JPH0247406B2 - - Google Patents
Info
- Publication number
- JPH0247406B2 JPH0247406B2 JP59014024A JP1402484A JPH0247406B2 JP H0247406 B2 JPH0247406 B2 JP H0247406B2 JP 59014024 A JP59014024 A JP 59014024A JP 1402484 A JP1402484 A JP 1402484A JP H0247406 B2 JPH0247406 B2 JP H0247406B2
- Authority
- JP
- Japan
- Prior art keywords
- ammonium sulfate
- mother liquor
- heater
- heat exchanger
- heat
- 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
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 53
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 53
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 53
- 239000012452 mother liquor Substances 0.000 claims description 35
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 30
- 239000000498 cooling water Substances 0.000 claims description 25
- 238000010521 absorption reaction Methods 0.000 claims description 19
- 239000000571 coke Substances 0.000 claims description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 5
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Treating Waste Gases (AREA)
- Industrial Gases (AREA)
Description
【発明の詳細な説明】
産業上の利用分野
本発明はコークス炉ガスから硫安を製造する装
置に関するものである。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to an apparatus for producing ammonium sulfate from coke oven gas.
従来例の構成とその問題点
第１図に従来例を示す。図において、１はコー
クス炉、２はコークス炉１から出た排ガス３を冷
却水４と熱交換させて冷却するプライマリークー
ラ、５はプライマリークーラ２により冷却された
排ガス３からアンモニアを吸収して硫安母液６を
生成する吸収塔で、内部には予め硫酸７が入れら
れている。８は吸収塔５で生成された硫安母液６
を貯溜するタンク、９はタンク８から引き出され
た硫安母液６を加熱する第１加熱器、１０は第１
加熱器９で加熱された硫安母液６を濃縮する例え
ば圧力が160〜200torrの第１蒸発缶で、該第１蒸
発缶１０で濃縮された硫安母液６の一部は再び前
記第１加熱器９に戻す構成とされている。１１は
第１蒸発缶１０で濃縮された硫安母液６を加熱す
る第２加熱器で、この第２加熱器１１の熱源には
前記第１蒸発缶１０のスチーム１２が用いられて
いる。１３は第２加熱器１１で加熱された硫安母
液６を濃縮して結晶状硫安１４を生成する第２蒸
発缶で、該第２蒸発缶１３からオーバーフローし
た硫安母液６はオーバーフロータンク１５に貯溜
された後、第１蒸発缶１０と第１加熱器９間の硫
安母液６循環ライン中に戻す構成とされている。
また、第２蒸発缶１３の上層硫安母液６は再び第
２加熱器１１に戻す構成とされている。なお、１
６は高温の冷却水４を導かれる冷却塔、１７は各
ポンプを示す。Configuration of conventional example and its problems Figure 1 shows a conventional example. In the figure, 1 is a coke oven, 2 is a primary cooler that cools the exhaust gas 3 emitted from the coke oven 1 by exchanging heat with cooling water 4, and 5 is a primary cooler that absorbs ammonia from the exhaust gas 3 cooled by the primary cooler 2. This is an absorption tower that produces mother liquor 6, and sulfuric acid 7 is previously placed inside. 8 is the ammonium sulfate mother liquor 6 produced in the absorption tower 5
9 is a first heater for heating the ammonium sulfate mother liquor 6 drawn out from the tank 8; 10 is a first heater;
The ammonium sulfate mother liquor 6 heated in the heater 9 is concentrated in a first evaporator at a pressure of, for example, 160 to 200 torr, and a part of the ammonium sulfate mother liquor 6 concentrated in the first evaporator 10 is returned to the first heater 9. It is said to be configured to return to . A second heater 11 heats the ammonium sulfate mother liquor 6 concentrated in the first evaporator 10, and the steam 12 of the first evaporator 10 is used as the heat source of the second heater 11. 13 is a second evaporator that condenses the ammonium sulfate mother liquor 6 heated by the second heater 11 to produce crystalline ammonium sulfate 14; the ammonium sulfate mother liquor 6 overflowing from the second evaporator 13 is stored in an overflow tank 15; After that, the ammonium sulfate mother liquor 6 is returned to the circulation line between the first evaporator 10 and the first heater 9.
Further, the upper ammonium sulfate mother liquor 6 of the second evaporator 13 is returned to the second heater 11 again. In addition, 1
Reference numeral 6 indicates a cooling tower to which the high temperature cooling water 4 is guided, and reference numeral 17 indicates each pump.
このような構成で、従来の硫安製造装置は次の
ような動作を行つていた。先ず、コークス炉１を
出た排ガス３はプライマリークーラ２を通された
後、吸収塔５に導かれる。プライマリークーラ２
を通すのは、排ガス３中のタール、ナフタリン等
を折出させるためで、プライマリークーラ２に入
る前の排ガス３温度は80℃、プライマリークーラ
２を出た排ガス３温度は20℃程度である。一方、
プライマリークーラ２に用いられた冷却水４の温
度は60〜70℃程度となる。吸収塔５で生成された
硫安母液６は、タンク８に一旦貯溜されるが、こ
こでの硫安母液６の温度は35〜42℃程度である。
タンク８に貯溜された硫安母液６は、次に第１蒸
発缶１０と第１加熱器９間の硫安母液６循環ライ
ン中に導かれ、第１加熱器９で加熱される。これ
により、硫安母液６は70℃前後の温度になつて第
１蒸発缶１０に導かれる。第１蒸発缶１０で濃縮
された硫安母液６の温度は65〜69℃程度となる。
次に、濃縮された硫安母液６は第２蒸発缶１３と
第２加熱器１１間の硫安母液６循環ライン中に導
かれ、第２加熱器１１で加熱された後、第２蒸発
缶１３に導かれる。第２蒸発缶１３で濃縮された
硫安母液６の温度は51〜54℃となり、ここで第２
蒸発缶１３の底に結晶状硫安１４が生成されるこ
とになる。結晶状硫安１４はスラリーポンプ１７
で経外に取出された後、脱水、乾燥される。 With such a configuration, a conventional ammonium sulfate manufacturing apparatus operates as follows. First, the exhaust gas 3 leaving the coke oven 1 is passed through the primary cooler 2 and then guided to the absorption tower 5. Primary cooler 2
The purpose of passing the exhaust gas is to separate out tar, naphthalene, etc. in the exhaust gas 3. The temperature of the exhaust gas 3 before entering the primary cooler 2 is 80°C, and the temperature of the exhaust gas 3 after leaving the primary cooler 2 is about 20°C. on the other hand,
The temperature of the cooling water 4 used in the primary cooler 2 is approximately 60 to 70°C. The ammonium sulfate mother liquor 6 produced in the absorption tower 5 is temporarily stored in a tank 8, and the temperature of the ammonium sulfate mother liquor 6 here is about 35 to 42°C.
The ammonium sulfate mother liquor 6 stored in the tank 8 is then introduced into the ammonium sulfate mother liquor 6 circulation line between the first evaporator 10 and the first heater 9 and heated by the first heater 9. As a result, the ammonium sulfate mother liquor 6 reaches a temperature of about 70° C. and is led to the first evaporator 10. The temperature of the ammonium sulfate mother liquor 6 concentrated in the first evaporator 10 is about 65 to 69°C.
Next, the concentrated ammonium sulfate mother liquor 6 is introduced into the ammonium sulfate mother liquor 6 circulation line between the second evaporator 13 and the second heater 11, heated by the second heater 11, and then transferred to the second evaporator 13. be guided. The temperature of the ammonium sulfate mother liquor 6 concentrated in the second evaporator 13 is 51 to 54°C, and the second
Crystalline ammonium sulfate 14 will be produced at the bottom of the evaporator 13. Crystalline ammonium sulfate 14 is slurry pump 17
After being taken out, it is dehydrated and dried.
しかしながら、このような従来の硫安製造装置
によると、プライマリークーラ２で熱交換を終え
た高温の冷却水４を単に冷却塔１６に導くだけで
有効利用する構成となつていないため、各蒸発缶
で熱を必要とするにもかかわらずせつかく60〜70
℃程度まで高められた冷却水４を無駄にするとい
う欠点があつた。 However, according to such conventional ammonium sulfate production equipment, the high-temperature cooling water 4 that has undergone heat exchange in the primary cooler 2 is not effectively utilized by simply guiding it to the cooling tower 16. 60-70 even though it requires heat
There was a drawback that the cooling water 4, which had been raised to about ℃, was wasted.
発明の目的
本発明は上記従来の欠点を解消するコークス炉
ガスから硫安を製造する装置を提供することを目
的とする。OBJECTS OF THE INVENTION An object of the present invention is to provide an apparatus for producing ammonium sulfate from coke oven gas, which eliminates the above-mentioned conventional drawbacks.
発明の構成
上記目的を達成するため、本発明のコークス炉
ガスから硫安を製造する装置は、コークス炉から
出た排ガスを冷却水と熱交換させて冷却するプラ
イマリークーラと、該プライマリークーラにより
冷却された排ガスからアンモニアを吸収して硫安
母液を生成する吸収塔と、該吸収塔で生成された
硫安母液を加熱する第１加熱器と、該第１加熱器
で加熱された硫安母液を濃縮する第１蒸発缶と、
該第１蒸発缶で濃縮された硫安母液を加熱する第
２加熱器と、該第２加熱器で加熱された硫安母液
を濃縮して結晶状硫安を生成する第２蒸発缶とを
有する硫安製造装置において、前記第１加熱器と
並列接続されて、前記吸収塔で生成された硫安母
液の一部を臭化リチウムと熱交換させる熱交換器
を設け、前記臭化リチウムに吸収させる水蒸気の
発生用熱源として前記プライマリークーラで熱交
換を終えた高温の冷却水を用いる構成としたもの
であり、これにより、プライマリークーラで熱交
換を終えた高温の冷却水を有効利用することがで
きるものである。Structure of the Invention In order to achieve the above object, the apparatus for producing ammonium sulfate from coke oven gas of the present invention includes a primary cooler that cools exhaust gas discharged from a coke oven by exchanging heat with cooling water; an absorption tower that absorbs ammonia from the collected exhaust gas to produce ammonium sulfate mother liquor; a first heater that heats the ammonium sulfate mother liquor produced in the absorption tower; and a first heater that concentrates the ammonium sulfate mother liquor heated by the first heater. 1 evaporator,
Ammonium sulfate production comprising: a second heater for heating the ammonium sulfate mother liquor concentrated in the first evaporator; and a second evaporator for concentrating the ammonium sulfate mother liquor heated by the second heater to produce crystalline ammonium sulfate. In the apparatus, a heat exchanger is provided which is connected in parallel with the first heater and exchanges heat with lithium bromide for a part of the ammonium sulfate mother liquor produced in the absorption tower, and generates water vapor to be absorbed by the lithium bromide. The system uses high-temperature cooling water that has undergone heat exchange in the primary cooler as a heat source, thereby making it possible to effectively utilize the high-temperature cooling water that has undergone heat exchange in the primary cooler. .
実施例と作用
以下、本発明の一実施例を図面に基づいて説明
する。Embodiment and Operation An embodiment of the present invention will be described below based on the drawings.
第２図は本硫安製造装置の要部を示し、図外の
構成は第１図に示したものと同一であるので説明
を省略する。図において、１８は第１加熱器９と
並列接続して設けられた吸収ヒートポンプで、相
隣接する第１および第２の熱交換器１９，２０
と、相隣接する第３および第４の熱交換器２１，
２２とから構成されている。２３は第１および第
２の熱交換器１９，２０の隣接壁２４中央部に設
けられた連通孔、２５は第３および第４の熱交換
器２１，２２の隣接壁２６中央部に設けられた連
通孔である。２７は第４熱交換器２２の底部から
引き出されて第１熱交換器１９の上部に導かれる
水、２８は第２熱交換器２０の底部から引き出さ
れて第３熱交換器２１の上部に導かれるととも
に、第３熱交換器２１の底部から引き出されて第
２熱交換器２０の上部に導かれる臭化リチウム
（LiBr水溶液）である。そして吸収塔５で生成さ
れた硫安母液６は、第１加熱器９に導かれる一
方、一部、吸収ヒートポンプ１８の第２熱交換器
２０に導かれ、該第２熱交換器２０で臭化リチウ
ム２８によつて加熱された後に第１蒸発缶１０に
導かれる構成とされている。また、プライマリー
クーラ２で熱交換を終えた高温の冷却水４は、一
部、第１熱交換器１９を経て第３熱交換器２１に
導かれ、これら第１、第３の熱交換器１９，２１
でその高熱を提供した後、冷却塔１６に導かれる
構成とされている。２９は経外から別個導かれた
冷却水で、第４熱交換器２２において冷媒蒸気を
冷却、凝縮させるものである。 FIG. 2 shows the main parts of the present ammonium sulfate manufacturing apparatus, and the configurations other than those shown are the same as those shown in FIG. 1, so their explanation will be omitted. In the figure, 18 is an absorption heat pump provided in parallel connection with the first heater 9, and adjacent first and second heat exchangers 19, 20.
and adjacent third and fourth heat exchangers 21,
It is composed of 22. 23 is a communication hole provided in the center of the wall 24 adjacent to the first and second heat exchangers 19 and 20, and 25 is a communication hole provided in the center of the wall 26 adjacent to the third and fourth heat exchangers 21 and 22. This is a communicating hole. 27 is water drawn out from the bottom of the fourth heat exchanger 22 and led to the top of the first heat exchanger 19; 28 is water drawn out from the bottom of the second heat exchanger 20 and led to the top of the third heat exchanger 21; Lithium bromide (LiBr aqueous solution) is drawn out from the bottom of the third heat exchanger 21 and led to the top of the second heat exchanger 20. The ammonium sulfate mother liquor 6 produced in the absorption tower 5 is led to the first heater 9, while a part of it is led to the second heat exchanger 20 of the absorption heat pump 18, where the ammonium sulfate mother liquor 6 is converted into bromide. After being heated by lithium 28, it is guided to the first evaporator 10. Further, a part of the high temperature cooling water 4 that has completed heat exchange in the primary cooler 2 is guided to the third heat exchanger 21 via the first heat exchanger 19, ,21
After providing the high heat, the cooling tower 16 is provided with the high heat. Cooling water 29 is separately introduced from outside and is used to cool and condense the refrigerant vapor in the fourth heat exchanger 22.
以下、上記構成における作用について説明す
る。先ず、プライマリークーラ２に例えば1450
m3／ｈで通された冷却水４は、コークス炉１の排
ガス３と熱交換して65℃程度の高温の冷却水４と
なり、一部は吸収ヒートポンプ１８の第１熱交換
器１９に導かれ、残りは冷却塔１６へと導かれ
る。第１熱交換器１９においては、この冷却水４
が水蒸気３０の発生用熱媒として働き、発生した
約60℃の水蒸気３０は連通孔２３から第２熱交換
器２０内に入り込む。そうすると、第２熱交換器
２０内の例えば43重量％の臭化リチウム２８がこ
の水蒸気３０を吸収し、40重量％に薄められると
ともに73〜76℃程度の温度レベルで吸収熱を発生
することになる。そこで、第２熱交換器２０に導
かれた吸収塔５からの硫安母液６（40℃程度）
は、この吸収熱によつて69℃程度まで加熱され、
第１蒸発缶１０へと導かれる。第１熱交換器１９
を出た冷却水４は62℃程度となつて第３熱交換器
２１に入り、前記第２熱交換器２０で薄められた
臭化リチウム２８を再生する働きをなす。すなわ
ち、第２熱交換器２０の底部から引き出された希
臭化リチウム２８は第３熱交換器２１の上部に導
かれ、高温の冷却水４との熱交換により約0.06
Kg／cm3absの水蒸気３０を発生して43重量％の濃
臭化リチウム２８となる。第３熱交換器２１を出
た冷却水４は59℃程度となつて吸収塔１６へと導
かれる。一方、第３熱交換器２１で発生した水蒸
気３０は連通孔２５から第４熱交換器２２内に入
り、該第４熱交換器２２を通る冷却水２９との熱
交換で冷却される。これにより、水蒸気３０は水
２７となり第４熱交換器２２底部から引き出され
て第１熱交換器１９の上部に導かれる。なお、冷
却水２９は例えば1780m3／ｈで第４熱交換器２２
を通され、第４熱交換器２２に入る前の温度が31
℃、出た時の温度が33.5℃程度となる。 Hereinafter, the effects of the above configuration will be explained. First, for example, set 1450 to primary cooler 2.
The cooling water 4 passed at a rate of m 3 /h exchanges heat with the exhaust gas 3 of the coke oven 1 to become cooling water 4 with a high temperature of about 65°C, and a part of it is led to the first heat exchanger 19 of the absorption heat pump 18. The rest is guided to the cooling tower 16. In the first heat exchanger 19, this cooling water 4
acts as a heat medium for generating steam 30, and the generated steam 30 of about 60° C. enters into the second heat exchanger 20 through the communication hole 23. Then, for example, 43% by weight of lithium bromide 28 in the second heat exchanger 20 absorbs this water vapor 30, dilutes it to 40% by weight, and generates absorption heat at a temperature level of about 73 to 76°C. Become. Therefore, the ammonium sulfate mother liquor 6 (about 40°C) from the absorption tower 5 is guided to the second heat exchanger 20.
is heated to about 69℃ by this absorbed heat,
It is guided to the first evaporator 10. First heat exchanger 19
The cooling water 4 that has left the cooling water reaches a temperature of about 62° C. and enters the third heat exchanger 21, where it serves to regenerate the lithium bromide 28 diluted in the second heat exchanger 20. That is, the diluted lithium bromide 28 drawn out from the bottom of the second heat exchanger 20 is led to the upper part of the third heat exchanger 21, and is reduced to about 0.06 by heat exchange with the high temperature cooling water 4.
Kg/cm 3 abs of water vapor 30 is generated and 43% by weight of concentrated lithium bromide 28 is produced. The cooling water 4 leaving the third heat exchanger 21 reaches a temperature of about 59° C. and is led to the absorption tower 16. On the other hand, water vapor 30 generated in the third heat exchanger 21 enters the fourth heat exchanger 22 through the communication hole 25 and is cooled by heat exchange with the cooling water 29 passing through the fourth heat exchanger 22. As a result, the water vapor 30 becomes water 27 and is drawn out from the bottom of the fourth heat exchanger 22 and guided to the top of the first heat exchanger 19. Note that the cooling water 29 is supplied to the fourth heat exchanger 22 at a rate of 1780 m 3 /h, for example.
The temperature before entering the fourth heat exchanger 22 is 31
℃, the temperature when it comes out is about 33.5℃.
第３図はこれらの温度と圧力の関係を示したも
のである。図中、イ点が第１熱交換器１９、ロ点
が第２熱交換器２０、ハ点が第３熱交換器２１、
ニ点が第４熱交換器２２に対応する。 FIG. 3 shows the relationship between these temperatures and pressures. In the figure, point A is the first heat exchanger 19, point B is the second heat exchanger 20, point C is the third heat exchanger 21,
Point two corresponds to the fourth heat exchanger 22.
なお、第２熱交換器２０における臭化リチウム
２８の吸収による発熱量QAは次式で与えられる。 Note that the calorific value Q A due to absorption of lithium bromide 28 in the second heat exchanger 20 is given by the following equation.
QA＝Hse＋Wli・Hli−（Wli＋１）・Hlo
ここでHse：第１熱交換器１９で発生した水蒸
気３０のエンクルピー
Wli：第２熱交換器２０に供給される臭化リチ
ウム２８の量
Hli：第２熱交換器２０に供給される臭化リチ
ウム２８のエンタルピー
Hlo：第２熱交換器２０から出る臭化リチウム
２８のエンタルピー
このように、本発明の硫安製造装置は、プライ
マリークーラ２で熱交換を終えた高温の冷却水４
を有効利用するものであるが、蒸気消費量だけを
とつてみると、例えば8.4T／Ｈの硫安製造装置
の場合、蒸気単価4000円／Ｔ、運転時間8000Hと
すると、｛（500Mcal／Ｔ・硫安
×8.4Ｔ・硫安／Ｈ
）／600Mcal／Ｔ・蒸気
｝×4000円／Ｔ・蒸気
×8000H＝224000千円の年間利得となる。 Q A = Hse + Wli・Hli−(Wli+1)・Hlo where Hse: Encyclopedia of water vapor 30 generated in the first heat exchanger 19 Wli: Amount of lithium bromide 28 supplied to the second heat exchanger 20 Hli: 2 Enthalpy of lithium bromide 28 supplied to the second heat exchanger 20 Hlo: Enthalpy of lithium bromide 28 discharged from the second heat exchanger 20 As described above, the ammonium sulfate production apparatus of the present invention performs heat exchange in the primary cooler 2. Finished high temperature cooling water 4
However, if we look only at steam consumption, for example, in the case of an 8.4T/H ammonium sulfate manufacturing equipment, if the steam unit price is 4000 yen/T and the operating time is 8000 H , then {(500 Mcal/T)・Ammonium sulfate ×8.4T・Ammonium sulfate/H )/600Mcal/T・Steam }×4000 yen/T・Steam
×8000 H = annual profit of 224,000,000 yen.
発明の効果
以上本発明によれば、プライマリークーラで熱
交換を終えた高温の冷却水を有効利用することが
できる。したがつて、冷却水を導入される冷却塔
の負荷を回収された熱量分だけ軽くすることがで
きるのは勿論、稼動費用の削減を図ることができ
る。Effects of the Invention According to the present invention, high-temperature cooling water that has undergone heat exchange in the primary cooler can be effectively used. Therefore, not only can the load on the cooling tower into which the cooling water is introduced be reduced by the amount of heat recovered, but also the operating cost can be reduced.
第１図は従来のコークス炉ガスから硫安を製造
する装置の全体工程図、第２図および第３図は本
発明の一実施例を示し、第２図は本発明に係るコ
ークス炉ガスから硫安を製造する装置の要部工程
図、第３図は温度と圧力の関係をあらわす図であ
る。
１……コークス炉、２……プライマリークー
ラ、３……排ガス、４……冷却水、５……吸収
塔、６……硫安母液、９……第１加熱器、１０…
…第１蒸発缶、１１……第２加熱器、１３……第
２蒸発缶、１４……結晶状硫安、１８……吸収ヒ
ートポンプ、２８……臭化リチウム、３０……水
蒸気。
FIG. 1 is an overall process diagram of a conventional apparatus for producing ammonium sulfate from coke oven gas, FIGS. 2 and 3 show an embodiment of the present invention, and FIG. FIG. 3 is a flowchart showing the main parts of the apparatus for manufacturing the . 1... Coke oven, 2... Primary cooler, 3... Exhaust gas, 4... Cooling water, 5... Absorption tower, 6... Ammonium sulfate mother liquor, 9... First heater, 10...
...First evaporator, 11...Second heater, 13...Second evaporator, 14...Crystalline ammonium sulfate, 18...Absorption heat pump, 28...Lithium bromide, 30...Steam vapor.
Claims (1)
させて冷却するプライマリークーラと、該プライ
マリークーラにより冷却された排ガスからアンモ
ニアを吸収して硫安母液を生成する吸収塔と、該
吸収塔で生成された硫安母液を加熱する第１加熱
器と、該第１加熱器で加熱された硫安母液を濃縮
する第１蒸発缶と、該第１蒸発缶で濃縮された硫
安母液を加熱する第２加熱器と、該第２加熱器で
加熱された硫安母液を濃縮して結晶状硫安を生成
する第２蒸発缶とを有する硫安製造装置におい
て、前記第１加熱器と並列接続されて、前記吸収
塔で生成された硫安母液の一部を臭化リチウムと
熱交換させる熱交換器を設け、前記臭化リチウム
に吸収させる水蒸気の発生用熱源として前記プラ
イマリークーラで熱交換を終えた高温の冷却水を
用いることを特徴とするコークス炉ガスから硫安
を製造する装置。1. A primary cooler that cools the exhaust gas emitted from the coke oven by exchanging heat with cooling water, an absorption tower that absorbs ammonia from the exhaust gas cooled by the primary cooler and generates ammonium sulfate mother liquor, and a a first heater for heating ammonium sulfate mother liquor, a first evaporator for concentrating the ammonium sulfate mother liquor heated by the first heater, and a second heater for heating the ammonium sulfate mother liquor concentrated in the first evaporator. and a second evaporator for producing crystalline ammonium sulfate by concentrating the ammonium sulfate mother liquor heated by the second heater, which is connected in parallel with the first heater, and in the absorption tower. A heat exchanger is provided to heat-exchange a part of the generated ammonium sulfate mother liquor with lithium bromide, and the high-temperature cooling water that has undergone heat exchange in the primary cooler is used as a heat source for generating steam to be absorbed by the lithium bromide. An apparatus for producing ammonium sulfate from coke oven gas, characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59014024A JPS60161325A (en) | 1984-01-27 | 1984-01-27 | Equipment for producing ammonium sulfate from coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59014024A JPS60161325A (en) | 1984-01-27 | 1984-01-27 | Equipment for producing ammonium sulfate from coke oven gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60161325A JPS60161325A (en) | 1985-08-23 |
| JPH0247406B2 true JPH0247406B2 (en) | 1990-10-19 |
Family
ID=11849604
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59014024A Granted JPS60161325A (en) | 1984-01-27 | 1984-01-27 | Equipment for producing ammonium sulfate from coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60161325A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102205201B (en) * | 2011-06-10 | 2012-11-21 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
| ITMI20130847A1 (en) * | 2013-05-24 | 2014-11-25 | Saipem Spa | METHOD AND SYSTEM FOR THE RECOVERY OF AMMONIUM SULPHATE FROM A GASEOUS FLOW OF A UREA PLANT |
| CN104649298B (en) * | 2014-04-21 | 2017-01-04 | 柳州钢铁股份有限公司 | The production method of ammonium sulfate |
-
1984
- 1984-01-27 JP JP59014024A patent/JPS60161325A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60161325A (en) | 1985-08-23 |
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