JPH0140875B2 - - Google Patents
Info
- Publication number
- JPH0140875B2 JPH0140875B2 JP55008478A JP847880A JPH0140875B2 JP H0140875 B2 JPH0140875 B2 JP H0140875B2 JP 55008478 A JP55008478 A JP 55008478A JP 847880 A JP847880 A JP 847880A JP H0140875 B2 JPH0140875 B2 JP H0140875B2
- Authority
- JP
- Japan
- Prior art keywords
- tower
- absorption
- ammonia
- absorption liquid
- pressure
- 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
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 69
- 239000007789 gas Substances 0.000 claims description 56
- 238000010521 absorption reaction Methods 0.000 claims description 52
- 229910021529 ammonia Inorganic materials 0.000 claims description 32
- 239000007788 liquid Substances 0.000 claims description 29
- 230000002378 acidificating effect Effects 0.000 claims description 24
- 239000002351 wastewater Substances 0.000 claims description 19
- 238000000034 method Methods 0.000 claims description 14
- 239000000571 coke Substances 0.000 claims description 13
- 238000004519 manufacturing process Methods 0.000 claims description 12
- 238000000746 purification Methods 0.000 claims description 12
- 239000010842 industrial wastewater Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000011084 recovery Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 8
- 239000002253 acid Substances 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Landscapes
- Gas Separation By Absorption (AREA)
- Industrial Gases (AREA)
Description
【発明の詳細な説明】
本発明はコークス炉ガス中に含有される硫化水
素、シアン化水素、二酸化炭素等の酸性ガス、ア
ンモニアガス等の揮発性ガス成分を安定して除去
すると共に、上記のような揮発性ガス成分を含有
する工業廃水から該ガス成分を除去して工業廃水
を精製し、しかも、該工業廃水から除去された揮
発性ガス成分とコークス炉ガスから除去された揮
発性ガス成分とを集中的に且つ効率よく回収する
ことができる精製コークス炉ガスの製造方法に関
するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention stably removes acid gases such as hydrogen sulfide, hydrogen cyanide, and carbon dioxide, and volatile gas components such as ammonia gas contained in coke oven gas. Purifying industrial wastewater by removing gas components from industrial wastewater containing volatile gas components, and further, purifying the volatile gas components removed from the industrial wastewater and the volatile gas components removed from coke oven gas. The present invention relates to a method for producing purified coke oven gas that can be recovered intensively and efficiently.
室炉式コークス炉等によるコークス炉ガス製造
工場においては、製造されるコークス炉ガス（以
下、COGという。）中に硫化水素（H2S）、二酸
化炭素（CO2）、シアン化水素（HCN）、アンモ
ニア（NH3）等の揮発性ガス成分を含有するの
で、これらを除去して精製されたCOGを得る必
要がある。一方、コークス炉において製造される
COGの冷却洗浄等には多量の洗浄水が用いられ
るが、その廃水中にも上記のような揮発性ガス成
分が含まれている。 In a coke oven gas production plant using an indoor coke oven, hydrogen sulfide (H 2 S), carbon dioxide (CO 2 ), hydrogen cyanide (HCN), Since it contains volatile gas components such as ammonia (NH 3 ), these must be removed to obtain purified COG. On the other hand, produced in a coke oven
A large amount of cleaning water is used for cooling and cleaning COG, but the wastewater also contains volatile gas components such as those mentioned above.
このような揮発性ガス成分を含有する工業廃水
は、上記の例に限らず、各種工場設備、例えば、
火力発電所、アンモニア製造工場からの排ガス中
のCO2あるいはNH3を水で吸収除去する際等にも
多量排出される。これらの工業廃水はそのまま放
流すると水質汚染の原因になるので、揮発性ガス
成分を除去した後に放流する必要がある。 Industrial wastewater containing such volatile gas components is not limited to the above examples, but is also used in various factory equipment, such as
Large amounts are also emitted when CO 2 or NH 3 in exhaust gas from thermal power plants and ammonia manufacturing plants is absorbed and removed with water. If these industrial wastewaters are discharged as they are, they may cause water pollution, so it is necessary to remove volatile gas components before discharging them.
本出願人等は、COG中の揮発性ガス成分を除
去して精製COGを製造する方法として、粗COG
にアンモニア吸収液を向流接触させ、該COG中
に含まれる揮発性酸性ガス性分を吸収除去する吸
収工程、この酸性ガス成分を吸収した吸収液を加
熱することにより揮発性酸性ガス成分を分離して
再生したのち前記吸収液として循環使用する脱酸
工程、アンモニア及び／又は揮発性酸性ガス成分
を含有する工業廃水を脱酸工程の温度よりも高い
温度に加熱してNH3及び／又は揮発性酸性ガス
成分を含む高圧水蒸気を駆出する廃水精製工程の
各工程を含み、得られた高圧水蒸気を脱酸工程へ
導入する方法を先に提案した（特開昭53―145807
号公報）。 Applicants have proposed a method for producing purified COG by removing volatile gas components from COG.
An absorption process in which ammonia absorption liquid is brought into countercurrent contact with COG to absorb and remove volatile acidic gas components contained in the COG, and volatile acidic gas components are separated by heating the absorption liquid that has absorbed this acidic gas component. In the deoxidation step, the industrial wastewater containing ammonia and/or volatile acidic gas components is heated to a higher temperature than the temperature in the deoxidation step to evaporate NH 3 and/or volatile acid gas components. We have previously proposed a method that includes each step of the wastewater purification process in which high-pressure steam containing acidic gas components is ejected, and the resulting high-pressure steam is introduced into the deoxidation process (Japanese Patent Application Laid-Open No. 145807-1982).
Publication No.).
ところが、上記の方法では廃水精製工程が高
温、高圧であるため、該工程から排出される排出
水中のアンモニア濃度が高く、また操作エネルギ
ーの損失が大きく且つ耐圧容器を必要とするので
設備建設費及び運転経費が割高となる欠点があ
る。 However, in the above method, since the wastewater purification process is at high temperature and high pressure, the concentration of ammonia in the waste water discharged from the process is high, the loss of operating energy is large, and a pressure-resistant container is required, resulting in high equipment construction costs and high pressure. The disadvantage is that operating costs are relatively high.
そこで、本発明者等はこれら欠点の解消策につ
き種々検討を重ねた結果、廃水精製工程の熱作圧
力を低下させることにより、該工程から排出され
る処理水中のアンモニア濃度が低減できると共
に、該工程で消費する水蒸気量が削減できること
を見出し、本発明を完成した。 Therefore, the inventors of the present invention have repeatedly studied various measures to solve these drawbacks, and have found that by lowering the thermal operating pressure of the wastewater purification process, it is possible to reduce the ammonia concentration in the treated water discharged from the process, and to reduce the ammonia concentration in the treated water discharged from the process. They discovered that the amount of water vapor consumed in the process could be reduced and completed the present invention.
すなわち、本発明の要旨は、(A)吸収塔でCOG
とアンモニア吸収液とを向流接触させて、該
COC中の揮発性酸性ガス成分を吸収除去する吸
収工程、(B)前記吸収塔より導出される吸収液を、
塔頂部内の温度が40℃以下に保持される脱酸塔に
導入し、110〜160℃の温度に加熱することにより
該吸収液中の揮発性酸性ガス成分を実質的に分離
除去した後、前記吸収塔の吸収液として導入循環
する脱酸工程、(C)NH3及び／又は揮発性酸性ガ
ス成分を含有する工業廃水を、前記脱酸塔内圧力
よりも低い圧力下、90〜140℃の温度に加熱する
ことにより、該工業廃水中のNH3及び／又は揮
発性酸性ガス成分を含有する低圧水蒸気を駆出す
る廃水精製工程、(D)前記吸収工程を経たCOGか
らNH3を回収するアンモニア回収工程、の各工
程を含み、前記廃水精製工程から駆出される低圧
水蒸気の一部又は全部を、５Kg／cm2・Ｇ以上の圧
力を有する水蒸気で駆動されるエジエクターの吸
引口に導入し、前記脱酸塔内の圧力よりも高い圧
力に昇圧した後、脱酸塔内へ導入して吸収液に直
接接触させることを特徴とする精製COGの製造
方法に存する。 In other words, the gist of the present invention is (A) COG
and the ammonia absorption liquid are brought into countercurrent contact, and the
Absorption step of absorbing and removing volatile acidic gas components in COC, (B) absorbing liquid derived from the absorption tower,
After introducing the absorbent into a deoxidizing tower in which the temperature in the top of the tower is maintained at 40°C or lower and heating it to a temperature of 110 to 160°C, volatile acidic gas components in the absorption liquid are substantially separated and removed. In the deoxidation step, industrial wastewater containing (C) NH 3 and/or volatile acidic gas components is introduced and circulated as an absorption liquid in the absorption tower, and is heated at 90 to 140°C under a pressure lower than the internal pressure of the deoxidation tower. A wastewater purification step in which low-pressure steam containing NH 3 and/or volatile acid gas components is ejected from the industrial wastewater by heating to a temperature of (D) recovering NH 3 from COG that has undergone the absorption step. Ammonia recovery step, and a part or all of the low-pressure steam discharged from the wastewater purification step is introduced into the suction port of an ejector driven by steam having a pressure of 5 kg/cm 2 · G or more. The method for producing purified COG is characterized in that the pressure is raised to a higher pressure than the pressure inside the deoxidizing tower, and then the COG is introduced into the deoxidizing tower and brought into direct contact with the absorption liquid.
以下、本発明を添付図面と共に詳細に説明す
る。 Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.
第１図は本発明を実施する一例の系統図であ
る。 FIG. 1 is a system diagram of an example of implementing the present invention.
図中、Ａは揮発性酸性ガスの吸収工程であり、
アンモニア吸収液が上部より散液され、COGが
これに向流接触するような泡鐘塔、多孔板塔、充
填塔、スプレー塔等の吸収塔２より構成されてい
る。 In the figure, A is the absorption process of volatile acidic gas,
It consists of an absorption tower 2, such as a bubble tower, perforated plate tower, packed tower, or spray tower, in which an ammonia absorption liquid is dispersed from the top and COG is brought into countercurrent contact therewith.
Ｂは脱酸工程であり、前記吸収塔２から導出さ
れるアンモニア吸収液を加熱して揮発性酸性ガス
成分を分離する脱酸塔１２より構成されている。 B is a deoxidation step, which is comprised of a deoxidation tower 12 that heats the ammonia absorption liquid derived from the absorption tower 2 to separate volatile acidic gas components.
Ｃは廃水精製工程であり、アンモニア及び／又
は揮発性酸性ガス成分を含有する廃水を直接水蒸
気等の加熱によりアンモニア及び／又は揮発性酸
性ガス成分を駆出するストリツピング塔１５より
構成されている。 C is a wastewater purification process, which is comprised of a stripping column 15 that drives out ammonia and/or volatile acidic gas components by directly heating the wastewater containing ammonia and/or volatile acidic gas components with steam or the like.
ＤはCOG中のNH3の回収工程であり、COGか
らのアンモニア分離設備２８から構成されてい
る。 D is a recovery process for NH 3 in COG, and is comprised of ammonia separation equipment 28 from COG.
２６は前記脱酸塔１２から駆出される酸性ガス
成分を有用物質として回収する設備である。 26 is equipment for recovering the acidic gas components discharged from the deoxidizing tower 12 as useful substances.
コークス炉から発生したCOGはプライマリー
クーラーで冷却された後、導管１から吸収塔２へ
導入される。導入されたCOGは吸収塔２内を上
昇する間に、塔頂の導管３から導入され、好まし
くは複数段階で散布される30〜60℃のアンモニ吸
収液と向流接触し、H2S，CO2，HCN等の揮発
性酸性ガス成分が吸収除去される。アンモニア吸
収液中のアンモニア濃度は、吸収塔２内の温度を
調節することにより４〜10ｇ／に制御される。
揮発性酸性ガス成分を吸収したアンモニア吸収液
は、導管５を通して吸収塔２より導出され、脱酸
塔１２頂部への導管７と中間部へ導管９とを通し
てれぞれ脱酸塔１２へ分割導入される。脱酸塔１
２においては、塔頂部内の温度が40℃以下に保持
され、導入された吸収液はリボイラー１４等によ
り110〜160℃に加熱される。吸収液中の揮発性酸
性ガス成分は濃縮分離され、塔頂より導管２７を
通して駆出される。 COG generated from the coke oven is cooled in a primary cooler and then introduced into an absorption tower 2 through a conduit 1. While the introduced COG rises in the absorption tower 2, it comes into countercurrent contact with the ammonia absorption liquid at 30 to 60° C., which is introduced from the conduit 3 at the top of the tower and is preferably sprayed in multiple stages, to generate H 2 S, Volatile acid gas components such as CO 2 and HCN are absorbed and removed. The ammonia concentration in the ammonia absorption liquid is controlled to 4 to 10 g/by adjusting the temperature inside the absorption tower 2.
The ammonia absorption liquid that has absorbed volatile acidic gas components is led out from the absorption tower 2 through a conduit 5, and dividedly introduced into the deoxidation tower 12 through a conduit 7 to the top of the deoxidation tower 12 and a conduit 9 to the middle part of the deoxidation tower 12. be done. Deoxidizing tower 1
In step 2, the temperature inside the column top is maintained at 40°C or lower, and the introduced absorption liquid is heated to 110 to 160°C by the reboiler 14 or the like. The volatile acidic gas components in the absorption liquid are concentrated and separated, and are discharged from the top of the column through a conduit 27.
再生されたアンモニア吸収液は、塔底部より導
管１０を通して導出されたのち分割され、一部は
導管３を通して吸収塔２へ導入循環されると共
に、残部は導管１１を通して廃水精製工程Ｃのス
トリツピング塔１５へ導入される。また他の系か
らくるアンモニア及び／又は揮発性酸性ガス成分
を含有する工業廃水は、導管１７より導入され前
記アンモニア吸収液に混合される。また、ストリ
ツピング塔１５においては、脱酸塔１２における
圧力よりも低い圧力下、90〜140℃の温度に加熱
される。すなわち、脱酸塔１２内の圧力は、操作
温度110〜160℃に対応して約2.5〜約7.3Kg／cm2・
Ｇであるから、ストリツピング塔１５内の圧力は
７Kg／cm2・Ｇ以下であればよいが、常圧〜３Kg／
cm2・Ｇの範囲で実施するのが好ましい。ストリツ
ピング塔内の圧力は圧力制御弁２０により所定圧
に制御される。加熱により前記廃水中の揮発性ガ
ス成分は水蒸気と共に駆出される。揮発性ガス成
分を駆出して精製された廃水は、導管１９を通し
て活性汚泥廃水処理設備（図示せず）等に供給さ
れる。 The regenerated ammonia absorption liquid is led out from the bottom of the tower through conduit 10 and then divided. A part is introduced and circulated through conduit 3 to absorption tower 2, and the remainder is passed through conduit 11 to stripping tower 15 of wastewater purification process C. will be introduced to Further, industrial wastewater containing ammonia and/or volatile acid gas components coming from other systems is introduced through the conduit 17 and mixed with the ammonia absorption liquid. Further, in the stripping tower 15, the material is heated to a temperature of 90 to 140°C under a pressure lower than that in the deoxidizing tower 12. That is, the pressure inside the deoxidizing tower 12 is about 2.5 to about 7.3 Kg/cm 2 ·corresponding to the operating temperature of 110 to 160°C.
G, the pressure inside the stripping column 15 should be 7 kg/cm 2 ·G or less, but the pressure should be between normal pressure and 3 kg/cm 2 ·G.
It is preferable to carry out in the range of cm 2 ·G. The pressure inside the stripping column is controlled to a predetermined pressure by a pressure control valve 20. By heating, volatile gas components in the wastewater are driven out together with water vapor. The wastewater purified by removing volatile gas components is supplied to an activated sludge wastewater treatment facility (not shown) or the like through a conduit 19.
駆出された揮発性ガス成分を含んだ水蒸気は導
管２１を通してエジエクター２４の吸引口へ導入
し、導管２３より導入される５Kg／cm2・Ｇ上、好
ましくは７〜40Kg／cm2・Ｇの高圧水蒸気により、
脱酸塔１２における圧力よりも高い圧力に昇圧し
た後、導管２５を通して脱酸塔１２内へ導入され
る。導管２５内の圧力は流量制御弁２２により所
定圧に制御される。脱酸塔１２内へ導入された揮
発性ガス成分を含んだ高圧蒸気は、ここで吸収液
と直接接触して、該吸収液の加熱に供されると共
に、含有する揮発性ガス成分のうち揮発性酸性ガ
ス成分が分離されて、前記吸収液から分離された
揮発性酸性ガス成分と共に脱酸塔頂部より導管２
７を通して駆出される。一方、水蒸気とNH3は
吸収液中に移行し、脱酸塔底部より導管１０を通
して抜出され、その一部は導管３を通して吸収塔
２へ導入され、他の一部は導管１１を通して再び
ストリツピング塔１５へ循環される。 The ejected steam containing volatile gas components is introduced into the suction port of the ejector 24 through the conduit 21, and is introduced from the conduit 23 at a rate of 5 kg/cm 2 ·G, preferably 7 to 40 kg/cm 2 ·G. By high pressure steam,
After increasing the pressure to a higher pressure than the pressure in the deoxidizing tower 12, it is introduced into the deoxidizing tower 12 through the conduit 25. The pressure within the conduit 25 is controlled to a predetermined pressure by the flow control valve 22. The high-pressure steam containing volatile gas components introduced into the deoxidizing tower 12 comes into direct contact with the absorption liquid, heats the absorption liquid, and removes the volatile gas components contained therein. The volatile acidic gas component is separated, and the volatile acidic gas component separated from the absorption liquid is passed from the top of the deoxidation tower to the conduit 2.
It is ejected through 7. On the other hand, water vapor and NH 3 move into the absorption liquid and are extracted from the bottom of the deoxidizing tower through conduit 10, part of which is introduced into absorption tower 2 through conduit 3, and the other part is stripped again through conduit 11. It is recycled to column 15.
脱酸塔１２から駆出され、濃縮された揮発性酸
性ガス成分は、酸性ガス成分回収設備２６へ導入
され有用物質として回収される。回収設備２６と
しては、希硫酸製造設備、硫安製造設備、石膏製
造設備あるいはクラウス炉のような単体硫黄製造
設備等が採用される。 The volatile acidic gas component discharged from the deoxidizing tower 12 and concentrated is introduced into the acidic gas component recovery equipment 26 and recovered as a useful substance. As the recovery equipment 26, dilute sulfuric acid manufacturing equipment, ammonium sulfate manufacturing equipment, gypsum manufacturing equipment, or elemental sulfur manufacturing equipment such as a Claus furnace is employed.
吸収塔２を経て揮発性酸性ガス成分が除去され
たCOGは、アンモニア回収設備２８へ導入され、
ここでNH3が回収される。 The COG from which volatile acidic gas components have been removed through the absorption tower 2 is introduced into the ammonia recovery equipment 28,
Here NH3 is recovered.
１３，１６は加熱用蒸気導管、８，１８は熱交
換器、４，６は冷却器である。 13 and 16 are heating steam conduits, 8 and 18 are heat exchangers, and 4 and 6 are coolers.
なお、前述の例では脱酸塔から導出された吸収
液の一部をストリツピング塔へ導入しているが、
吸収塔から導出される吸収液の一部をストリツピ
ング塔へ導入することもできる。 In addition, in the above example, a part of the absorption liquid derived from the deoxidizing tower is introduced into the stripping tower,
A portion of the absorption liquid discharged from the absorption tower can also be introduced into the stripping tower.
以上詳述したように、本発明では廃水精製工程
の圧力が低いので、該廃水中に含有されるNH3
又はアンモニア及び酸性ガス成分の除去率が高
く、また耐圧容器を必要としない利点があり、さ
らに、廃水精製工程の加熱温度が低く、かつ余剰
熱エネルギーを脱酸工程の熱源としているので、
熱エネルギー効率が極めて高いという効果がある
から、精製コークス炉ガスの製造方法として有用
である。 As detailed above, in the present invention, since the pressure in the wastewater purification process is low, the NH3 contained in the wastewater is
Alternatively, it has the advantage of having a high removal rate of ammonia and acidic gas components, and does not require a pressure-resistant container, and furthermore, the heating temperature in the wastewater purification process is low, and surplus thermal energy is used as the heat source for the deoxidation process.
Since it has the effect of extremely high thermal energy efficiency, it is useful as a method for producing purified coke oven gas.
たとえば、本発明方法により、ストリツプ塔内
の圧力を1.1Kg／cm2Ｇ（温度約100℃）とした場合、
理論段数15段、アンモニア濃度：入口5100ppm、
出口250ppmpmで、ストリツプ用蒸気原単位は、
８Kg／廃水m3削減できる。 For example, when the pressure inside the strip column is set to 1.1 Kg/cm 2 G (temperature about 100°C) using the method of the present invention,
Number of theoretical plates: 15, ammonia concentration: inlet 5100ppm,
At an outlet of 250pppm, the steam consumption for strips is:
8kg/ m3 of wastewater can be reduced.
第１図は本発明の一実施態様を示す系統図であ
る。
Ａ：吸収工程、Ｂ：脱酸工程、Ｃ：廃水精製工
程、Ｄ：アンモニア回収工程、２：吸収塔、１
２：脱酸塔、１５：ストリツピング塔、２４：エ
ジエクター、２６：酸性ガス成分回収設備、２
８：アンモニア回収設備。
FIG. 1 is a system diagram showing one embodiment of the present invention. A: Absorption process, B: Deoxidation process, C: Wastewater purification process, D: Ammonia recovery process, 2: Absorption tower, 1
2: Deoxidizing tower, 15: Stripping tower, 24: Ejector, 26: Acid gas component recovery equipment, 2
8: Ammonia recovery equipment.
Claims (1)
液とを向流接触させて、該コークス炉ガス中の
揮発性酸性ガス成分を吸収除去する吸収工程、 (B) 前記吸収塔より導出される吸収液を、塔頂部
内の温度が40℃以下に保持される脱酸塔に導入
し、110〜160℃の温度に加熱することにより該
吸収液中の揮発性酸性ガス成分を実質的に分離
除去した後、前記吸収塔の吸収液として導入循
環する脱酸工程、 (C) アンモニア及び／又は揮発性酸性ガス成分を
含有する工業廃水を、前記脱酸塔内圧力よりも
低い圧力下、90〜140℃の温度に加熱すること
により、該工業廃水中のアンモニア及び／又は
揮発性酸性ガス成分を含有する低圧水蒸気を駆
出する廃水精製工程、 (D) 前記吸収工程を経たコークス炉ガスからアン
モニアを回収するアンモニア回収工程、 の各工程を含み、前記廃水精製工程から駆出さ
れる水蒸気の一部又は全部を、５Kg／cm2・Ｇ以
上の圧力を有する水蒸気で駆動されるエジエク
ターの吸引口に導入し、前記脱酸塔内の圧力よ
りも高い圧力に昇圧した後、脱酸塔内へ導入し
て吸収液に直接接触させることを特徴とする精
製コークス炉ガスの製造方法。 ２ 工業廃水が、吸収塔底部から導出されるアン
モニア吸収液の一部及び／又は脱酸塔底部から導
出されるアンモニア吸収液の一部であることを特
徴とする、特許請求の範囲第１項記載の精製コー
クス炉ガスの製造方法。[Scope of Claims] 1(A) An absorption step of bringing coke oven gas and ammonia absorption liquid into countercurrent contact in an absorption tower to absorb and remove volatile acidic gas components in the coke oven gas, (B) the above-mentioned The absorption liquid discharged from the absorption tower is introduced into a deoxidation tower in which the temperature inside the tower top is maintained at 40°C or lower, and volatile acidic gases in the absorption liquid are removed by heating to a temperature of 110 to 160°C. (C) a deoxidation step in which the components are substantially separated and removed and then introduced and recycled as an absorption liquid in the absorption tower; (D) a wastewater purification step in which low-pressure steam containing ammonia and/or volatile acidic gas components is ejected from the industrial wastewater by heating to a temperature of 90 to 140°C under a low pressure; (D) the absorption step; an ammonia recovery step in which ammonia is recovered from coke oven gas that has passed through the process, and a part or all of the water vapor ejected from the wastewater purification step is driven by water vapor having a pressure of 5 kg/cm 2 G or more. The refined coke oven gas is introduced into the suction port of the eductor to be heated to a pressure higher than that in the deoxidizing tower, and then introduced into the deoxidizing tower to directly contact the absorption liquid. Production method. 2. Claim 1, characterized in that the industrial wastewater is a part of the ammonia absorption liquid derived from the bottom of the absorption tower and/or a part of the ammonia absorption liquid derived from the bottom of the deoxidation tower. The method for producing purified coke oven gas as described.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP847880A JPS56104994A (en) | 1980-01-28 | 1980-01-28 | Production of purified coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP847880A JPS56104994A (en) | 1980-01-28 | 1980-01-28 | Production of purified coke oven gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56104994A JPS56104994A (en) | 1981-08-21 |
| JPH0140875B2 true JPH0140875B2 (en) | 1989-08-31 |
Family
ID=11694212
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP847880A Granted JPS56104994A (en) | 1980-01-28 | 1980-01-28 | Production of purified coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS56104994A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0198694A (en) * | 1987-10-12 | 1989-04-17 | Mitsubishi Kakoki Kaisha Ltd | Method of conducting optimized control of desulfurization of coke oven gas |
| JP2006232904A (en) * | 2005-02-23 | 2006-09-07 | Hitachi Ltd | Gas refining method for coal gasification system |
| EP2014347A1 (en) * | 2007-07-03 | 2009-01-14 | ALSTOM Technology Ltd | Removal of carbon dioxide from flue gas |
| JP5501730B2 (en) * | 2009-10-22 | 2014-05-28 | 三菱重工業株式会社 | Ammonia recovery device and recovery method |
| JP5751892B2 (en) * | 2011-03-31 | 2015-07-22 | 日揮株式会社 | Gas processing method and gas processing apparatus |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53145807A (en) * | 1977-05-25 | 1978-12-19 | Mitsubishi Chem Ind Ltd | Production of purified coke oven gas |
-
1980
- 1980-01-28 JP JP847880A patent/JPS56104994A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53145807A (en) * | 1977-05-25 | 1978-12-19 | Mitsubishi Chem Ind Ltd | Production of purified coke oven gas |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56104994A (en) | 1981-08-21 |
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