JPH05124804A - Production of dilute sulfuric acid and manufacturing equipment - Google Patents
Production of dilute sulfuric acid and manufacturing equipmentInfo
- Publication number
- JPH05124804A JPH05124804A JP31194391A JP31194391A JPH05124804A JP H05124804 A JPH05124804 A JP H05124804A JP 31194391 A JP31194391 A JP 31194391A JP 31194391 A JP31194391 A JP 31194391A JP H05124804 A JPH05124804 A JP H05124804A
- Authority
- JP
- Japan
- Prior art keywords
- sulfuric acid
- mixer
- cooler
- water
- diluted
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、濃硫酸を水で希釈して
溥硫酸を製造する方法及び装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and apparatus for producing concentrated sulfuric acid by diluting concentrated sulfuric acid with water.
【０００２】[0002]
【従来の技術】従来、濃硫酸を水で希釈する溥硫酸製造
方法には、攪拌機と冷却器を備えた希釈槽内に濃硫酸と
水を或る割合で導き、目的濃度の溥硫酸を間欠的に得る
方法と、濃硫酸と水をミキサで連続的に混合し、得られ
た溥硫酸を冷却器で冷却し、目的濃度の溥硫酸を連続的
に得る方法があった。2. Description of the Related Art Hitherto, in a method for producing oleic sulfuric acid in which concentrated sulfuric acid is diluted with water, concentrated sulfuric acid and water are introduced at a certain ratio into a diluting tank equipped with a stirrer and a cooler to intermittently produce an intended concentration of oleic sulfuric acid. And a method in which concentrated sulfuric acid and water are continuously mixed in a mixer, and the obtained sulfuric acid is cooled in a cooler to continuously obtain the desired concentration of sulfuric acid.
【０００３】[0003]
【発明が解決しようとする課題】しかし、希釈槽内に濃
硫酸と水を導く前者の方法は、希釈槽を密閉型に構成で
き、密閉した希釈槽の上部に空間が残る範囲内で運転で
きるので、希釈によって硫酸が沸騰するようなことが起
こっても、危険が少ないものであるが、この方法は、バ
ッチ処理であるため、連続して溥硫酸を得ることができ
ないという生産性の欠点があった。またこの構成で連続
して溥硫酸を得ようとすると、同様の希釈槽をいくつか
設け、これらの希釈槽を交互に運転しなければならない
ので、設備が大掛かりなものとなる欠点があった。However, in the former method of introducing concentrated sulfuric acid and water into the diluting tank, the diluting tank can be constructed as a closed type, and the diluting tank can be operated within a range where a space remains above the diluting tank. Therefore, even if boiling of sulfuric acid occurs due to dilution, it is less dangerous, but since this method is a batch process, there is a drawback in productivity that continuous sulfuric acid cannot be obtained. there were. Further, if it is attempted to continuously obtain oleic sulfuric acid with this configuration, several similar diluting tanks have to be provided and these diluting tanks have to be operated alternately, so there is a drawback that the equipment becomes large-scale.
【０００４】一方、後者の方法で、例えば９８％重量濃
度の濃硫酸を希釈して、例えば７０％重量濃度の溥硫酸
を製造する場合には、得られる溥硫酸の温度は、発生す
る希釈熱のため、約１６０°Ｃまで上昇するが、得られ
る７０％重量濃度の溥硫酸の沸点が１６２〜３°Ｃであ
るという事実から、濃硫酸と希釈水を混合する際、双方
の混合比を正確になるように計量する装置が必要であ
り、そのような計量装置の精度が低いときや、誤動作を
起こしたときには、希釈熱が過剰に発生し、硫酸が沸騰
し危険となる欠点があった。On the other hand, in the latter method, for example, when concentrated sulfuric acid having a concentration of 98% by weight is diluted to produce, for example, sulfuric acid having a concentration of 70% by weight, the temperature of the obtained sulfuric acid is the dilution heat generated. Therefore, the boiling point of the resulting 70% by weight sulfuric acid is 162 to 3 ° C, but when mixing concentrated sulfuric acid and diluting water, the mixing ratio of both is increased. It is necessary to have a device that weighs accurately, and when the precision of such a weighing device is low or when it malfunctions, excessive dilution heat is generated, and sulfuric acid boils, which is a danger. ..
【０００５】したがって、本発明の目的は、連続的に溥
硫酸を得る形式の方法及び装置において、硫酸が沸騰す
る危険をなくした新規な製造方法及び装置を提供するこ
とにある。Therefore, it is an object of the present invention to provide a novel manufacturing method and apparatus which eliminates the risk of boiling sulfuric acid in a method and apparatus of the type for continuously obtaining oleic sulfuric acid.
【０００６】[0006]
【課題を解決するための手段】前述の目的を達成するた
めに、本発明は、濃硫酸を水で希釈することにより溥硫
酸を連続的に製造する方法において、第１ミキサ内で濃
硫酸を希釈水である濃度に希釈し、希釈した硫酸を第１
クーラで冷却し、第２ミキサ内で前記冷却した硫酸をさ
らに希釈水で希釈して溥硫酸を得て、該溥硫酸を第２ク
ーラで冷却する、ことを特徴とする溥硫酸の製造方法を
採用するものである。In order to achieve the above object, the present invention provides a method for continuously producing concentrated sulfuric acid by diluting concentrated sulfuric acid with water, wherein concentrated sulfuric acid is prepared in a first mixer. Dilute the diluted sulfuric acid to a certain concentration and dilute the sulfuric acid first.
A method for producing bisulfate, which comprises cooling with a cooler, further diluting the cooled sulfuric acid in a second mixer with dilution water to obtain oleum, and cooling the oleum with the second cooler. To be adopted.
【０００７】また、本発明は、濃硫酸を水で希釈するこ
とにより溥硫酸を連続的に製造する装置において、濃硫
酸の供給源と水の供給源に連結されていて濃硫酸と希釈
水を混合して希釈する第１ミキサと、第１ミキサの出口
と連結されていて第１ミキサからの希釈した硫酸を冷却
する第１クーラと、第１クーラの出口と前記水の供給源
と連結されていて第１クーラで冷却して硫酸と水の供給
源からの希釈水とを混合してさらに希釈する第２ミキサ
と、第２ミキサの出口と連結されていて第２ミキサで希
釈された溥硫酸を冷却する第２クーラとを有することを
特徴とする溥硫酸の製造装置を採用するものである。Further, according to the present invention, in a device for continuously producing oleic sulfuric acid by diluting concentrated sulfuric acid with water, the concentrated sulfuric acid and the dilution water are connected to a concentrated sulfuric acid supply source and a water supply source. A first mixer for mixing and diluting, a first cooler connected to an outlet of the first mixer for cooling diluted sulfuric acid from the first mixer, an outlet of the first cooler and a source of the water. A second mixer that cools with a first cooler and mixes sulfuric acid with dilution water from a water source to further dilute it; and an outlet that is connected to the outlet of the second mixer and diluted with the second mixer. The present invention employs a manufacturing apparatus for oleic sulfuric acid, which has a second cooler for cooling sulfuric acid.
【０００８】[0008]
【作用】本発明の製造方法及び装置の構成では、硫酸の
温度上昇をもたらす希釈熱発生の機会を２度に分割し、
１度目の熱発生と２度目の熱発生後に硫酸を冷却して除
熱の機会を与えることにより、希釈される硫酸の温度が
到達しうる最高温度を、そのときの硫酸の濃度における
沸点以下の温度に抑えることができる。これにより硫酸
の沸騰の危険を排除するものである。In the structure of the manufacturing method and apparatus of the present invention, the opportunity for the heat of dilution to bring about the temperature rise of sulfuric acid is divided into two,
By cooling the sulfuric acid after the first heat generation and the second heat generation to give an opportunity for heat removal, the maximum temperature that the temperature of the diluted sulfuric acid can reach is lower than the boiling point at the sulfuric acid concentration at that time. Can be suppressed to temperature. This eliminates the risk of boiling sulfuric acid.
【０００９】[0009]
【実施例】次に、本発明の好ましい実施例を図面を参照
して説明する。図１は本発明の製造装置のブロック図で
ある。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT A preferred embodiment of the present invention will now be described with reference to the drawings. FIG. 1 is a block diagram of a manufacturing apparatus of the present invention.
【００１０】図１において、例えば９８％重量濃度の濃
硫酸は、濃硫酸供給ポンプ１によって第１ミキサ２に供
給される。一方、希釈用の工業用水は、希釈水ポンプ３
によって昇圧された後、希釈水流量調節弁４によって硫
酸の濃度が８０〜９０％重量濃度となるように調節され
て第１ミキサ２に供給される。この第１ミキサで第１回
目の即ち前段の希釈が行われる。この時点で硫酸の温度
は生成よる希釈熱のため１５０〜１３０°Ｃにまで上昇
している。In FIG. 1, concentrated sulfuric acid of 98% weight concentration, for example, is supplied to the first mixer 2 by the concentrated sulfuric acid supply pump 1. On the other hand, the industrial water for dilution is the dilution water pump 3
After the pressure is increased by, the concentration of sulfuric acid is adjusted by the dilution water flow rate control valve 4 to be 80 to 90% by weight and supplied to the first mixer 2. The first mixer, that is, the first-stage dilution is performed in this first mixer. At this point, the temperature of the sulfuric acid has risen to 150 to 130 ° C due to the heat of dilution due to the formation.
【００１１】この硫酸は直ちに第１クーラ５に運ばれ、
そこで７０〜８０°Ｃまで冷却される。冷却された硫酸
は第２ミキサ６に送られ、希釈水流量調節弁４により流
量調節された工業用水によって７０％重量濃度になるよ
うに希釈される。この時点での硫酸の温度は１１０〜１
００°Ｃまで上昇するので、第２クーラ７によって６０
°Ｃまで冷却される。冷却された溥硫酸は続いて第３ク
ーラ８によって４０°Ｃまで冷却される。得られた溥硫
酸は中継槽９に一時的に貯蔵され、中継ポンプ１０によ
って溥硫酸タンク（図示せず）に送られる。This sulfuric acid is immediately carried to the first cooler 5,
There it is cooled to 70-80 ° C. The cooled sulfuric acid is sent to the second mixer 6 and is diluted with the industrial water whose flow rate is adjusted by the dilution water flow rate control valve 4 to have a 70% weight concentration. The temperature of sulfuric acid at this point is 110-1
Since the temperature rises to 00 ° C, 60 is set by the second cooler 7.
It is cooled to ° C. The cooled oleum is then cooled by the third cooler 8 to 40 ° C. The obtained hydrosulfuric acid is temporarily stored in the relay tank 9, and sent to a hydrosulfuric acid tank (not shown) by the relay pump 10.
【００１２】なお、クーラの冷却媒体としては、海水が
用いられてもよく、この場合、海水はストレーナ１１を
経た後、冷却水流量計１２を通して各クーラに供給さ
れ、熱交換後に排出される。Seawater may be used as the cooling medium of the cooler. In this case, after passing through the strainer 11, the seawater is supplied to each cooler through the cooling water flow meter 12 and discharged after heat exchange.
【００１３】[0013]
【発明の効果】以上詳細に説明したように、本発明によ
れば、硫酸の沸騰の危険を排除し、能率的な連続工程に
より溥硫酸を製造することができる。As described in detail above, according to the present invention, the risk of boiling of sulfuric acid can be eliminated, and oleic sulfuric acid can be produced by an efficient continuous process.
【図１】図１は、本発明の好ましい実施例の製造装置の
ブロック図である。FIG. 1 is a block diagram of a manufacturing apparatus according to a preferred embodiment of the present invention.
１ 濃硫酸供給ポンプ ２ 第１ミキサ ３ 希釈水供給ポンプ ４ 希釈水流量調節弁 ５ 第１クーラ ６ 第２ミキサ ７ 第２クーラ ８ 第３ミキサ 1 Concentrated Sulfuric Acid Supply Pump 2 1st Mixer 3 Dilution Water Supply Pump 4 Dilution Water Flow Control Valve 5 1st Cooler 6 2nd Mixer 7 2nd Cooler 8 3rd Mixer
─────────────────────────────────────────────────────
─────────────────────────────────────────────────── ───
【手続補正書】[Procedure amendment]
【提出日】平成４年１０月２０日[Submission date] October 20, 1992
【手続補正１】[Procedure Amendment 1]
【補正対象書類名】明細書[Document name to be amended] Statement
【補正対象項目名】全文[Name of item to be corrected] Full text
【補正方法】変更[Correction method] Change
【補正内容】[Correction content]
【書類名】 明細書[Document name] Statement
【発明の名称】 薄硫酸の製造方法及び製造装置Title: Method and apparatus for manufacturing thin sulfuric acid
【特許請求の範囲】[Claims]
【発明の詳細な説明】Detailed Description of the Invention
【０００１】[0001]
【産業上の利用分野】本発明は、濃硫酸を水で希釈して
薄硫酸を製造する方法及び装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and a device for producing concentrated sulfuric acid by diluting concentrated sulfuric acid with water.
【０００２】[0002]
【従来の技術】従来、濃硫酸を水で希釈する薄硫酸製造
方法には、攪拌機と冷却器を備えた希釈槽内に濃硫酸と
水を或る割合で導き、目的濃度の薄硫酸を間欠的に得る
方法と、濃硫酸と水をミキサで連続的に混合し、得られ
た薄硫酸を冷却器で冷却し、目的濃度の薄硫酸を連続的
に得る方法があった。2. Description of the Related Art Conventionally, in a method for producing diluted sulfuric acid in which concentrated sulfuric acid is diluted with water, concentrated sulfuric acid and water are introduced at a certain ratio into a diluting tank equipped with a stirrer and a cooler to intermittently produce a diluted sulfuric acid having a desired concentration. And a method in which concentrated sulfuric acid and water are continuously mixed in a mixer, and the resulting thin sulfuric acid is cooled in a cooler to continuously obtain a desired concentration of diluted sulfuric acid.
【０００３】[0003]
【発明が解決しようとする課題】しかし、希釈槽内に濃
硫酸と水を導く前者の方法は、希釈槽を密閉型に構成で
き、密閉した希釈槽の上部に空間が残る範囲内で運転で
きるので、希釈によって硫酸が沸騰するようなことが起
こっても、危険が少ないものであるが、この方法は、バ
ッチ処理であるため、連続して薄硫酸を得ることができ
ないという生産性の欠点があった。またこの構成で連続
して薄硫酸を得ようとすると、同様の希釈槽をいくつか
設け、これらの希釈槽を交互に運転しなければならない
ので、設備が大掛かりなものとなる欠点があった。However, in the former method of introducing concentrated sulfuric acid and water into the diluting tank, the diluting tank can be constructed as a closed type, and the diluting tank can be operated within a range where a space remains above the diluting tank. Therefore, even if boiling of sulfuric acid occurs due to dilution, there is little danger, but since this method is a batch process, there is a drawback in productivity that continuous thin sulfuric acid cannot be obtained. there were. Further, in order to continuously obtain dilute sulfuric acid with this configuration, it is necessary to provide several similar diluting tanks and to alternately operate these diluting tanks, so that there is a drawback that the equipment becomes large-scale.
【０００４】一方、後者の方法で、例えば９８％重量濃
度の濃硫酸を希釈して、例えば７０％重量濃度の薄硫酸
を製造する場合には、得られる薄硫酸の温度は、発生す
る希釈熱のため、約１６０°Ｃまで上昇するが、得られ
る７０％重量濃度の薄硫酸の沸点が１６２〜３°Ｃであ
るという事実から、濃硫酸と希釈水を混合する際、双方
の混合比を正確になるように計量する装置が必要であ
り、そのような計量装置の精度が低いときや、誤動作を
起こしたときには、希釈熱が過剰に発生し、硫酸が沸騰
し危険となる欠点があった。On the other hand, in the latter method, when concentrated sulfuric acid having a concentration of 98% by weight is diluted to produce diluted sulfuric acid having a concentration of 70% by weight, for example, the temperature of the obtained diluted sulfuric acid is the heat of dilution generated. Therefore, the boiling point of the obtained 70% weight-concentrated thin sulfuric acid is 162 to 3 ° C, but when mixing concentrated sulfuric acid and diluting water, the mixing ratio of both is increased. It is necessary to have a device that weighs accurately, and when the precision of such a weighing device is low or when it malfunctions, excessive dilution heat is generated, and sulfuric acid boils, which is a danger. ..
【０００５】したがって、本発明の目的は、連続的に薄
硫酸を得る形式の方法及び装置において、硫酸が沸騰す
る危険をなくした新規な製造方法及び装置を提供するこ
とにある。SUMMARY OF THE INVENTION It is therefore an object of the present invention to provide a novel method and apparatus for continuously producing dilute sulfuric acid without the risk of boiling sulfuric acid.
【０００６】[0006]
【課題を解決するための手段】前述の目的を達成するた
めに、本発明は、濃硫酸を水で希釈することにより薄硫
酸を連続的に製造する方法において、第１ミキサ内で濃
硫酸を希釈水である濃度に希釈し、希釈した硫酸を第１
クーラで冷却し、第２ミキサ内で前記冷却した硫酸をさ
らに希釈水で希釈して薄硫酸を得て、該薄硫酸を第２ク
ーラで冷却する、ことを特徴とする薄硫酸の製造方法を
採用するものである。In order to achieve the above object, the present invention provides a method for continuously producing diluted sulfuric acid by diluting concentrated sulfuric acid with water, wherein concentrated sulfuric acid is added in a first mixer. Dilute the diluted sulfuric acid to a certain concentration and dilute the sulfuric acid first.
Cooling with a cooler, further diluting the cooled sulfuric acid in a second mixer with dilution water to obtain diluted sulfuric acid, and cooling the diluted sulfuric acid with a second cooler. To be adopted.
【０００７】また、本発明は、濃硫酸を水で希釈するこ
とにより薄硫酸を連続的に製造する装置において、濃硫
酸の供給源と水の供給源に連結されていて濃硫酸と希釈
水を混合して希釈する第１ミキサと、第１ミキサの出口
と連結されていて第１ミキサからの希釈した硫酸を冷却
する第１クーラと、第１クーラの出口と前記水の供給源
と連結されていて第１クーラで冷却して硫酸と水の供給
源からの希釈水とを混合してさらに希釈する第２ミキサ
と、第２ミキサの出口と連結されていて第２ミキサで希
釈された薄硫酸を冷却する第２クーラとを有することを
特徴とする薄硫酸の製造装置を採用するものである。Further, the present invention is an apparatus for continuously producing diluted sulfuric acid by diluting concentrated sulfuric acid with water, which is connected to a source of concentrated sulfuric acid and a source of water to separate concentrated sulfuric acid and dilution water. A first mixer for mixing and diluting, a first cooler connected to an outlet of the first mixer for cooling diluted sulfuric acid from the first mixer, an outlet of the first cooler and a source of the water. A second mixer that cools with a first cooler and mixes sulfuric acid with dilution water from a water source to further dilute; and a thin mixer that is connected to the outlet of the second mixer and diluted with a second mixer. A thin sulfuric acid manufacturing apparatus is adopted which has a second cooler for cooling the sulfuric acid.
【０００８】[0008]
【作用】本発明の製造方法及び装置の構成では、硫酸の
温度上昇をもたらす希釈熱発生の機会を２度に分割し、
１度目の熱発生と２度目の熱発生後に硫酸を冷却して除
熱の機会を与えることにより、希釈される硫酸の温度が
到達しうる最高温度を、そのときの硫酸の濃度における
沸点以下の温度に抑えることができる。これにより硫酸
の沸騰の危険を排除するものである。In the structure of the manufacturing method and apparatus of the present invention, the opportunity for the heat of dilution to bring about the temperature rise of sulfuric acid is divided into two,
By cooling the sulfuric acid after the first heat generation and the second heat generation to give an opportunity for heat removal, the maximum temperature that the temperature of the diluted sulfuric acid can reach is lower than the boiling point at the sulfuric acid concentration at that time. Can be suppressed to temperature. This eliminates the risk of boiling sulfuric acid.
【０００９】[0009]
【実施例】次に、本発明の好ましい実施例を図面を参照
して説明する。図１は本発明の製造装置のブロック図で
ある。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT A preferred embodiment of the present invention will now be described with reference to the drawings. FIG. 1 is a block diagram of a manufacturing apparatus of the present invention.
【００１０】図１において、例えば９８％重量濃度の濃
硫酸は、濃硫酸供給ポンプ１によって第１ミキサ２に供
給される。一方、希釈用の工業用水は、希釈水ポンプ３
によって昇圧された後、希釈水流量調節弁４によって硫
酸の濃度が８０〜９０％重量濃度となるように調節され
て第１ミキサ２に供給される。この第１ミキサで第１回
目の即ち前段の希釈が行われる。この時点で硫酸の温度
は生成よる希釈熱のため１５０〜１３０°Ｃにまで上昇
している。In FIG. 1, concentrated sulfuric acid of 98% weight concentration, for example, is supplied to the first mixer 2 by the concentrated sulfuric acid supply pump 1. On the other hand, the industrial water for dilution is the dilution water pump 3
After the pressure is increased by, the concentration of sulfuric acid is adjusted by the dilution water flow rate control valve 4 to be 80 to 90% by weight and supplied to the first mixer 2. The first mixer, that is, the first-stage dilution is performed in this first mixer. At this point, the temperature of the sulfuric acid has risen to 150 to 130 ° C due to the heat of dilution due to the formation.
【００１１】この硫酸は直ちに第１クーラ５に運ばれ、
そこで７０〜８０°Ｃまで冷却される。冷却された硫酸
は第２ミキサ６に送られ、希釈水流量調節弁４により流
量調節された工業用水によって７０％重量濃度になるよ
うに希釈される。この時点での硫酸の温度は１１０〜１
００°Ｃまで上昇するので、第２クーラ７によって６０
°Ｃまで冷却される。冷却された薄硫酸は続いて第３ク
ーラ８によって４０°Ｃまで冷却される。得られた薄硫
酸は中継槽９に一時的に貯蔵され、中継ポンプ１０によ
って薄硫酸タンク（図示せず）に送られる。This sulfuric acid is immediately carried to the first cooler 5,
There it is cooled to 70-80 ° C. The cooled sulfuric acid is sent to the second mixer 6 and is diluted with the industrial water whose flow rate is adjusted by the dilution water flow rate control valve 4 to have a 70% weight concentration. The temperature of sulfuric acid at this point is 110-1
Since the temperature rises to 00 ° C, 60 is set by the second cooler 7.
It is cooled to ° C. The cooled thin sulfuric acid is subsequently cooled to 40 ° C. by the third cooler 8. The obtained thin sulfuric acid is temporarily stored in the relay tank 9 and sent to a thin sulfuric acid tank (not shown) by the relay pump 10.
【００１２】なお、クーラの冷却媒体としては、海水が
用いられてもよく、この場合、海水はストレーナ１１を
経た後、冷却水流量計１２を通して各クーラに供給さ
れ、熱交換後に排出される。Seawater may be used as the cooling medium of the cooler. In this case, after passing through the strainer 11, the seawater is supplied to each cooler through the cooling water flow meter 12 and discharged after heat exchange.
【００１３】[0013]
【発明の効果】以上詳細に説明したように、本発明によ
れば、硫酸の沸騰の危険を排除し、能率的な連続工程に
より薄硫酸を製造することができる。As described in detail above, according to the present invention, the risk of boiling of sulfuric acid can be eliminated, and thin sulfuric acid can be produced by an efficient continuous process.
【図面の簡単な説明】[Brief description of drawings]
【図１】図１は、本発明の好ましい実施例の製造装置の
ブロック図である。FIG. 1 is a block diagram of a manufacturing apparatus according to a preferred embodiment of the present invention.
【符号の説明】 １ 濃硫酸供給ポンプ ２ 第１ミキサ ３ 希釈水供給ポンプ ４ 希釈水流量調節弁 ５ 第１クーラ ６ 第２ミキサ ７ 第２クーラ ８ 第３ミキサ[Explanation of Codes] 1 concentrated sulfuric acid supply pump 2 first mixer 3 dilution water supply pump 4 dilution water flow rate control valve 5 first cooler 6 second mixer 7 second cooler 8 third mixer
Claims (3)
を連続的に製造する方法において、第１ミキサ内で濃硫
酸を希釈水である濃度に希釈し、希釈した硫酸を第１ク
ーラで冷却し、第２ミキサ内で前記冷却した硫酸をさら
に希釈水で希釈して溥硫酸を得て、該溥硫酸を第２クー
ラで冷却する、ことを特徴とする溥硫酸の製造方法。1. A method of continuously producing concentrated sulfuric acid by diluting concentrated sulfuric acid with water, comprising diluting concentrated sulfuric acid to a concentration of dilution water in a first mixer, and diluting the diluted sulfuric acid with a first cooler. A method for producing oleic sulfuric acid, which comprises cooling, and further diluting the chilled sulfuric acid in a second mixer with dilution water to obtain oleic sulfuric acid, and cooling the oleoresin with a second cooler.
を連続的に製造する装置において、濃硫酸の供給源と水
の供給源に連結されていて濃硫酸と希釈水を混合して希
釈する第１ミキサと、第１ミキサの出口と連結されてい
て第１ミキサからの希釈した硫酸を冷却する第１クーラ
と、第１クーラの出口と前記水の供給源と連結されてい
て第１クーラで冷却して硫酸と水の供給源からの希釈水
とを混合してさらに希釈する第２ミキサと、第２ミキサ
の出口と連結されていて第２ミキサで希釈された溥硫酸
を冷却する第２クーラとを有することを特徴とする溥硫
酸の製造装置。2. An apparatus for continuously producing oleic sulfuric acid by diluting concentrated sulfuric acid with water, which is connected to a source of concentrated sulfuric acid and a source of water to mix and dilute concentrated sulfuric acid and dilution water. And a first cooler connected to the outlet of the first mixer to cool the diluted sulfuric acid from the first mixer, an outlet of the first cooler and the water supply source, and A second mixer that cools with a cooler and mixes sulfuric acid with dilution water from a water source to further dilute it, and cools the oleic sulfuric acid that is connected to the outlet of the second mixer and diluted with the second mixer An apparatus for producing oleic sulfuric acid, comprising: a second cooler.
第２クーラからの溥硫酸をさらに冷却する第３クーラを
さらに有することを特徴とする製造装置。3. The manufacturing apparatus according to claim 2, further comprising a third cooler that further cools the sulfuric acid from the second cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP31194391A JPH05124804A (en) | 1991-10-30 | 1991-10-30 | Production of dilute sulfuric acid and manufacturing equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP31194391A JPH05124804A (en) | 1991-10-30 | 1991-10-30 | Production of dilute sulfuric acid and manufacturing equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH05124804A true JPH05124804A (en) | 1993-05-21 |
Family
ID=18023305
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP31194391A Pending JPH05124804A (en) | 1991-10-30 | 1991-10-30 | Production of dilute sulfuric acid and manufacturing equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH05124804A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100792215B1 (en) * | 2006-05-25 | 2008-01-07 | 정석희 | Manufacturing apparatus of diluted sulfuric acid |
| CN105817175A (en) * | 2016-01-09 | 2016-08-03 | 郑州大学 | Automatic sulfuric acid blending system and control method |
| CN106830135A (en) * | 2017-02-14 | 2017-06-13 | 襄阳华虹高科新材料有限公司 | A kind of sulfuric acid complex acid cooling water recirculation system |
| CN107585744A (en) * | 2017-10-04 | 2018-01-16 | 山东胜星化工有限公司 | A kind of sulfuric acid concentration adjusting means |
| CN109433039A (en) * | 2018-12-14 | 2019-03-08 | 中冶焦耐(大连)工程技术有限公司 | A kind of coking industry sulfuric acid preparing process and equipment |
| CN109647236A (en) * | 2019-01-11 | 2019-04-19 | 中冶焦耐(大连)工程技术有限公司 | A kind of continuous preparing process of coking industry sulfuric acid and device |
-
1991
- 1991-10-30 JP JP31194391A patent/JPH05124804A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100792215B1 (en) * | 2006-05-25 | 2008-01-07 | 정석희 | Manufacturing apparatus of diluted sulfuric acid |
| CN105817175A (en) * | 2016-01-09 | 2016-08-03 | 郑州大学 | Automatic sulfuric acid blending system and control method |
| CN105817175B (en) * | 2016-01-09 | 2020-10-02 | 郑州大学 | Automatic sulfuric acid preparation system and control method |
| CN106830135A (en) * | 2017-02-14 | 2017-06-13 | 襄阳华虹高科新材料有限公司 | A kind of sulfuric acid complex acid cooling water recirculation system |
| CN107585744A (en) * | 2017-10-04 | 2018-01-16 | 山东胜星化工有限公司 | A kind of sulfuric acid concentration adjusting means |
| CN109433039A (en) * | 2018-12-14 | 2019-03-08 | 中冶焦耐(大连)工程技术有限公司 | A kind of coking industry sulfuric acid preparing process and equipment |
| CN109647236A (en) * | 2019-01-11 | 2019-04-19 | 中冶焦耐(大连)工程技术有限公司 | A kind of continuous preparing process of coking industry sulfuric acid and device |
| CN109647236B (en) * | 2019-01-11 | 2023-10-24 | 中冶焦耐(大连)工程技术有限公司 | Continuous preparation process and device for sulfuric acid in coking industry |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JPH05124804A (en) | Production of dilute sulfuric acid and manufacturing equipment | |
| US9988269B2 (en) | Method for producing peroxymonosulfuric acid and apparatus for continuously producing peroxymonosulfuric acid | |
| CN108250176A (en) | A kind of quick continuous flow synthesis technology of fluorinated ethylene carbonate | |
| US2969280A (en) | Process and apparatus for producing cooled aqueous ammonium phosphate fertilizer | |
| CN115938990A (en) | SPM solution mixed acid output control method | |
| CN105859581A (en) | New nitration technology used in production of 2-cyano-4-nitro chlorobenzene | |
| CN114455548A (en) | Method for continuously producing peroxysulfuric acid | |
| CN205146056U (en) | Novel emulsification device of integrated form | |
| CN111704553B (en) | Cyclic synthesis method of nitroaniline chloride | |
| CN211098943U (en) | Cooling system | |
| CN101553427A (en) | Process for producing monopersulfuric acid and monopersulfuric acid continuous production apparatus | |
| CN204714731U (en) | For the preparation of the equipment of aromatic dicarboxylic acid | |
| US5094833A (en) | High yield sodium hydrosulfite generation | |
| EP0377521B1 (en) | High yield sodium hydrosulfite generation | |
| JPS6045538A (en) | Alkane liquid phase oxidation | |
| US4220601A (en) | Process for the continuous manufacture of 3-nitro-4-acetylamino-toluene and corresponding apparatus | |
| CN110433755A (en) | A kind of method and apparatus that serialization prepares diazonium compound | |
| CN110893325A (en) | Device and method for preparing ozone water | |
| CN219186862U (en) | Process device for synthesizing sodium lauroyl sarcosinate | |
| CN205550204U (en) | Automatic complex acid system of sulphuric acid | |
| CN111106041A (en) | Wet etching machine table and recovery method of wet etching liquid medicine | |
| CN220496040U (en) | Concentrated sulfuric acid online dilution system | |
| CN217093443U (en) | Solvent rearrangement reaction system | |
| JPS5821825A (en) | Preparation of semiconductor treating solution | |
| JPH09162094A (en) | Method for diluting original developer |