. then SO 2
The activated carbon adsorbed is supplied to the desorption tower 2, where it is heated by the desorption heating gas introduced from the conduit 13, and the activated carbon is regenerated by desorbing SO2 . The regenerated activated carbon is cooled by a conduit 12 through which cooling water flows, and then circulated to the adsorption tower 1 again. The desorbed SO 2 gas reacts with carbon, which is a reducing agent, at approximately 500 to 800°C in the SO 2 reduction tower 3, and is converted into sulfur gas, hydrogen sulfide, and final reacted SO 2 gas, and a portion of which is converted to canibonyl sulfide. , the sulfur gas is sent to the sulfur condenser 4.
The hydrogen sulfide, carbonyl sulfide and SO2 gas are cooled to 120-170℃ and collected in the Claus reactor 6.
The sulfur is converted into sulfur at a temperature of about 200 to 300°C, and further sulfur is recovered in the sulfur condenser 4.
ここで、クラウス反応器での反応は一般に次式
で示される。 Here, the reaction in the Claus reactor is generally expressed by the following formula.
COS＋H2O→H2S＋CO2
2H2S＋SO2→3S＋2H2O
上式で生成される硫黄は、温度などの条件によ
りS2〜S8などの形態をとるが、クラウス反応器６
を含むそれ以後の部分ではクラウス反応の進行に
ともなつて硫黄ガスの濃度が上昇し、硫黄が一部
凝縮して液体硫黄ミストとなり、クラウス触媒や
装置、配管等に固着し、これらを閉塞させる原因
となる。 COS + H 2 O → H 2 S + CO 2 2H 2 S + SO 2 → 3S + 2H 2 O The sulfur produced in the above equation takes the form of S 2 to S 8 depending on conditions such as temperature,
As the Claus reaction progresses, the concentration of sulfur gas increases in the subsequent part containing the Claus reaction, and some of the sulfur condenses into liquid sulfur mist, which sticks to the Claus catalyst, equipment, piping, etc., and blocks them. Cause.
このため、従来はクラウス反応器６の前段に加
熱器（熱交換器）５を設置し、クラウス反応器出
口の硫黄分の濃度に合つた気体―液体の平衡温度
（平衡組成での温度）の＋20〜＋60℃以上に加熱
していたが、このような従来装置では、特別な加
熱器が必要であるばかりでなく、そのための外部
熱源を必要とするという欠点がある。 For this reason, conventionally, a heater (heat exchanger) 5 is installed before the Claus reactor 6, and the gas-liquid equilibrium temperature (temperature at equilibrium composition) is adjusted to match the sulfur concentration at the outlet of the Claus reactor. However, such conventional devices have the disadvantage that they not only require a special heater but also an external heat source for this purpose.
本発明の目的は、上記した従来技術の欠点をな
くし、特別な加熱器や熱源を必要とすることな
く、クラウス反応器入口のガス温度を所要範囲に
調整することができる乾式脱硫装置提供すること
にある。 An object of the present invention is to provide a dry desulfurization device that eliminates the drawbacks of the prior art described above and can adjust the gas temperature at the inlet of a Claus reactor to a required range without requiring a special heater or heat source. It is in.
本発明は、クラウス反応器入口の所要温度に見
合うように、SO2還元塔出口ガス（例えば約500
〜800℃）を、直接クラウス反応器入口に供給し、
温度を調整しようとするものである。すなわち、
本発明装置は、クラウス反応器の入口ガスにSO2
還元塔の出口ガスを混入する配管系と、クラウス
反応器の温度が所要範囲になるように前記混合ガ
ス量を調整する制御系統を設けたことを特徴とす
る。 The present invention provides a method for reducing SO 2 reduction column outlet gas (e.g., about 500
~800℃) directly to the inlet of the Claus reactor,
It attempts to regulate the temperature. That is,
The device of the present invention supplies SO 2 to the inlet gas of the Claus reactor.
The present invention is characterized by providing a piping system for mixing the outlet gas of the reduction tower and a control system for adjusting the amount of the mixed gas so that the temperature of the Claus reactor falls within a required range.
以下、本発明を図面により詳細に説明する。 Hereinafter, the present invention will be explained in detail with reference to the drawings.
第２図は、本発明の乾式脱硫装置の一実施例を
示す系統図である。第１図の従来装置と異なる点
は、従来の加熱器５をなくし、SO2還元塔３の出
口ガスを直接クラウス反応器６および６Ａに供給
するための導管２５および２６を設け、かつその
供給量を調節するために弁３０および３１を設け
たことである。クラウス反応器６入口のガス温度
を調節するには、ガス温度に応じてSO2還元塔３
の出口ガスを導管２５または２６を介して導管１
８または２１に供給すればよいが、具体的には、
クラウス反応器５，５Ａ入口のガス温度を検出
し、これらの温度が所定値になるように弁３０，
３１の開度を調節する。この場合、温度検出器は
導管１８，２１またはクラウス反応器５，５Ａ内
のいずれに設けてもよい。なお、硫黄の回収率を
高める観点から、SO2還元塔３出口のガス中の
H2SとSO2の比は２：１に調整されていることが
好ましい。なお、最終段の硫黄凝縮器４を出た残
存硫黄を含む排ガスは酸化物７で酸化された後、
導管２４を経て吸着塔１への排ガス供給管８に循
環される。 FIG. 2 is a system diagram showing an embodiment of the dry desulfurization apparatus of the present invention. The difference from the conventional apparatus shown in FIG. 1 is that the conventional heater 5 is eliminated, and conduits 25 and 26 are provided for directly supplying the outlet gas of the SO 2 reduction column 3 to the Claus reactors 6 and 6A, and Valves 30 and 31 are provided to adjust the amount. To adjust the gas temperature at the inlet of the Claus reactor 6, the SO 2 reduction tower 3 is added according to the gas temperature.
The outlet gas is passed through conduit 25 or 26 to conduit 1
8 or 21, specifically,
The gas temperature at the inlet of the Claus reactor 5, 5A is detected, and the valve 30,
Adjust the opening degree of 31. In this case, the temperature detector may be provided either in the conduits 18, 21 or in the Claus reactors 5, 5A. In addition, from the viewpoint of increasing the sulfur recovery rate, the amount of gas in the SO 2 reduction tower 3 outlet is
Preferably, the ratio of H 2 S and SO 2 is adjusted to 2:1. In addition, after the exhaust gas containing residual sulfur that exits the final stage sulfur condenser 4 is oxidized with oxide 7,
It is circulated via the conduit 24 to the exhaust gas supply pipe 8 to the adsorption tower 1 .
以上、本発明によれば、特別な加熱器および外
部熱源を要することなく、従来装置の簡単な変更
により、クラウス反応器の入口ガスを所要の温度
に制御することができる。 As described above, according to the present invention, the temperature of the inlet gas of the Claus reactor can be controlled to a desired temperature by simple modification of the conventional device without requiring a special heater or external heat source.
第１図および第２図は、それぞれ従来装置およ
び本発明装置の実施例を示す系統図である。
１……吸着塔、２……脱離塔、３……SO2還元
塔、４……硫黄凝縮器、５……加熱器、６，６Ａ
……クラウス反応器、２５，２６……導管、３
０，３１……弁。
FIG. 1 and FIG. 2 are system diagrams showing a conventional device and an embodiment of the present invention device, respectively. 1... Adsorption tower, 2... Desorption tower, 3... SO 2 reduction tower, 4... Sulfur condenser, 5... Heater, 6,6A
... Claus reactor, 25, 26 ... Conduit, 3
0,31...Valve.
Claims (1)
から単体硫黄を凝縮分離した後、クラウス反応器
でガス中の硫化カルボニル、硫化水素および二酸
化硫黄を反応させてさらに単体硫黄を回収する乾
式脱硫装置において、前記クラウス反応器の入口
ガスに前記還元塔の出口ガスを混合する配管系
と、該混合ガス量により前記クラウス反応器の温
度を調整する制御系統とを設けたことを特徴とす
る乾式脱硫装置。1 A dry desulfurization device that condenses and separates elemental sulfur from the elemental sulfur-containing gas that exits the sulfur dioxide reduction tower, and then reacts carbonyl sulfide, hydrogen sulfide, and sulfur dioxide in the gas in a Claus reactor to recover elemental sulfur. Dry desulfurization, characterized in that it is provided with a piping system for mixing the outlet gas of the reduction tower with the inlet gas of the Claus reactor, and a control system for adjusting the temperature of the Claus reactor according to the amount of the mixed gas. Device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56157452A JPS5858133A (en) | 1981-10-05 | 1981-10-05 | Dry desulfurization apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56157452A JPS5858133A (en) | 1981-10-05 | 1981-10-05 | Dry desulfurization apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5858133A JPS5858133A (en) | 1983-04-06 |
| JPH0214083B2 true JPH0214083B2 (en) | 1990-04-06 |
Family
ID=15649962
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP56157452A Granted JPS5858133A (en) | 1981-10-05 | 1981-10-05 | Dry desulfurization apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5858133A (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5645743A (en) * | 1979-09-20 | 1981-04-25 | Hitachi Ltd | Exhaust gas desulfurization equipment using carbonaceous adsorbent |
-
1981
- 1981-10-05 JP JP56157452A patent/JPS5858133A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5645743A (en) * | 1979-09-20 | 1981-04-25 | Hitachi Ltd | Exhaust gas desulfurization equipment using carbonaceous adsorbent |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5858133A (en) | 1983-04-06 |
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