WO2018090167A1 - Waste acid treatment process - Google Patents
Waste acid treatment process Download PDFInfo
- Publication number
- WO2018090167A1 WO2018090167A1 PCT/CN2016/105836 CN2016105836W WO2018090167A1 WO 2018090167 A1 WO2018090167 A1 WO 2018090167A1 CN 2016105836 W CN2016105836 W CN 2016105836W WO 2018090167 A1 WO2018090167 A1 WO 2018090167A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- acid
- waste acid
- waste
- liquid
- treatment process
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/03—Preparation from chlorides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G49/00—Compounds of iron
- C01G49/14—Sulfates
Definitions
- the invention belongs to the field of solar energy technology, and particularly relates to a waste acid treatment process.
- the acid utilization rate is very low, and a large amount of acid is discharged along with the acid wastewater. If the waste acid is discharged into the environment without treatment, it not only acidifies the water or soil, but also harms the ecological environment and wastes a lot of resources. In addition to being acidic, waste acid and acid waste water also contain a large amount of impurities.
- the waste acid containing ferrous chloride is treated, and the waste acid is generally concentrated by evaporation, and then the excess concentrated sulfuric acid is added while being heated, and then absorbed by the recovery purification tower, and the generated ferrous sulfate solution is then subjected to baking treatment, but this treatment is performed.
- the by-products obtained by the method are of low quality.
- the technical problem to be solved by the present invention is to provide a waste acid treatment process capable of producing high quality by-products and enabling recycling of spent acid after treatment.
- the technical solution of the present invention is: a waste acid treatment process, wherein the waste acid contains ferrous chloride
- the innovation is that the method includes the following steps: conveying the waste acid liquid generated by pickling to The impurities are removed by precipitation in the acid storage tank; the waste acid after removing impurities is sent to the three-effect evaporator group for evaporation and concentration, so that the content of ferrous chloride in the spent acid is increased, and the excess concentrated sulfuric acid is added in batches to make chlorine The chlorine in the ferrous iron is replaced; when the chlorine gas is volatilized, it is absorbed by the recovery tower to form a recyclable hydrochloric acid, and a ferrous sulfate solution is formed; the ferrous sulfate solution is sent to the regulating tank, and sulfuric acid is added to the sulfuric acid concentration.
- the waste acid solution in the conditioning tank is sent to the cooling crystallization tank, and the waste acid solution is stirred at a temperature of 0 to 5 degrees with a stirrer rotating at 60 to 70 rpm until The spent acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
- the waste acid treatment process of the present invention wherein the conventional evaporation is three-effect evaporation, thereby completely evaporating, capable of producing high quality by-products, and the regenerated acid after treatment can be recycled;
- the waste acid treatment process of the present invention is Before cooling and crystallization, the concentration of sulfuric acid in the spent acid is adjusted to 15% to 20%, and the temperature is controlled to be 0 to 5 degrees during the cooling crystallization process. Increasing the concentration of concentrated sulfuric acid and lowering the crystallization temperature can make the sulfuric acid The solubility of ferrous iron becomes small, and ferrous sulfate crystal grains are crystallized.
- the waste acid contains ferrous chloride, and the following steps are included:
- the waste acid solution produced by pickling is transported to the acid storage tank to remove impurities by precipitation; the waste acid after removing the impurities is sent to a 60-degree three-effect evaporator group for evaporation and concentration for 1.5 hours to make ferrous chloride in the spent acid.
- the excess concentrated sulfuric acid is added in batches to displace the chlorine in the ferrous chloride; when the chlorine gas is volatilized, it is absorbed by the recovery and purification tower to form a recyclable hydrochloric acid, and at the same time, a ferrous sulfate solution is formed;
- the ferrous solution is sent to the conditioning tank, and sulfuric acid is added to the sulfuric acid concentration of 15%; the waste acid liquid in the conditioning tank is sent to the cooling crystallization tank, and the waste is continuously stirred at a temperature of 5 degrees at a rate of 60 degrees per minute.
- the acid solution is not crystallized until the waste acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
- the waste acid contains ferrous chloride, and the following steps are included:
- the waste acid solution produced by pickling is transported to the acid storage tank to remove impurities by precipitation; the waste acid after removing impurities is sent to a 50-degree three-effect evaporator group for evaporation and concentration for 1.5 hours to make ferrous chloride in the spent acid.
- the excess concentrated sulfuric acid is added in batches to displace the chlorine in the ferrous chloride; when the chlorine gas is volatilized, it is absorbed by the recovery and purification tower to form a recyclable hydrochloric acid, and at the same time, a ferrous sulfate solution is formed;
- the ferrous solution is sent to the conditioning tank, and sulfuric acid is added to the sulfuric acid concentration of 20%; the waste acid liquid in the conditioning tank is sent to the cooling crystallization tank, and the waste acid is continuously stirred at a temperature of 0 degrees at a rate of 70 revolutions per minute.
- the liquid is not crystallized until the waste acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
- the waste acid contains ferrous chloride, and the following steps are included:
- the waste acid solution produced by pickling is transported to the acid storage tank to remove impurities by precipitation; the waste acid after removing impurities is sent to a 55-degree three-effect evaporator group for evaporation and concentration for 1.5 hours to make ferrous chloride in the spent acid.
- the excess concentrated sulfuric acid is added in batches to displace the chlorine in the ferrous chloride; when the chlorine gas is volatilized, it is absorbed by the recovery and purification tower to form a recyclable hydrochloric acid, and at the same time, a ferrous sulfate solution is formed;
- the ferrous solution is sent to the conditioning tank, and sulfuric acid is added to the sulfuric acid concentration of 17%; the waste acid liquid in the conditioning tank is sent to the cooling crystallization tank, and the waste acid is continuously stirred at a temperature of 3 degrees at a rate of 65 rpm.
- the liquid is not crystallized until the waste acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
- the content of sulfuric acid in the regenerated acid obtained by the waste acid treatment process of the invention is about 25 percent, which can meet the requirements of the pickling process, that is, the regenerated acid can be recycled; the obtained content of ferrous sulfate crystal grains exceeds 95 In addition, it can meet the quality standards of chemical products and has high economic value.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Removal Of Specific Substances (AREA)
Abstract
A waste acid treatment process, wherein waste acid contains ferrous chloride. The treatment process comprises the following steps: precipitating waste acid liquid produced by acid washing to remove impurities; sending waste acid having impurities removed into a three-effect evaporator group for evaporation and concentration; adding over-concentrated sulfuric acid in batches while hot such that chlorine in ferrous chloride is replaced; when chlorine gas is volatilized, generating reusable hydrochloric acid by means of absorption by a recovery and purification tower, while generating a ferrous sulfate solution; transferring the ferrous sulfate solution to an adjustment tank; adding sulfuric acid to send waste acid liquid in the adjustment tank to a cooling and crystallization tank; continuously stirring the waste acid liquid until the waste acid liquid no longer crystallizes; sending the crystallized waste acid liquid to a centrifugal separation device for solid-liquid separation so as to obtain ferrous sulfate crystals and a regenerated acid respectively. The advantages are that the treatment process may produce high quality by-products and reduce treatment costs of waste acid, and that acid regenerated following the treatment may be recycled.
Description
技术领域Technical field
本发明属于太阳能技术领域，特别涉及一种废酸处理工艺。 The invention belongs to the field of solar energy technology, and particularly relates to a waste acid treatment process.
背景技术Background technique
在太阳能生产过程中，酸的利用率很低，大量的酸随同酸废水排放出去。这些废酸如不经过处理而排放到环境中，不仅使水体或土壤酸化，对生态环境造成危害，而且浪费大量资源。废酸和酸性废水除具有酸性外，还含有大量的杂质。In the solar energy production process, the acid utilization rate is very low, and a large amount of acid is discharged along with the acid wastewater. If the waste acid is discharged into the environment without treatment, it not only acidifies the water or soil, but also harms the ecological environment and wastes a lot of resources. In addition to being acidic, waste acid and acid waste water also contain a large amount of impurities.
现有的一些企业针对上述现象，采用了比较简单的用含碱性材料对废酸中和处理，但由于废渣太多不易脱水，极易产生二次污染，且成本太高，因此这些设施基本上是处于半瘫痪状态。其他大部分企业均采用蒸发浓缩法进行废酸处理，由于副产品质量差、销路窄、运行成本太高，这些环保设施也是举步维艰。Some existing enterprises have adopted a relatively simple method of neutralizing waste acid with alkaline materials for the above phenomenon, but because the waste residue is too much to be dehydrated, it is easy to cause secondary pollution, and the cost is too high, so these facilities are basically The top is in a semi-squat state. Most other companies use the evaporation concentration method for waste acid treatment. Due to the poor quality of by-products, narrow sales and high operating costs, these environmental protection facilities are also difficult.
现在对含有氯化亚铁的废酸进行处理，一般将废酸蒸发浓缩，然后趁热加入过量浓硫酸，再经回收净化塔吸收，生成的硫酸亚铁溶液再通过焙烧处理，但这种处理方法得到的副产品质量低。Now, the waste acid containing ferrous chloride is treated, and the waste acid is generally concentrated by evaporation, and then the excess concentrated sulfuric acid is added while being heated, and then absorbed by the recovery purification tower, and the generated ferrous sulfate solution is then subjected to baking treatment, but this treatment is performed. The by-products obtained by the method are of low quality.
因此，研发一种能够产生高质量的副产品，而且能使处理后的废酸能够循环利用的废酸处理工艺是非常有必要的。 Therefore, it is necessary to develop a waste acid treatment process which can produce high quality by-products and which can recycle the spent acid after treatment.
发明内容Summary of the invention
本发明要解决的技术问题是提供一种能够产生高质量的副产品，而且能使处理后的废酸能够循环利用的废酸处理工艺。The technical problem to be solved by the present invention is to provide a waste acid treatment process capable of producing high quality by-products and enabling recycling of spent acid after treatment.
为解决上述技术问题，本发明的技术方案为：一种废酸处理工艺，所述废酸中含有氯化亚铁，其创新点在于：包括如下步骤：将酸洗产生的废酸液输送至储酸池内经沉淀除去杂质；将除去杂质后的废酸送入三效蒸发器组进行蒸发浓缩，使废酸内的氯化亚铁含量升高，趁热分批加入过量浓硫酸，使氯化亚铁中的氯被置换出来；氯气挥发出来时，经回收净化塔吸收生成可回用盐酸，同时生成硫酸亚铁溶液；将硫酸亚铁溶液输送至调节池，并加入硫酸至硫酸浓度为百分之15至百分之20；将调节池内的废酸液输送至冷却结晶罐，在0度至5度的温度下持续用转速为60至70转每分钟的搅拌机搅拌废酸液，直至废酸液不再结晶；将结晶后的废酸液输送至离心分离装置进行固液分离，分别得到硫酸亚铁晶粒和再生酸液。In order to solve the above technical problem, the technical solution of the present invention is: a waste acid treatment process, wherein the waste acid contains ferrous chloride, and the innovation is that the method includes the following steps: conveying the waste acid liquid generated by pickling to The impurities are removed by precipitation in the acid storage tank; the waste acid after removing impurities is sent to the three-effect evaporator group for evaporation and concentration, so that the content of ferrous chloride in the spent acid is increased, and the excess concentrated sulfuric acid is added in batches to make chlorine The chlorine in the ferrous iron is replaced; when the chlorine gas is volatilized, it is absorbed by the recovery tower to form a recyclable hydrochloric acid, and a ferrous sulfate solution is formed; the ferrous sulfate solution is sent to the regulating tank, and sulfuric acid is added to the sulfuric acid concentration. 15% to 20%; the waste acid solution in the conditioning tank is sent to the cooling crystallization tank, and the waste acid solution is stirred at a temperature of 0 to 5 degrees with a stirrer rotating at 60 to 70 rpm until The spent acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
本发明的优点在于：The advantages of the invention are:
本发明的废酸处理工艺，其中，该传统的蒸发为三效蒸发，因而使蒸发完全，能够产生高质量的副产品，且处理后的再生酸还能循环利用；本发明的废酸处理工艺在冷却结晶前将废酸中硫酸的浓度调配为15百分之至20百分之，并在冷却结晶过程中将温度控制在0度至5度，增加浓硫酸浓度和降低结晶温度都能使得硫酸亚铁的溶解度变小，结晶出硫酸亚铁晶粒。The waste acid treatment process of the present invention, wherein the conventional evaporation is three-effect evaporation, thereby completely evaporating, capable of producing high quality by-products, and the regenerated acid after treatment can be recycled; the waste acid treatment process of the present invention is Before cooling and crystallization, the concentration of sulfuric acid in the spent acid is adjusted to 15% to 20%, and the temperature is controlled to be 0 to 5 degrees during the cooling crystallization process. Increasing the concentration of concentrated sulfuric acid and lowering the crystallization temperature can make the sulfuric acid The solubility of ferrous iron becomes small, and ferrous sulfate crystal grains are crystallized.
具体实施方式detailed description
下面的实施例可以使本专业的技术人员更全面地理解本发明，但并不因此将本发明限制在所述的实施例范围之中。The following examples are intended to provide a fuller understanding of the invention, and are not intended to limit the invention.
实施例1Example 1
本实施例废酸处理工艺，废酸中含有氯化亚铁，包括如下步骤：In the waste acid treatment process of the embodiment, the waste acid contains ferrous chloride, and the following steps are included:
将酸洗产生的废酸液输送至储酸池内经沉淀除去杂质；将除去杂质后的废酸送入60度的三效蒸发器组进行蒸发浓缩1.5h，使废酸内的氯化亚铁含量升高，趁热分批加入过量浓硫酸，使氯化亚铁中的氯被置换出来；氯气挥发出来时，经回收净化塔吸收生成可回用盐酸，同时生成硫酸亚铁溶液；将硫酸亚铁溶液输送至调节池，并加入硫酸至硫酸浓度为百分之15；将调节池内的废酸液输送至冷却结晶罐，在5度的温度下以60度转每分钟的速率持续搅拌废酸液，直至废酸液不再结晶；将结晶后的废酸液输送至离心分离装置进行固液分离，分别得到硫酸亚铁晶粒和再生酸液。The waste acid solution produced by pickling is transported to the acid storage tank to remove impurities by precipitation; the waste acid after removing the impurities is sent to a 60-degree three-effect evaporator group for evaporation and concentration for 1.5 hours to make ferrous chloride in the spent acid. When the content is increased, the excess concentrated sulfuric acid is added in batches to displace the chlorine in the ferrous chloride; when the chlorine gas is volatilized, it is absorbed by the recovery and purification tower to form a recyclable hydrochloric acid, and at the same time, a ferrous sulfate solution is formed; The ferrous solution is sent to the conditioning tank, and sulfuric acid is added to the sulfuric acid concentration of 15%; the waste acid liquid in the conditioning tank is sent to the cooling crystallization tank, and the waste is continuously stirred at a temperature of 5 degrees at a rate of 60 degrees per minute. The acid solution is not crystallized until the waste acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
实施例2Example 2
本实施例废酸处理工艺，废酸中含有氯化亚铁，包括如下步骤：In the waste acid treatment process of the embodiment, the waste acid contains ferrous chloride, and the following steps are included:
将酸洗产生的废酸液输送至储酸池内经沉淀除去杂质；将除去杂质后的废酸送入50度的三效蒸发器组进行蒸发浓缩1.5h，使废酸内的氯化亚铁含量升高，趁热分批加入过量浓硫酸，使氯化亚铁中的氯被置换出来；氯气挥发出来时，经回收净化塔吸收生成可回用盐酸，同时生成硫酸亚铁溶液；将硫酸亚铁溶液输送至调节池，并加入硫酸至硫酸浓度为百分之20；将调节池内的废酸液输送至冷却结晶罐，在0度的温度下以70转每分钟的速率持续搅拌废酸液，直至废酸液不再结晶；将结晶后的废酸液输送至离心分离装置进行固液分离，分别得到硫酸亚铁晶粒和再生酸液。The waste acid solution produced by pickling is transported to the acid storage tank to remove impurities by precipitation; the waste acid after removing impurities is sent to a 50-degree three-effect evaporator group for evaporation and concentration for 1.5 hours to make ferrous chloride in the spent acid. When the content is increased, the excess concentrated sulfuric acid is added in batches to displace the chlorine in the ferrous chloride; when the chlorine gas is volatilized, it is absorbed by the recovery and purification tower to form a recyclable hydrochloric acid, and at the same time, a ferrous sulfate solution is formed; The ferrous solution is sent to the conditioning tank, and sulfuric acid is added to the sulfuric acid concentration of 20%; the waste acid liquid in the conditioning tank is sent to the cooling crystallization tank, and the waste acid is continuously stirred at a temperature of 0 degrees at a rate of 70 revolutions per minute. The liquid is not crystallized until the waste acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
实施例3Example 3
本实施例废酸处理工艺，废酸中含有氯化亚铁，包括如下步骤：In the waste acid treatment process of the embodiment, the waste acid contains ferrous chloride, and the following steps are included:
将酸洗产生的废酸液输送至储酸池内经沉淀除去杂质；将除去杂质后的废酸送入55度的三效蒸发器组进行蒸发浓缩1.5h，使废酸内的氯化亚铁含量升高，趁热分批加入过量浓硫酸，使氯化亚铁中的氯被置换出来；氯气挥发出来时，经回收净化塔吸收生成可回用盐酸，同时生成硫酸亚铁溶液；将硫酸亚铁溶液输送至调节池，并加入硫酸至硫酸浓度为百分之17；将调节池内的废酸液输送至冷却结晶罐，在3度的温度下以65转每分钟的速率持续搅拌废酸液，直至废酸液不再结晶；将结晶后的废酸液输送至离心分离装置进行固液分离，分别得到硫酸亚铁晶粒和再生酸液。The waste acid solution produced by pickling is transported to the acid storage tank to remove impurities by precipitation; the waste acid after removing impurities is sent to a 55-degree three-effect evaporator group for evaporation and concentration for 1.5 hours to make ferrous chloride in the spent acid. When the content is increased, the excess concentrated sulfuric acid is added in batches to displace the chlorine in the ferrous chloride; when the chlorine gas is volatilized, it is absorbed by the recovery and purification tower to form a recyclable hydrochloric acid, and at the same time, a ferrous sulfate solution is formed; The ferrous solution is sent to the conditioning tank, and sulfuric acid is added to the sulfuric acid concentration of 17%; the waste acid liquid in the conditioning tank is sent to the cooling crystallization tank, and the waste acid is continuously stirred at a temperature of 3 degrees at a rate of 65 rpm. The liquid is not crystallized until the waste acid solution is no longer crystallized; the spent acid solution after crystallization is sent to a centrifugal separation device for solid-liquid separation to obtain ferrous sulfate crystal grains and a regenerated acid solution, respectively.
本发明的废酸处理工艺处理得到的再生酸中硫酸的含量为25百分之左右，可满足酸洗工序的要求，即再生酸可循环利用；得到的硫酸亚铁晶粒的含量超过95百分之，能够达到化工产品质量标准，具有很高的经济价值。The content of sulfuric acid in the regenerated acid obtained by the waste acid treatment process of the invention is about 25 percent, which can meet the requirements of the pickling process, that is, the regenerated acid can be recycled; the obtained content of ferrous sulfate crystal grains exceeds 95 In addition, it can meet the quality standards of chemical products and has high economic value.
本行业的技术人员应该了解，本发明不受上述实施例的限制，上述实施例和说明书中描述的只是说明本发明的原理，在不脱离本发明精神和范围的前提下，本发明还会有各种变化和改进，这些变化和改进都落入要求保护的本发明范围内。本发明要求保护范围由所附的权利要求书及其等效物界定。
It should be understood by those skilled in the art that the present invention is not limited by the foregoing embodiments, and that the present invention is only described in the foregoing description and the description of the present invention, without departing from the spirit and scope of the invention. Various changes and modifications are intended to be included within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and their equivalents.
Claims (1)
- 一种废酸处理工艺，所述废酸中含有氯化亚铁，其特征在于：包括如下步骤：将酸洗产生的废酸液输送至储酸池内经沉淀除去杂质；将除去杂质后的废酸送入三效蒸发器组进行蒸发浓缩，使废酸内的氯化亚铁含量升高，趁热分批加入过量浓硫酸，使氯化亚铁中的氯被置换出来；氯气挥发出来时，经回收净化塔吸收生成可回用盐酸，同时生成硫酸亚铁溶液；将硫酸亚铁溶液输送至调节池，并加入硫酸至硫酸浓度为百分之15至百分之20；将调节池内的废酸液输送至冷却结晶罐，在0度至5度的温度下持续用转速为60至70转每分钟的搅拌机搅拌废酸液，直至废酸液不再结晶；将结晶后的废酸液输送至离心分离装置进行固液分离，分别得到硫酸亚铁晶粒和再生酸液。A waste acid treatment process, wherein the waste acid contains ferrous chloride, which comprises the steps of: transporting the waste acid liquid produced by pickling to an acid storage tank to remove impurities by precipitation; and removing waste after removing impurities The acid is sent to the three-effect evaporator group for evaporation and concentration, so that the ferrous chloride content in the spent acid is increased, and the excess concentrated sulfuric acid is added in batches to remove the chlorine in the ferrous chloride; when the chlorine gas is volatilized The recovered purification tower absorbs and generates recyclable hydrochloric acid, and simultaneously generates a ferrous sulfate solution; the ferrous sulfate solution is sent to the regulating tank, and sulfuric acid is added to the sulfuric acid concentration of 15 to 20 percent; The waste acid liquid is sent to the cooling crystallization tank, and the waste acid liquid is continuously stirred by a mixer rotating at 60 to 70 rpm at a temperature of 0 to 5 degrees until the waste acid liquid is no longer crystallized; the spent acid liquid after crystallization The mixture is sent to a centrifugal separator for solid-liquid separation to obtain ferrous sulfate grains and a regenerated acid solution, respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CN2016/105836 WO2018090167A1 (en) | 2016-11-15 | 2016-11-15 | Waste acid treatment process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CN2016/105836 WO2018090167A1 (en) | 2016-11-15 | 2016-11-15 | Waste acid treatment process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| WO2018090167A1 true WO2018090167A1 (en) | 2018-05-24 |
Family
ID=62145955
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/CN2016/105836 WO2018090167A1 (en) | 2016-11-15 | 2016-11-15 | Waste acid treatment process |
Country Status (1)
| Country | Link |
|---|---|
| WO (1) | WO2018090167A1 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113149082A (en) * | 2021-04-29 | 2021-07-23 | 斯瑞尔环境科技股份有限公司 | Method for producing high-purity ferrous sulfate water and ferrous sulfate heptahydrate by using waste acid |
| CN114604901A (en) * | 2022-03-20 | 2022-06-10 | 深圳市长隆科技有限公司 | Method for treating waste acid generated in dye sulfonation |
| CN114671421A (en) * | 2022-04-29 | 2022-06-28 | 中国科学院过程工程研究所 | Method and system for preparing iron phosphate by recycling iron-containing hydrochloric acid pickling waste liquid |
| CN115232645A (en) * | 2022-08-17 | 2022-10-25 | 山东沾化阳光化学有限公司 | Refining process and equipment for recovering hydrochloric acid in chlorinated paraffin production process |
| CN116143179A (en) * | 2022-09-09 | 2023-05-23 | 河北圣雪大成制药有限责任公司 | Method for preparing ferrous sulfate for Fenton oxidation by using oxytetracycline hydrochloride waste acid |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10273326A (en) * | 1997-03-28 | 1998-10-13 | Nittetsu Mining Co Ltd | Production of ferrous sulfate or iron polysulfate having high purity from waste hydrochloric acid containing ferrous compound |
| US20050281732A1 (en) * | 2004-06-22 | 2005-12-22 | Alexander Kehrmann | Method of producing ferrous sulfate heptahydrate |
| CN1803656A (en) * | 2006-01-24 | 2006-07-19 | 杨淙垣 | Regeneration treatment method of steel sheet pickling waste liquor |
| CN105110540A (en) * | 2015-08-28 | 2015-12-02 | 新兴铸管股份有限公司 | Recovery treatment method of galvanizing pickling waste hydrochloric acid |
| CN105776139A (en) * | 2016-03-16 | 2016-07-20 | 江苏双能太阳能有限公司 | Waste acid treatment process |
-
2016
- 2016-11-15 WO PCT/CN2016/105836 patent/WO2018090167A1/en active Application Filing
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10273326A (en) * | 1997-03-28 | 1998-10-13 | Nittetsu Mining Co Ltd | Production of ferrous sulfate or iron polysulfate having high purity from waste hydrochloric acid containing ferrous compound |
| US20050281732A1 (en) * | 2004-06-22 | 2005-12-22 | Alexander Kehrmann | Method of producing ferrous sulfate heptahydrate |
| CN1803656A (en) * | 2006-01-24 | 2006-07-19 | 杨淙垣 | Regeneration treatment method of steel sheet pickling waste liquor |
| CN105110540A (en) * | 2015-08-28 | 2015-12-02 | 新兴铸管股份有限公司 | Recovery treatment method of galvanizing pickling waste hydrochloric acid |
| CN105776139A (en) * | 2016-03-16 | 2016-07-20 | 江苏双能太阳能有限公司 | Waste acid treatment process |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113149082A (en) * | 2021-04-29 | 2021-07-23 | 斯瑞尔环境科技股份有限公司 | Method for producing high-purity ferrous sulfate water and ferrous sulfate heptahydrate by using waste acid |
| CN114604901A (en) * | 2022-03-20 | 2022-06-10 | 深圳市长隆科技有限公司 | Method for treating waste acid generated in dye sulfonation |
| CN114671421A (en) * | 2022-04-29 | 2022-06-28 | 中国科学院过程工程研究所 | Method and system for preparing iron phosphate by recycling iron-containing hydrochloric acid pickling waste liquid |
| CN114671421B (en) * | 2022-04-29 | 2023-10-10 | 中国科学院过程工程研究所 | Method and system for preparing ferric phosphate by utilizing ferric acid pickling waste liquid resource |
| CN115232645A (en) * | 2022-08-17 | 2022-10-25 | 山东沾化阳光化学有限公司 | Refining process and equipment for recovering hydrochloric acid in chlorinated paraffin production process |
| CN116143179A (en) * | 2022-09-09 | 2023-05-23 | 河北圣雪大成制药有限责任公司 | Method for preparing ferrous sulfate for Fenton oxidation by using oxytetracycline hydrochloride waste acid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2018090167A1 (en) | Waste acid treatment process | |
| CN102249262B (en) | Concentration and cold-precipitation separation method of sodium sulfate and ammonium sulfate from vanadium-precipitation mother liquor high-salt wastewater | |
| CN106865571B (en) | Method for preparing sodium bicarbonate and ammonium sulfate from chemical concentrated brine | |
| JP5466749B2 (en) | Vanadium oxide production wastewater treatment method | |
| CN105776139A (en) | Waste acid treatment process | |
| CN110227702B (en) | Method for preparing flux by using chemical waste salt | |
| CN106185989A (en) | The method reclaiming inorganic salt in one way of life incineration of refuse flyash | |
| CN113105138A (en) | Method and system for water washing dechlorination of waste incineration fly ash and evaporation mass-separation crystallization of water washing liquid | |
| CN110550680B (en) | Method for preventing multi-effect concentration and one-effect scaling of titanium dioxide waste acid produced by sulfuric acid process | |
| CN109607503A (en) | Phosphatic abraum salt recycling processing method | |
| CN103402917A (en) | Method and device for recovering boric acid | |
| CN104495953A (en) | Process for treating industrial waste hydrochloric acid in recycling way through salt fractionation method | |
| WO2018000730A1 (en) | Treatment method for resource recycling of hexavalent chromium-containing residues | |
| WO2016110081A1 (en) | Acid waste gas treatment and resource utilization | |
| WO2014194791A1 (en) | Method for processing sulphur paste as by-product from coke oven coal gas desulphuration | |
| CN112225242A (en) | Resourceful treatment device and process for mother liquor generated by reaction of waste incineration fly ash and hydrochloric acid | |
| CN106277005A (en) | A kind of recovery cryolite, calcium carbonate and method of sodium sulfate from calcium fluoride sludge resource | |
| CN100357176C (en) | Method for recovering vitriol from waste vitrol containing metal salt | |
| CN116199377B (en) | Incineration fly ash resource utilization method for quality control of washing waste salt | |
| CN113800539A (en) | Process for purifying and recovering salt in wet-process leaching solution of overhaul residues | |
| CN109336138A (en) | The separation method of potassium sodium in a kind of mixed sulfate containing potassium and sodium | |
| CN101973650A (en) | Closed circulation method for sodium hypochlorite waste water treatment of acetylene purification process in polyvinyl chloride (PVC) production by calcium carbide method | |
| CN107162935A (en) | The recovery method of phosphorus-containing compound in useless chemical polishing agent | |
| CN103819042A (en) | Purification treatment method for hydrochloric acid waste liquid | |
| CN113526542B (en) | Method for removing fluorine and chlorine in zinc sulfate solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| 121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 16921469 Country of ref document: EP Kind code of ref document: A1 |
|
| NENP | Non-entry into the national phase |
Ref country code: DE |
|
| 122 | Ep: pct application non-entry in european phase |
Ref document number: 16921469 Country of ref document: EP Kind code of ref document: A1 |