JPS6379720A - Production of aqueous anmonium sulfate - Google Patents
Production of aqueous anmonium sulfateInfo
- Publication number
- JPS6379720A JPS6379720A JP22325786A JP22325786A JPS6379720A JP S6379720 A JPS6379720 A JP S6379720A JP 22325786 A JP22325786 A JP 22325786A JP 22325786 A JP22325786 A JP 22325786A JP S6379720 A JPS6379720 A JP S6379720A
- Authority
- JP
- Japan
- Prior art keywords
- sulfuric acid
- reaction
- reaction tank
- ammonia
- water
- 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
- 238000004519 manufacturing process Methods 0.000 title claims description 8
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 title abstract 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 83
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 230000005484 gravity Effects 0.000 claims abstract description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 65
- 229910021529 ammonia Inorganic materials 0.000 claims description 32
- 239000000243 solution Substances 0.000 claims description 28
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 24
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 24
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 24
- 239000012295 chemical reaction liquid Substances 0.000 claims description 12
- 239000007864 aqueous solution Substances 0.000 claims description 5
- 239000002994 raw material Substances 0.000 abstract description 5
- 230000003472 neutralizing effect Effects 0.000 abstract description 3
- 239000002253 acid Substances 0.000 abstract description 2
- 238000007664 blowing Methods 0.000 abstract description 2
- 230000006835 compression Effects 0.000 abstract 1
- 238000007906 compression Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 8
- 239000000047 product Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 238000001514 detection method Methods 0.000 description 3
- ZFSLODLOARCGLH-UHFFFAOYSA-N isocyanuric acid Chemical compound OC1=NC(O)=NC(O)=N1 ZFSLODLOARCGLH-UHFFFAOYSA-N 0.000 description 3
- 239000012452 mother liquor Substances 0.000 description 3
- 239000013078 crystal Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000002452 interceptive effect Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
Description
【発明の詳細な説明】
産業上の利用分野
この発明は濃度約３８％以上、好ましくは３８ないし４
０％の硫安水を工業的規模で連続的に製造する方法に関
するものであり、本発明方法によれば、反応の自動制御
によって著しい省力化を図ることができ、また系外に放
出する排ガス中のアンモニアを皆無とし、環境汚染防止
に大きく寄与することができる。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application This invention is suitable for use in a concentration of about 38% or higher, preferably between 38% and 4%.
This invention relates to a method for continuously producing 0% ammonium sulfate water on an industrial scale. According to the method of the present invention, it is possible to achieve significant labor savings through automatic control of the reaction, and there is no This eliminates all ammonia and greatly contributes to the prevention of environmental pollution.
従来の技術
硫酸水溶液にアンモニア含有ガスを反応させて硫安水を
製造する工業的な方法は、反応系のＰＨを測定し゛自動
制御の手段によって、アンモニアの供給量に見合う硫酸
を添加させるものであった。Conventional technology The industrial method of producing ammonium sulfate water by reacting an ammonia-containing gas with an aqueous sulfuric acid solution involves measuring the pH of the reaction system and adding sulfuric acid in an amount corresponding to the amount of ammonia supplied by means of automatic control. Ta.
発明が解決しようとする問題点
しかしながら、従来法によればアンモニア含有ガスの濃
度あるいは温度に変化を伴う場合、反応液中の水分蒸発
量が大幅に変化し、硫安水を所定濃度として取り出すこ
とが極めて困難であった。Problems to be Solved by the Invention However, according to the conventional method, when the concentration or temperature of the ammonia-containing gas changes, the amount of water evaporation in the reaction solution changes significantly, making it difficult to extract ammonium sulfate water at a predetermined concentration. It was extremely difficult.
硫安水の望ましい濃度は３８ないし４０％の範囲であり
、これ以上の濃度になると結晶が析出し、反応槽内や移
送配管に閉塞トラブルを生じ、連続的な運転に支障を来
すものであり、また硫安水の濃度が３８％を下田ると濃
縮や輸送に要する費用が増加して実用性に欠ける難点が
あった。The desirable concentration of ammonium sulfate is in the range of 38 to 40%; if the concentration is higher than this, crystals will precipitate, causing blockage problems in the reaction tank and transfer piping, and hindering continuous operation. Moreover, if the concentration of ammonium sulfate water was 38%, the cost required for concentration and transportation would increase, making it impractical.
さらに、原料としてシアヌル酸製造工程等において生じ
る硫酸排液のように、酸濃度が低く且つバラツキがある
ものを用いる場合には、硫酸原料の供給量を自動制御す
るのに、極めて複雑な制御機構を要するものであった。Furthermore, when using raw materials with low and variable acid concentrations, such as sulfuric acid wastewater generated in the cyanuric acid manufacturing process, an extremely complex control mechanism is required to automatically control the supply amount of the sulfuric acid raw materials. It required
問題点を解決するための手段
本発明者等は、このような事情に鑑み種々の試験研究を
重ねた結果、硫酸水溶液にアンモニア含有ガスを接触さ
せて硫安水を製造するに当り、硫酸水溶液を貯留しこれ
に主たるアンモニア含有ガス及び追加の硫酸と水を供給
して反応させる第一反応槽において、反応液の電導度測
定値を信号として取り出し、これを硫酸の供給系に連動
させて反応液の電導度を常に０．４５ないし０．４６ｖ
／ｃｍの範囲に維持し、且つ該反応液の比重測定値を信
号として取り出し、これを水の供給系に連動させて反応
液の比重を常に１．２１ないし１．２３ｇ／ｃｃの範囲
に保持し、このようにして生じた第一反応槽の硫安と未
反応硫酸を含む反応液を第二反応槽に導き、第二反応槽
においてその反応液中にアンモニア含有ガスを供給して
残存する未反応硫酸を中和し、第二反応槽において生じ
るアンモニア含有排ガスを第一反応槽に供給させること
によって所期の目的を達成したものである。Means for Solving the Problems In view of the above circumstances, the inventors of the present invention have conducted various tests and researches, and as a result, when producing ammonium sulfate water by bringing an ammonia-containing gas into contact with a sulfuric acid aqueous solution, In the first reaction tank where the main ammonia-containing gas and additional sulfuric acid and water are stored and reacted, the measured value of the electrical conductivity of the reaction liquid is taken out as a signal, and this is linked to the sulfuric acid supply system. conductivity of always 0.45 to 0.46v
The specific gravity of the reaction solution is maintained within the range of 1.21 to 1.23 g/cc by taking out the measured value of the specific gravity of the reaction solution as a signal and linking this to the water supply system. Then, the reaction solution containing ammonium sulfate and unreacted sulfuric acid in the first reaction tank thus generated is led to the second reaction tank, and ammonia-containing gas is supplied into the reaction solution in the second reaction tank to remove the remaining unreacted sulfuric acid. The intended purpose was achieved by neutralizing the reacted sulfuric acid and supplying the ammonia-containing exhaust gas generated in the second reaction tank to the first reaction tank.
本発明方法の実施に当たっては、第一反応槽における反
応液の電導度を常に０．４５ないし０．４６ｖ／ａｍの
範囲に維持すべきであり、その電導度がこれより低い″
場合には、反応液中に含まれる硫酸が少なくなってアン
モニアの吸収を十分に為し得す、排ガス中に未反応アン
モニアが同伴する惧れがあり、また電導度がこの範囲を
土建る場合には、生じた硫安水中の硫酸が多くなり、第
二反応槽で未反応硫酸をアンモニア含有ガスで中和させ
る工程が複雑になり、且つ第二反応槽から取り出す硫安
水の濃度を所定の範囲に保つことが難しい。When carrying out the method of the present invention, the electrical conductivity of the reaction solution in the first reaction tank should always be maintained in the range of 0.45 to 0.46 v/am, and the electrical conductivity should be lower than this range.
In some cases, the amount of sulfuric acid contained in the reaction solution decreases and ammonia can be absorbed sufficiently, or there is a risk that unreacted ammonia will be entrained in the exhaust gas, and if the conductivity exceeds this range. In this case, the amount of sulfuric acid in the generated ammonium sulfate solution increases, and the process of neutralizing unreacted sulfuric acid with ammonia-containing gas in the second reaction tank becomes complicated, and the concentration of ammonium sulfate solution taken out from the second reaction tank is limited to a predetermined range. difficult to maintain.
第一反応槽における反応液の比重は常に１．２１ないし
１．２３ｇ／ｃｃの範囲に維持すべきであり、反応液の
比重がこれより小さい場合には、第二反応槽から取り出
す硫安水の濃度が下がり、これを濃縮して固型硫安を製
造する際の熱効率を低下させ、またその反応液の比重が
これより大きい場合には、反応液中の硫安濃度が増加し
て結晶の析出が起こり、これが反応槽や移送配管の壁面
等に付着して閉塞トラブルを生じ、連続的な操業に支障
を来す惧れがある。The specific gravity of the reaction liquid in the first reaction tank should always be maintained in the range of 1.21 to 1.23 g/cc, and if the specific gravity of the reaction liquid is lower than this, the ammonium sulfate solution taken out from the second reaction tank should be The concentration decreases, reducing the thermal efficiency when concentrating it to produce solid ammonium sulfate, and if the specific gravity of the reaction solution is greater than this, the ammonium sulfate concentration in the reaction solution increases and crystals precipitate. There is a risk that this will adhere to the walls of the reaction tank or transfer piping, causing clogging problems, and interfering with continuous operation.
本発明の実施において、シアヌル酸製造工程等において
生じる低濃度の硫酸含有排液を原料とする場合は、これ
を第一反応槽の母液として用いるかあるいは追加する水
の供給系から導入して使用すべきである。In the practice of the present invention, when a low-concentration sulfuric acid-containing wastewater generated in the cyanuric acid production process is used as a raw material, it is used as the mother liquor of the first reaction tank or introduced from the additional water supply system. Should.
また第二反応槽において生じた硫安水は、通常ＰＨが７
ないしｌＯの範囲となるので、必要に応じてこれに少量
の硫酸を加えて製品のＰＨを調整すれば良い。In addition, the ammonium sulfate water produced in the second reaction tank usually has a pH of 7.
The pH of the product can be adjusted by adding a small amount of sulfuric acid, if necessary.
作用
本発明方法によれば、硫酸水溶液にアンモニア含有ガス
を反応させて硫安水を製造するに当り、第一反応槽にお
ける反応液の電導度を検出し、これが０．４５ないし０
．４６ｖ／ｃｓ＋の範囲になるように制御して追加の硫
酸を供給しているため、アンモニア含有ガスの導入によ
って硫酸が消費されると、その消費量に相当する硫酸が
直ちに供給され、反応系には常に約４ないし５％の硫酸
が存在して、第一反応槽における排ガス中の未反応アン
モニアを皆無とすることができ、且つ第一反応槽におけ
る反応液の比重を測定し、これが１．２１ないし１゜２
３ｇ７ｃｃとなるように制御して追加の水を供給してい
るため、第一反応槽の反応液は、常に硫安の濃度を約３
３ないし３４％の範囲に保たれ、これを第二反応槽に導
き、アンモニア含有ガスによって未反応硫酸を中和すれ
ば、所期の約３８ないし４０％濃度の硫安水に容易に転
換させることができる。According to the method of the present invention, when producing ammonium sulfate water by reacting a sulfuric acid aqueous solution with an ammonia-containing gas, the electrical conductivity of the reaction solution in the first reaction tank is detected, and the electrical conductivity is determined to be between 0.45 and 0.
．． Additional sulfuric acid is supplied under control to be within the range of 46v/cs+, so when sulfuric acid is consumed by introducing ammonia-containing gas, sulfuric acid equivalent to the consumed amount is immediately supplied to the reaction system. About 4 to 5% sulfuric acid is always present, so that there is no unreacted ammonia in the exhaust gas in the first reaction tank, and the specific gravity of the reaction liquid in the first reaction tank is measured, and this is 1. 21 to 1°2
Since additional water is controlled to be 3g7cc, the reaction solution in the first reaction tank always has an ammonium sulfate concentration of about 3g.
If the concentration is maintained in the range of 3 to 34%, and this is led to the second reaction tank and the unreacted sulfuric acid is neutralized with ammonia-containing gas, it can be easily converted to ammonium sulfate water with the desired concentration of about 38 to 40%. Can be done.
実施例
本発明方法の実施に適する製造装置の一例を図面によっ
て説明する。EXAMPLE An example of a manufacturing apparatus suitable for carrying out the method of the present invention will be explained with reference to the drawings.
第一反応槽（１１は硫酸を含む反応液を循環ポンプ（２
）によってリサイクルさせ、これを噴霧させてアンモニ
ア含有ガスと接触させるアンモニア吸収塔であり、この
反応槽には反応液の循環経路に、電導度肝（３）の検出
部及び密度計（４）の検出部を設置し、該電導度肝の測
定値を信号として取り出し、濃硫酸の自動制御バルブ（
５）を反応液の電導度に応じて開閉させ、且つ密度計（
４）の測定値を信号として取り出し、水あるいは低濃度
硫酸水溶液の自動制御バルブ（６）を反応液の比重に応
じて開閉させたものである。アンモニア含有ガスは供給
ファン（７）によって第一反応槽（１）に導入させ、第
一反応槽＋１１において生じた反応液は順次循環ポンプ
（８）によってアンモニア吹込管を備えた第二反応槽（
９）に供給し、アンモニア含有ガスの一部を加圧供給フ
ァンａ・によって第二反応槽（９）に吹き込み第二反応
槽におけるアンモニアを含む未反応ガスを第一反応槽（
１）に導いたものである。The first reaction tank (11 is a circulation pump (2) that circulates the reaction solution containing sulfuric acid.
), which is recycled by ammonia gas, is sprayed and brought into contact with an ammonia-containing gas, and this reaction tank is equipped with a conductivity meter (3) detection unit and a density meter (4) detection unit in the reaction liquid circulation path. The measured value of the conductivity is taken out as a signal, and the concentrated sulfuric acid automatic control valve (
5) is opened and closed depending on the conductivity of the reaction solution, and the density meter (
The measured value of 4) is taken out as a signal, and an automatic control valve (6) for water or a low concentration sulfuric acid aqueous solution is opened and closed depending on the specific gravity of the reaction liquid. Ammonia-containing gas is introduced into the first reaction tank (1) by a supply fan (7), and the reaction liquid produced in the first reaction tank +11 is sequentially transferred to a second reaction tank (1) equipped with an ammonia blowing pipe by a circulation pump (8).
9), a part of the ammonia-containing gas is blown into the second reaction tank (9) by a pressurized supply fan a, and the unreacted gas containing ammonia in the second reaction tank is transferred to the first reaction tank (9).
This led to 1).
図中、αυは調圧弁、亜は製品ポンプを示す。In the figure, αυ indicates a pressure regulating valve, and sub indicates a product pump.
次に前記装置を用いて、シアヌル酸製造工程において生
じたアンモニア含有ガス及び硫酸排液を原料とする硫安
水の製造について説明する。Next, the production of ammonium sulfate water using the ammonia-containing gas and sulfuric acid waste liquid produced in the cyanuric acid production process as raw materials will be explained using the above-mentioned apparatus.
第一反応槽（１）に硫酸１１．４％を含む硫酸排液１５
５ｋｇを母液として投入し、これを循環ポンプ（２）に
よってリサイクルさせながら、アンモニアを平均６．５
ｗ／ｖ％含有するガスを、供給ファン（７）によって１
時間当り４００ｍ’の割合で第一反応槽（１）及び第二
反応槽（９）に導き、電導度肝（３）の検出信号によっ
て反応液の電導度が０．４５ないし０．４６Ｖ／（Ｊｌ
の範囲となるように自動制御バルブ（５）を作動させて
９８％濃度の硫酸を継続的に供給し、且つ密度計（４）
の検出信号によって反応液の比重が１．２１ないし１．
２３ｇ／ＣＣの範囲となるように自動制御バルブ（６）
を作動させて前記母液と同じ濃度の低い硫酸水溶液を継
続的に供給した。Sulfuric acid wastewater 15 containing 11.4% sulfuric acid in the first reaction tank (1)
5 kg of mother liquor is input, and while this is recycled by the circulation pump (2), an average of 6.5 kg of ammonia is added.
The gas containing 1% w/v is supplied by the supply fan (7) to 1
The conductivity of the reaction solution is 0.45 to 0.46 V/(Jl) by introducing the reaction solution into the first reaction tank (1) and the second reaction tank (9) at a rate of 400 m' per hour.
The automatic control valve (5) is operated to continuously supply sulfuric acid with a concentration of 98%, and the density meter (4)
Depending on the detection signal, the specific gravity of the reaction solution is between 1.21 and 1.21.
Automatic control valve (6) to maintain a range of 23g/CC
was operated to continuously supply an aqueous sulfuric acid solution with the same low concentration as the mother liquor.
また第一反応槽（１）において生じた反応液は循環ポン
プ（８）によって、第二反応槽（９）に順次移送し、ア
ンモニア含有ガスの一部を加圧供給ファンαφによって
第二反応槽（９）に吹き込み、第二反応槽（９）におけ
る反応液のＰＲが７ないし１０となる迄で中和し、未反
応アンモニアを含む排ガスを第一反応槽（１）に導き、
第二反応槽（９）の反応液を製品ポンプαυによって取
り出し、硫安水として回収した。In addition, the reaction liquid generated in the first reaction tank (1) is sequentially transferred to the second reaction tank (9) by a circulation pump (8), and a part of the ammonia-containing gas is transferred to the second reaction tank by a pressurized supply fan αφ. (9), neutralize the reaction solution in the second reaction tank (9) until the PR becomes 7 to 10, and guide the exhaust gas containing unreacted ammonia to the first reaction tank (1).
The reaction liquid in the second reaction tank (9) was taken out by the product pump αυ and recovered as ammonium sulfate water.
このような反応操作を２４時間継続したところ、第一反
応槽において生じる湿排気ガス中には、６６ｋｇ／時間
の水を含みいずれの時間においもアンモニアは検出され
ず、その間に供給した９８％硫酸は１１３７ｋｇ、 １
１．４％の硫酸排液は６０００ｋｇ、アンモニアは６２
４ｋｇであり、製品として取り出された硫安水の濃度は
３８．３ないし３９．８％の範囲であり、平均３９．２
％の硫安水を６１８０ｋｇ得た。When such a reaction operation was continued for 24 hours, the humid exhaust gas generated in the first reaction tank contained 66 kg/hour of water, and no ammonia was detected at any time. is 1137kg, 1
1.4% sulfuric acid waste water is 6000 kg, ammonia is 62
4 kg, and the concentration of ammonium sulfate taken out as a product ranged from 38.3 to 39.8%, with an average of 39.2%.
% ammonium sulfate solution was obtained.
なお、この収量は理論値に相当するものであった。Note that this yield corresponded to the theoretical value.
発明の効果
この発明の方法によれば、硫酸水溶液にアンモニア含有
ガスを接触させて約３８ないし４０％濃度の硫安水を製
造する工程を自動制御によって円滑に操作することがで
き、且つ反応系外に放出される排ガス中に含まれるアン
モニアを皆無として、作業環境改善をしうるなど実践面
の効果は顕著である。Effects of the Invention According to the method of the present invention, the process of bringing an ammonia-containing gas into contact with an aqueous sulfuric acid solution to produce an aqueous ammonium sulfate solution having a concentration of about 38 to 40% can be smoothly operated by automatic control. The practical effects are significant, such as eliminating ammonia contained in the exhaust gas emitted by the system, improving the working environment.
Claims (1)
製造するに当り、硫酸水溶液を貯留しこれに主たるアン
モニア含有ガス及び追加の硫酸と水を供給して反応させ
る第一反応槽において、反応液の電導度測定値を信号と
して取り出し、これを硫酸の供給系に連動させて反応液
の電導度を常に０．４５ないし０．４６ｖ／ｃｍの範囲
に維持し、且つ該反応液の比重測定値を信号として取り
出し、これを水の供給系に連動させて反応液の比重を常
に１．２１ないし１．２３ｇ／ｃｃの範囲に保持し、こ
のようにして生じた第一反応槽の硫安と未反応硫酸を含
む反応液を第二反応槽に導き、第二反応槽においてその
反応液中にアンモニア含有ガスを供給して残存する未反
応硫酸を中和し、第二反応槽において生じるアンモニア
含有排ガスを第一反応槽に供給させることを特徴とする
硫安水の製造法。When producing ammonium sulfate water by bringing an ammonia-containing gas into contact with a sulfuric acid aqueous solution, the reaction solution is heated in a first reaction tank in which the sulfuric acid aqueous solution is stored and reacted by supplying the main ammonia-containing gas and additional sulfuric acid and water. The measured value of conductivity is taken out as a signal, and this is linked to the sulfuric acid supply system to maintain the conductivity of the reaction liquid in the range of 0.45 to 0.46 v/cm, and the measured value of specific gravity of the reaction liquid is This is taken out as a signal and linked to the water supply system to maintain the specific gravity of the reaction liquid in the range of 1.21 to 1.23 g/cc. The reaction solution containing sulfuric acid is introduced into the second reaction tank, and the remaining unreacted sulfuric acid is neutralized by supplying ammonia-containing gas into the reaction solution in the second reaction tank, and the ammonia-containing exhaust gas generated in the second reaction tank is A method for producing ammonium sulfate water, which comprises supplying ammonium sulfate water to a first reaction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22325786A JPS6379720A (en) | 1986-09-19 | 1986-09-19 | Production of aqueous anmonium sulfate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22325786A JPS6379720A (en) | 1986-09-19 | 1986-09-19 | Production of aqueous anmonium sulfate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6379720A true JPS6379720A (en) | 1988-04-09 |
Family
ID=16795265
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP22325786A Pending JPS6379720A (en) | 1986-09-19 | 1986-09-19 | Production of aqueous anmonium sulfate |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6379720A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439174A (en) * | 2015-12-19 | 2016-03-30 | 鄄城康泰化工有限公司 | Preparation method of ammonium sulfate |
-
1986
- 1986-09-19 JP JP22325786A patent/JPS6379720A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439174A (en) * | 2015-12-19 | 2016-03-30 | 鄄城康泰化工有限公司 | Preparation method of ammonium sulfate |
| CN105439174B (en) * | 2015-12-19 | 2018-02-02 | 鄄城康泰化工有限公司 | A kind of preparation method of ammonium sulfate |
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