JPS6015675B2 - How to eject light oil, etc. - Google Patents
How to eject light oil, etc.Info
- Publication number
- JPS6015675B2 JPS6015675B2 JP17871180A JP17871180A JPS6015675B2 JP S6015675 B2 JPS6015675 B2 JP S6015675B2 JP 17871180 A JP17871180 A JP 17871180A JP 17871180 A JP17871180 A JP 17871180A JP S6015675 B2 JPS6015675 B2 JP S6015675B2
- Authority
- JP
- Japan
- Prior art keywords
- oil
- light oil
- coke oven
- oven gas
- tower
- 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
Links
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 38
- 239000000571 coke Substances 0.000 claims description 29
- 238000010521 absorption reaction Methods 0.000 claims description 28
- 238000000034 method Methods 0.000 claims description 13
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims 1
- 239000003921 oil Substances 0.000 description 77
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- WHRZCXAVMTUTDD-UHFFFAOYSA-N 1h-furo[2,3-d]pyrimidin-2-one Chemical compound N1C(=O)N=C2OC=CC2=C1 WHRZCXAVMTUTDD-UHFFFAOYSA-N 0.000 description 1
- 235000006173 Larrea tridentata Nutrition 0.000 description 1
- 244000073231 Larrea tridentata Species 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000010692 aromatic oil Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229960002126 creosote Drugs 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003380 propellant Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 210000000689 upper leg Anatomy 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
【発明の詳細な説明】
本発明は、コークス炉ガス中の軽油分及びナフタリン分
を吸収油を用いて吸収し、該軽油分及びナフタリン分を
吸収油から回収する方法において、軽油分およびナフタ
リン分を除去したコークス炉ガスを用いて該吸収油から
軽油分等を駆出し、吸収油を再生する方法に関するもの
である。Detailed Description of the Invention The present invention provides a method for absorbing light oil and naphthalene in coke oven gas using absorbing oil and recovering the light oil and naphthalene from the absorbed oil. The present invention relates to a method for regenerating absorbed oil by ejecting light oil and the like from the absorbed oil using coke oven gas from which the coke oven gas has been removed.
コークス炉ガスから芳香族系化学品として重要な軽油分
（ベンゼン・トルェン・キシレン混合物）及びナフタリ
ン分を吸収油（クレオソート油、アントラセン油等の比
較的車質の芳香族系油の混合物）を循環吸収溶剤として
用いて吸収及び回収する方法は、製鉄業及び都市ガス工
業等のコークス炉ガス処理分野において以前から広く採
用されている。従来用いられているコークス炉ガス中の
軽油分及びナフタリン分等の吸収及び回収方法は、コー
クス炉ガスを吸収塔に導入し、該吸収塔で前記吸収油と
向流接触せしめて軽油分及びナフタリン分を吸収油に吸
収移行させ、此の吸収独（以下舎ペン吸収油という）を
加熱炉等で軽油分等を駆出するに必要な温度まで加熱し
、駆出塔の中段に供給し、同じく塔底に供給されて塔内
を上昇する駆出スチームとトレー上で向硫酸馳せしめて
軽油分及びナフタリン分を夫々塔頂留分及び側留分とし
て蟹出回収し軽油分等を駆出された吸収油（以下脱ペン
吸収油という）は搭底から抜き出されて前記吸収塔に戻
され循環再使用される方法が用いられている。以上の如
く、従来は駆出塔における駆出剤としてスチームが使用
されているが此のスチームによる駆出方法では、今日の
オイルショック以降のスチームのコストが非常に高い上
に運転状況によっては駆出塔内でスチームが凝縮しこれ
が駆出率の低下、回収ナフタリン分の純度低下及び舷出
塔内腐食の原因となるという欠点を有していた。又駆出
塔頂からの留出軽油分ペーパーは駆出スチームを含んで
いるため軽油コンデンサーでの冷却負荷が大きく、多量
の冷却水を必要とし、その上軽油分から静暦分離された
凝縮水はかなりの油分を含んでいるため公害防止の観点
から相当の処理が必要となる欠点も有していた。本発明
は以上の点に鑑みてなされたものであり従来のスチーム
による含ペン吸収油からの軽油分等の駆出方法の多くの
欠点を除き、同時に高価なスチームの使用を回避して経
済的な駆出塔の運転ができる方法を提供するものであっ
て、その要旨とするところは、コークス炉ガス中の軽油
分及びナフタリン分を吸収油を用いて吸収し、該吸収油
から該軽油分及びナフタリン分を駆出し回収し、該吸収
油を再生する軽油分等の回収方法において駆出剤として
吸収塔の塔頂から出た軽油分ならびにナフタリン分を除
去されたコークス炉ガスの一部を使用することを特徴と
する軽油分等の駆出方法である。Absorbs light oil (benzene, toluene, xylene mixture) and naphthalene, which are important aromatic chemicals, from coke oven gas (mixture of relatively high quality aromatic oils such as creosote oil and anthracene oil). The method of absorption and recovery using a circulating absorption solvent has been widely adopted in the field of coke oven gas processing such as the steel industry and the city gas industry. A conventional method for absorbing and recovering light oil and naphthalene from coke oven gas involves introducing the coke oven gas into an absorption tower, where it is brought into countercurrent contact with the absorbed oil to remove light oil and naphthalene. This absorbed oil (hereinafter referred to as pen absorption oil) is heated in a heating furnace to the temperature necessary to eject light oil, etc., and then supplied to the middle stage of the ejection tower. Similarly, the ejected steam that is supplied to the bottom of the column and rises inside the column is mixed with sulfuric acid on a tray, and the light oil and naphthalene components are recovered as an overhead fraction and a side fraction, respectively, and the light oil and other components are discharged. A method is used in which the absorbed oil (hereinafter referred to as depenned absorbed oil) is extracted from the bottom of the tower, returned to the absorption tower, and recycled for reuse. As mentioned above, steam has conventionally been used as the ejecting agent in ejecting towers, but with this method of ejection, the cost of steam is very high after today's oil crisis, and the ejection may be difficult depending on the operating conditions. This method has the disadvantage that steam condenses in the outgoing column, which causes a decrease in the ejection rate, a decrease in the purity of the recovered naphthalene, and corrosion in the outgoing column. In addition, since the distilled light oil paper from the top of the ejection tower contains ejected steam, the cooling load on the light oil condenser is large and a large amount of cooling water is required. Since it contains a considerable amount of oil, it also has the disadvantage of requiring considerable treatment from the viewpoint of pollution prevention. The present invention has been made in view of the above points, and eliminates many of the drawbacks of the conventional method of ejecting light oil components from pen-containing absorbed oil using steam, and at the same time avoids the use of expensive steam and is economical. The purpose of the present invention is to absorb light oil and naphthalene in coke oven gas using absorption oil, and extract the light oil from the absorption oil. A part of the coke oven gas from which the light oil and naphthalene components have been removed and the light oil components discharged from the top of the absorption tower are used as ejecting agents in a method for recovering light oil components, etc., in which the naphthalene components are ejected and recovered, and the absorbed oil is regenerated. This is a method for ejecting light oil, etc., which is characterized in that it is used.
以下実施例に基づき本発明について説明する。The present invention will be described below based on Examples.
第１図は本発明の方法の一実施例を示す系統図である。
軽油分及びナフタリン分を含んだコークス炉ガスＡは吸
収塔１の底部に入り、塔項より流下する脱ペン吸収油Ｄ
と向流接触し、軽油分及びナフタリン分は該吸収油中に
吸収補集される。FIG. 1 is a system diagram showing one embodiment of the method of the present invention.
Coke oven gas A containing light oil and naphthalene enters the bottom of absorption tower 1, and depened absorption oil D flows down from the tower section.
The light oil and naphthalene components are absorbed and collected in the absorbing oil.
吸収塔１の塔底部を出る該成分の濃度が濃くなった含ペ
ン吸収油Ｃは該軽油分等を回収し同時に吸収油を再生す
るために回収工程に送られる。含ペン吸収油Ｃは先ずオ
イル熱交２にて駆出塔５からの高温の脱ペン吸収油Ｄと
熱交換し予熱され脱水塔３に供給される。この脱水塔は
含ペン吸収渦中の水分を分離するために設置されるもの
である。該脱水塔３にて脱水された含ペン吸収油Ｃは更
に加熱炉４にて所定温度迄加熱し駆出塔５の中段に供Ｖ
給される。前記脱水塔３で分離した水分Ｅは駆出塔５の
塔頂部に供給される。腿出塔５の塔底部には駆出剤とし
て吸収塔１を出た軽油分及びナフタリン分を除かれたコ
ークス炉ガスＢの一部が袋入される。駆出塔５の塔内に
おいては加熱により吸収油中の軽油分の溶解度が小さく
なり同時に駆出剤の吹込により軽油分等の分圧が小さく
なるため沸点より低い温度で塔頂から軽油分のペーパー
と樋出用コークス炉ガスの混合物が留出してくる。塔頂
から留出した軽油分ペーパー及び駆出用コークス炉ガス
は気液分離のために軽油コンデンサー６に入り軽油分は
凝縮しコークス炉ガスから分離する。該軽油分を分離さ
れたコークス炉ガスＢ′は軽油コンデンサーに使用する
冷却水の温度により若干の軽油分を含むため此をそのま
ま吸収塔１を出たコークス炉ガスＢに戻す事はできない
。このため分離されたコークス炉ガス８は若干含まれて
いる軽油分等を回収するために再度前記吸収塔に戻しコ
ークス炉ガスＡに循環合流される。該凝縮分離した軽油
分はリフラックスドラム７に入り一部は駆出塔頂温度調
節用の還流液として駆出塔６の塔碩に戻され、残部は製
品軽油Ｆとして抜き出される。ナフタリン分Ｇは側留と
して鱗出塔の上段より抜き出される。駆出塔５の努底か
ら出る高温の脱ペン吸収油Ｄはオイル熱交２にて低温の
含ペン吸収油Ｃと熱交換し更にオイルクーラ−８にて所
定の温度まで冷却後、脱ペン吸収油○として吸収塔１の
塔頂に供給され循環再使用される。一方吸収塔１を出た
大部分のコークス炉ガスは次工程へ送り出される。The pen-containing absorbed oil C, which has a high concentration of components, leaving the bottom of the absorption tower 1 is sent to a recovery step to recover the light oil and the like and at the same time regenerate the absorbed oil. The penned absorption oil C is first preheated by exchanging heat with the high-temperature depenned absorption oil D from the ejection tower 5 in the oil heat exchanger 2, and then supplied to the dehydration tower 3. This dehydration tower is installed to separate the moisture in the pen-containing absorption vortex. The pen-containing absorbed oil C dehydrated in the dehydration tower 3 is further heated to a predetermined temperature in a heating furnace 4 and supplied to the middle stage of the ejection tower 5.
be provided. The water E separated in the dehydration tower 3 is supplied to the top of the ejection tower 5. A portion of the coke oven gas B from which the light oil and naphthalene components have been removed and which has exited the absorption tower 1 is placed in a bag as a propellant at the bottom of the thigh tower 5. In the expulsion tower 5, the solubility of the light oil in the absorbed oil decreases due to heating, and at the same time, the partial pressure of the light oil, etc. decreases due to the blowing of the ejector, so the light oil is removed from the top of the column at a temperature lower than the boiling point. A mixture of paper and coke oven gas is distilled out. The light oil paper distilled from the top of the tower and the coke oven gas for ejection enter the light oil condenser 6 for gas-liquid separation, and the light oil is condensed and separated from the coke oven gas. The coke oven gas B' from which the light oil content has been separated contains some light oil content depending on the temperature of the cooling water used in the light oil condenser, so it cannot be returned as it is to the coke oven gas B leaving the absorption tower 1. Therefore, the separated coke oven gas 8 is returned to the absorption tower again to be recycled and merged with the coke oven gas A in order to recover some light oil and the like contained therein. The condensed and separated light oil component enters the reflux drum 7, and a portion is returned to the bottom of the ejection column 6 as a reflux liquid for controlling the temperature at the top of the ejection column, and the remainder is extracted as a product light oil F. The naphthalene fraction G is extracted from the upper stage of the scale tower as a side stream. The high-temperature de-pentened absorption oil D discharged from the bottom of the ejection tower 5 exchanges heat with the low-temperature pen-containing absorption oil C in the oil heat exchanger 2, and is further cooled to a predetermined temperature in the oil cooler 8 before being de-penciled. It is supplied to the top of the absorption tower 1 as absorption oil ○ and is recycled and reused. On the other hand, most of the coke oven gas leaving the absorption tower 1 is sent to the next process.
以上説明した装置機成によりコークス炉ガス中の軽油分
及びナフタリン分を吸収ならびに回収すれば騒出塔内で
の水分凝縮等による軽油分等の駆出率低下及び回収ナフ
タリン分の純度低下等の種々のトラブルが防止され安定
した駆出塔の運転ができる上騒出塔内には凝縮水分がな
いので腐食を激減することができる。更に高価なスチー
ムを全く使用しないし、その上スチームを使用しないた
めに油分を含んだ凝縮水が出ないので公害防止のための
水処理設備が不用になり非常に経済的である。なお、本
発明の方法は前記実施例に限定されるものではなく、軽
油コンデンサーにて軽油分を凝縮分離されたコークス炉
ガスは軽油分が飽和しているため発熱量が高いのでその
まま高カロリー燃料として使用したり、又は軽油コンデ
ンサーに使用する冷却水の温度に依っては軽油コンデン
サーで軽油分を分離されたコークス炉ガスＢ′は再度前
記吸収塔に戻す事は醸しに、そのまま吸収塔１を出たコ
ークス炉ガスＢに合流する事もできる。By absorbing and recovering the light oil and naphthalene in the coke oven gas using the device configuration described above, there will be no reduction in the ejection rate of the light oil, etc. due to water condensation in the decoupling tower, and a reduction in the purity of the recovered naphthalene. Various troubles can be prevented and the ejection tower can be operated stably, and since there is no condensed water in the ejection tower, corrosion can be drastically reduced. Furthermore, it does not use expensive steam at all, and since it does not use steam, no condensed water containing oil is produced, so water treatment equipment for pollution prevention is not required, making it very economical. It should be noted that the method of the present invention is not limited to the above-described embodiments, and the coke oven gas from which light oil has been condensed and separated in a light oil condenser has a high calorific value because it is saturated with light oil, so it can be directly used as high-calorie fuel. Depending on the temperature of the cooling water used in the light oil condenser, the coke oven gas B' from which the light oil has been separated in the light oil condenser may not be returned to the absorption tower again, but may be sent to the absorption tower 1 as it is. It can also join the coke oven gas B that comes out.
あるいは第２の吸収塔を設け所定の温度まで冷却された
脱ペン吸収油によりコークス炉ガスＢ中の飽和した軽油
分を吸収補集し、該軽油分を除去されたコークス炉ガス
を吸収塔１の出口の下流点でコークス炉ガスＢに合流さ
せることもできる。Alternatively, a second absorption tower is provided, and the saturated light oil content in the coke oven gas B is absorbed and collected by depenned absorption oil cooled to a predetermined temperature, and the coke oven gas from which the light oil content has been removed is transferred to the absorption tower 1. It is also possible to join the coke oven gas B at a point downstream of the outlet of the coke oven gas B.
第１図は本発明の１実施例を示す系統図である。 FIG. 1 is a system diagram showing one embodiment of the present invention.
Claims (1)
油を用いて吸収し、該吸収油から該軽油分及びナフタリ
ン分を駆出し回収し、該吸収油を再生する軽油分等の回
収方法において、駆出剤として吸収塔の塔頂から出た軽
油分ならびにナフタリン分を除去されたコークス炉ガス
の１部を使用することを特徴とする軽油分等の駆出方法
。1. A method for recovering light oil, etc., in which the light oil and naphthalene in coke oven gas are absorbed using absorbing oil, the light oil and naphthalene are expelled and recovered from the absorbed oil, and the absorbed oil is regenerated, A method for expelling light oil, etc., characterized in that a part of the coke oven gas from which the light oil and naphthalene components have been removed, discharged from the top of an absorption tower, is used as a discharging agent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17871180A JPS6015675B2 (en) | 1980-12-19 | 1980-12-19 | How to eject light oil, etc. |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17871180A JPS6015675B2 (en) | 1980-12-19 | 1980-12-19 | How to eject light oil, etc. |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57102220A JPS57102220A (en) | 1982-06-25 |
| JPS6015675B2 true JPS6015675B2 (en) | 1985-04-20 |
Family
ID=16053221
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP17871180A Expired JPS6015675B2 (en) | 1980-12-19 | 1980-12-19 | How to eject light oil, etc. |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6015675B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100804232B1 (en) * | 2001-12-21 | 2008-02-18 | 재단법인 포항산업과학연구원 | Recovery of light oil and naphthalene in coke oven gas |
| JP2007116622A (en) * | 2005-10-24 | 2007-05-10 | Seiko Instruments Inc | Piezoelectric vibrator and method for manufacturing the same, surface mount type piezoelectric vibrator and method for manufacturing the same, oscillator, electronic device, and radio timepiece |
-
1980
- 1980-12-19 JP JP17871180A patent/JPS6015675B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57102220A (en) | 1982-06-25 |
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