JPS5864214A - Recovering method for ammonia - Google Patents
Recovering method for ammoniaInfo
- Publication number
- JPS5864214A JPS5864214A JP56160471A JP16047181A JPS5864214A JP S5864214 A JPS5864214 A JP S5864214A JP 56160471 A JP56160471 A JP 56160471A JP 16047181 A JP16047181 A JP 16047181A JP S5864214 A JPS5864214 A JP S5864214A
- Authority
- JP
- Japan
- Prior art keywords
- soln
- tank
- tower
- absorption liquid
- ammonia
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Activated Sludge Processes (AREA)
- Industrial Gases (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、コークス炉で発生するＣＯＯ中のアンモニア
を回収するアンモニア回収方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an ammonia recovery method for recovering ammonia in COO generated in a coke oven.
この種のアンモニア回収方法は、吸収塔でＣＯＧ中のア
ｙｘｅ：ｊ−アを燐酸吸収液（燐酸１アンそニウム、
Ｎ）ｉ、Ｈ，ＰＯ，）に吸収させた後。This type of ammonia recovery method uses a phosphoric acid absorption liquid (1 amsonium phosphate,
N) i, H, PO, ) after absorption.
この吸収液を蒸留塔に尋いて、アンモニア分を蒸留し良
にこれを精留塔で精留する。一方アンそニア分を分離し
た吸収液は吸収塔に戻されて循環使用される。この場合
秋収液にはアンモニアとともにＣＯＧ中のタール、ダス
ト、炭化水素類の不純物、Ｈ，８，ＨＣＮ、ＣＯ，など
の酸性ガスが瞼収される。従来のアンモニア回収装置は
、これらの＊ｍガスをコンダクタ−にて排除し、さらに
精留時に苛性ソーダー１−添加して酸性ガスの一部を排
除し、不純物の堆積防止を図っている。しかしこの回収
方法では、較収液がｌｌｗＩするクローズド系であるた
め堀の＃縮。This absorption liquid is sent to a distillation column, and the ammonia content is distilled off, and then this is rectified in a rectification column. On the other hand, the absorption liquid from which the anthonia component has been separated is returned to the absorption tower and recycled. In this case, the autumn harvest liquid contains ammonia as well as impurities such as tar, dust, and hydrocarbons in COG, and acid gases such as H, 8, HCN, and CO. In conventional ammonia recovery equipment, these *m gases are removed by a conductor, and caustic soda is added during rectification to remove a portion of the acid gas, thereby preventing the accumulation of impurities. However, in this collection method, the calibrator is a closed system in which the calibrator is llwI, so the moat is #shrinked.
不純物の蓄積が起り、その結果設備とくに精留塔が腐食
し、熱交換器等が閉塞するなどのＦ！’１題がある。ま
た不純物を蓄積した液は、ＣＯＯが高くそのままでは放
橢することができない問題もある。Accumulation of impurities occurs, resulting in corrosion of equipment, especially rectification towers, and blockage of heat exchangers, etc.F! 'There is one problem. There is also the problem that the liquid with accumulated impurities has a high COO and cannot be left alone.
本発明看は１級収液の処理につき研究の結果活性汚泥処
理に着目した７すなわち、コークス炉から発生する安水
は、不純物を含むため、Ｗ用物質を分離回収後、活性汚
泥処理、凝集沈殿処理し、ｌＫに活性炭で処理して放漬
している。The present invention focuses on activated sludge treatment as a result of research on the treatment of first class liquid.7 Namely, ammonium water generated from coke ovens contains impurities, so after separating and recovering the W material, activated sludge treatment and flocculation are conducted. It is precipitated, treated with activated carbon at 1K, and left to soak.
この活性汚泥処理は、バクテリアにより液を浄化してＣ
ＯＯを減少させるもので、バクテリアの栄養源として燐
酸を用いている。This activated sludge treatment uses bacteria to purify the liquid and
It reduces OO and uses phosphoric acid as a food source for bacteria.
本発明は、この点に着目してなされたもので。The present invention has been made with attention to this point.
その目的とするところは、系内を循環する吸収液の一部
を活性汚泥処理におけるバクテリアの栄養源として利用
し、その分の新液を系内に補給することにより、不純物
の蓄積を防止し、もって設備の腐食、不純物による管路
の閉塞をそれぞれ防止することができるアンモニア回収
方法な得んとするものである。The purpose of this is to use part of the absorption liquid circulating in the system as a nutrient source for bacteria in activated sludge treatment, and to replenish that amount of new liquid into the system, thereby preventing the accumulation of impurities. The present invention provides an ammonia recovery method that can prevent corrosion of equipment and blockage of pipes due to impurities.
すなわち本発明は、コークス炉で発生するＣ０Ｇｖ秋収
塔に導入してそのアンモニア分を燐酸吸収液で吸収した
後、該吸収液を蒸留塔に導入しアンそニア分を蒸留する
とともに吸収液を上記吸収塔に戻し、更に蒸留したアン
モニア分を精留塔で精留する。アンモニア回収方法にお
いて、上記吸収塔と蒸留塔との間を循環する吸収液の一
部を活性汚泥処理槽に導入して、該吸収液を活性汚泥処
理におけるバクテリアの栄養源とするとともに、活性汚
泥処理槽に入れた吸収液と等量の吸収液を補給すること
を特徴とするアンモニア回収方法である。That is, the present invention introduces COGv generated in a coke oven into a fall collection column, absorbs the ammonia content with a phosphoric acid absorption liquid, and then introduces the absorption liquid into a distillation column to distill the anthonia content and absorb the absorption liquid. The ammonia is returned to the absorption tower, and the distilled ammonia is further rectified in a rectification tower. In the ammonia recovery method, a part of the absorption liquid circulating between the absorption tower and the distillation tower is introduced into the activated sludge treatment tank, and the absorption liquid is used as a nutrient source for bacteria in the activated sludge treatment. This is an ammonia recovery method characterized by replenishing an equal amount of absorption liquid to the absorption liquid put into a processing tank.
以下本発明をＳ画を参Ｍ１７て説明する。The present invention will be explained below with reference to the S picture M17.
第１閃はアンモニア回収方法の系統図である、この回収
方法では、吸収塔ｌ内にＣＯａを余剰安水とともに導入
し、ＣＯＯ中のアンモニア分を燐酸吸収液２に吸収させ
る。この吸収液２は例えば３０１１燐酸水溶液である。The first picture is a system diagram of an ammonia recovery method. In this recovery method, COa is introduced into the absorption tower 1 together with surplus ammonium water, and the ammonia content in the COO is absorbed into the phosphoric acid absorption liquid 2. This absorption liquid 2 is, for example, a 3011 phosphoric acid aqueous solution.
この吸収液１は、デビュレータＩにより浄化された後リ
ッチ液タンク４に入り、ここから熱交換＠Ｓ、コンタク
タＩＩを経て蒸留塔プンデン＋１から蒸留塔１に導かれ
る。蒸留塔８ではスチーム−によりアンモニア分が蒸留
され、アンモニア分を分離した吸収液は熱交換５ｉｚｖ
経て吸収塔１に戻される。一方アンモニア分は、蒸留塔
コンデンサ１で凝縮された後精留塔ブイードタンク１０
に溜められる。このフイー−ドタｙり１０に苛性ソーダ
−１１を添加して酸性ガスの一部を排除し。After being purified by the debutator I, the absorbent liquid 1 enters the rich liquid tank 4, and is guided from there to the distillation column 1 from the distillation column Punden+1 via a heat exchange @S and a contactor II. In the distillation column 8, the ammonia content is distilled using steam, and the absorption liquid from which the ammonia content has been separated is subjected to heat exchange 5izv.
After that, it is returned to the absorption tower 1. On the other hand, the ammonia content is condensed in the distillation column condenser 1 and then transferred to the rectification column buid tank 10.
It is stored in Caustic soda 11 was added to this feed tank 10 to remove part of the acid gas.
不純物の堆積を防止するつ次いでフィードタンク１０内
のアンモニア分を精留塔１２に導き。The ammonia content in the feed tank 10 is then led to the rectification column 12 to prevent the accumulation of impurities.
精留する。rectify.
しかしてこの装置では、吸収塔１からデビュレータ１へ
の吸収液管路７３１：１分岐管１４を取付け、この分岐
管１４をドレンタンク１５を介して活性汚泥処理槽１６
に接続している。この活性汚泥処理槽１６は、不純物を
含む安水をバクテリアで処理するもので、このバクテリ
アは＃１１峻を栄養源と１７でいる０本発明では、循環
する吸収液の一部を活性汚泥処理槽１６に導入する。こ
の導入量は、吸収液の循環量に対して通常３〜４憾程度
とする。また活性汚泥処理槽１ｇに入れた分だけ新しい
吸、収液な補給する。However, in this device, an absorption liquid pipe line 731:1 branch pipe 14 is installed from the absorption tower 1 to the debutator 1, and this branch pipe 14 is connected to the activated sludge treatment tank 16 via the drain tank 15.
is connected to. This activated sludge treatment tank 16 is for treating ammonium water containing impurities with bacteria, and this bacteria uses #11 as a nutrient source and #17 as a nutrient source. Introduced into tank 16. The amount introduced is usually about 3 to 4 times the amount of circulating absorption liquid. Also, replenish new absorption liquid for the amount put into each gram of activated sludge treatment tank.
次に本発明の実施例を説叩する。Next, embodiments of the present invention will be explained.
吸収液として３０悌憎障水溶液２０トンを用い、０．８
）７７７日ずつ更新しながらアンモニアの回収をおこな
゛つた。この方法において、蒸留塔の入口温度の変化、
すなわち、熱交換器の不純物の付着による熱交換効亭の
低下割合を調べた。その結果な第２因に折線謬で示す。Using 20 tons of 30% aqueous solution as the absorption liquid, 0.8
) Ammonia collection was carried out with updates every 777 days. In this method, changes in the inlet temperature of the distillation column,
That is, the rate of decrease in heat exchange efficiency due to adhesion of impurities to the heat exchanger was investigated. The second cause of this is shown by the broken line.
これに対し、更新しない従来の方法における無留塔の入
口温度の開化を第２図の折線すで示す。On the other hand, the broken line in FIG. 2 shows the opening of the inlet temperature of the non-removal column in the conventional method without updating.
第２図から、従来操業後１ケ月で清掃作業が必要である
のに対し１本発明では２．５ケ月後と延長されることが
わかる。From FIG. 2, it can be seen that while conventional cleaning work is required one month after operation, in the present invention the cleaning work is extended to 2.5 months after operation.
第２因から明らかなように本発明によれば。According to the present invention, as is clear from the second factor.
燐酸吸収液を適宜更新しているので不純物の蓄積を防止
し、プラントの切替、清掃の頻ずを少なくすることがで
考るとともに、不純物による腐食Ｖ軽減することができ
る。また抜き出を吸収液は、活性汚泥処理におけるバク
テリアの栄養源として利用されるため、全体の燐酸使用
量が増加することなく、そのランニングコストを従来と
同様に維持することができる、Since the phosphoric acid absorption liquid is updated as appropriate, it is possible to prevent the accumulation of impurities, reduce the frequency of plant switching and cleaning, and reduce corrosion caused by impurities. In addition, since the extracted and absorbed liquid is used as a nutrient source for bacteria in activated sludge treatment, the overall amount of phosphoric acid used does not increase, and running costs can be maintained at the same level as before.
第１１ｇは本発明の一実施例を示す系統図、第２図は本
発明方法における蒸留塔入口ｆｆ１ｌｆの変化を従来の
ものとともに示す説明図であるう１・・・吸収塔、２・
・・吸収液、１・・・デビュレータ。
４・・・リッチ液タンク、５・・・熱交換器、６・・・
コンタク！、１・・・蒸留塔コンデンサ、８・・・蒸留
塔。
９・・・スチーム、１０・・・精留塔フィードタンク。
１１・・・苛性ソーダ−，１２・・・精留塔、ＪＪ・・
・吸収液管路、１４・・・分岐管、１５・・・ドレンタ
ンク。
Ｊ６・・・活性汚泥処理槽No. 11g is a system diagram showing one embodiment of the present invention, and FIG. 2 is an explanatory diagram showing changes in the distillation column inlet ff1lf in the method of the present invention together with the conventional one.
... Absorbing liquid, 1... Debulator. 4...Rich liquid tank, 5...Heat exchanger, 6...
Contact! , 1... Distillation column condenser, 8... Distillation column. 9... Steam, 10... Rectifier feed tank. 11... Caustic soda, 12... Rectification column, JJ...
- Absorbent pipe line, 14...branch pipe, 15...drain tank. J6...Activated sludge treatment tank
Claims (1)
ンモニア分を燐＃ｌＩ＠収液で吸収した後、咳吸収液を
蒸留塔に導入しアンモニア分を蒸留するとともに吸収液
を上記吸収塔に戻し、更に蒸留したアンモニア分を精留
塔で精留するアンモニア回収方法において、上記吸収塔
と蒸留塔との間を循環する吸収液の一部を活性汚泥＃＆
処理槽導入して該吸収液を活性汚泥処理におけるノ５ク
テツアの栄養舗とするとともに、活性汚泥処理槽に入れ
た吸収液と等量の吸収液を補給することを特徴とするア
ンモニア回収方法。After introducing the COG generated in the coke oven into the absorption tower and absorbing its ammonia content with the phosphorus #lI@recovery liquid, the cough absorption liquid is introduced into the distillation tower to distill off the ammonia content and the absorption liquid is transferred to the above absorption tower. In an ammonia recovery method in which the returned and further distilled ammonia is rectified in a rectification column, a part of the absorption liquid circulating between the absorption column and the distillation column is converted into activated sludge #&
An ammonia recovery method characterized by introducing the absorption liquid into a treatment tank and using the absorption liquid as a nutrient store in activated sludge treatment, and replenishing the same amount of absorption liquid as the absorption liquid put into the activated sludge treatment tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56160471A JPS5864214A (en) | 1981-10-08 | 1981-10-08 | Recovering method for ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56160471A JPS5864214A (en) | 1981-10-08 | 1981-10-08 | Recovering method for ammonia |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5864214A true JPS5864214A (en) | 1983-04-16 |
| JPS615652B2 JPS615652B2 (en) | 1986-02-20 |
Family
ID=15715663
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP56160471A Granted JPS5864214A (en) | 1981-10-08 | 1981-10-08 | Recovering method for ammonia |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5864214A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008013406A (en) * | 2006-07-06 | 2008-01-24 | Air Water Inc | Method for recovering ammonia, method for reutilizing ammonia, ammonia recovery system and ammonia reutilization system |
| CN103805291A (en) * | 2014-02-27 | 2014-05-21 | 神华集团有限责任公司 | System for removing ammonia from water gas |
| CN105174346A (en) * | 2015-09-21 | 2015-12-23 | 中国成达工程有限公司 | Mother liquor deamination process and equipment for soda production through thermal method |
| CN114797380A (en) * | 2022-03-09 | 2022-07-29 | 铜陵泰富特种材料有限公司 | System and method for efficiently washing ammonia with phosphoric acid and producing high-purity ammonia water |
-
1981
- 1981-10-08 JP JP56160471A patent/JPS5864214A/en active Granted
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008013406A (en) * | 2006-07-06 | 2008-01-24 | Air Water Inc | Method for recovering ammonia, method for reutilizing ammonia, ammonia recovery system and ammonia reutilization system |
| CN103805291A (en) * | 2014-02-27 | 2014-05-21 | 神华集团有限责任公司 | System for removing ammonia from water gas |
| CN105174346A (en) * | 2015-09-21 | 2015-12-23 | 中国成达工程有限公司 | Mother liquor deamination process and equipment for soda production through thermal method |
| CN114797380A (en) * | 2022-03-09 | 2022-07-29 | 铜陵泰富特种材料有限公司 | System and method for efficiently washing ammonia with phosphoric acid and producing high-purity ammonia water |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS615652B2 (en) | 1986-02-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101665309B (en) | Method for treating gasified waste water containing high-concentration phenol and ammonia | |
| US3920419A (en) | Method of removing ammonia from ammonia containing liquor | |
| US5318758A (en) | Apparatus and process for removing carbon dioxide from combustion exhaust gas | |
| EP0133208A2 (en) | Removal of acidic gases from gaseous mixtures | |
| US4009243A (en) | Continuous process for scrubbing out hydrogen sulfide and ammonia from coke oven gas | |
| US4668250A (en) | Process for continuously removing and recovering respectively a gas dissolved in a liquid, particularly ammonia from aqueous ammonia waste water | |
| CN101717096A (en) | Technology for preparing desulfurizing agent ammonia water in sintering flue gas desulfurization by coking residual ammonia water | |
| US4124685A (en) | Method for substantially complete removal of hydrogen sulfide from sulfur bearing industrial gases | |
| CN102266707A (en) | Flue gas sulfur dioxide absorption solvent with high-selectivity wet method | |
| CN201658945U (en) | Sintering flue gas purification system based on heat pipe waste heat recovery technology | |
| JPS595031B2 (en) | Method and apparatus for removing volatile components from a liquid with hot gas | |
| US3000693A (en) | Method of removing and disposing of ammonia from coke oven gas | |
| US4342731A (en) | Method for removing hydrogen sulfide from coke oven gas | |
| JPS5864214A (en) | Recovering method for ammonia | |
| US4499060A (en) | Process for removing hydrogen sulfide from gases, particularly coal distillation gases | |
| CN206108916U (en) | Recovery system of ammonia among coking raw coke oven gas and coking wastewater | |
| US4778490A (en) | Process for removal of volatile matter from coke-oven plant waters | |
| US4277311A (en) | Apparatus for distillation | |
| US3790448A (en) | Method of purifying waste fluid | |
| CN212559825U (en) | Purifier of waste ammonia water | |
| US3912578A (en) | Apparatus for and a method of purifying waste fluid | |
| US2070620A (en) | Gas purification process | |
| US2789035A (en) | Process for the production of sulfur dioxide from petroleum acid sludge | |
| CN100496660C (en) | Process for treating residual ammonia water of coking | |
| CN114797380B (en) | System and method for efficiently washing ammonia with phosphoric acid and producing high-purity ammonia water |