CN103160321A - Method and equipment for continuously refining liquid paraffin by virtue of by-product hydrochloric acid during chlorinated paraffin production - Google Patents
Method and equipment for continuously refining liquid paraffin by virtue of by-product hydrochloric acid during chlorinated paraffin production Download PDFInfo
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- CN103160321A CN103160321A CN201310110616XA CN201310110616A CN103160321A CN 103160321 A CN103160321 A CN 103160321A CN 201310110616X A CN201310110616X A CN 201310110616XA CN 201310110616 A CN201310110616 A CN 201310110616A CN 103160321 A CN103160321 A CN 103160321A
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Abstract
The invention belongs to the technical field of fine chemistry, and relates to a method and equipment for refining raw material liquid paraffin and by-product hydrochloric acid simultaneously during a continuous production process for chlorinated paraffin, wherein the equipment is an extraction tower. The method comprises the following steps of: continuously and manually extracting the by-product hydrochloric acid and the raw material liquid paraffin generated during the continuous production process for chlorinated paraffin, so as to improve the purity of the liquid paraffin entering in a chlorination reaction phase; and reacting the raw material liquid paraffin with free chlorine in the hydrochloric acid, so as to reduce the concentration of the free chlorine in the by-product hydrochloric acid. According to the method and the equipment disclosed by the invention, via the mutual extraction and reaction of the by-product hydrochloric acid and the raw material liquid paraffin, the contents of aromatic hydrocarbon, basic nitrogen, mechanical impurities and water in the liquid paraffin are reduced, the purity of the raw material liquid paraffin is improved, and then the colour of the chlorinated paraffin product is improved, and the colour numbers of platinum and cobalt are reduced to be less than 100; simultaneously, the raw material liquid paraffin can be reacted with the free chlorine in the by-product hydrochloric acid, so that the quality of the by-product hydrochloric acid is improved, and the content of the free chlorine in the by-product hydrochloric acid is reduced to 0.006 from about 0.015 originally after extraction.
Description
Technical field
The invention belongs to the fine chemical technology field, related to a kind of method and apparatus of in the continuous chloroparaffin production process, stock liquid wax and by-product hydrochloric acid being made with extra care simultaneously, this equipment is a kind of extraction tower.
Background technology
in recent years, along with widening of the use of clorafin, domestic clorafin industrial scale constantly enlarges, but using at present state's production fluid wax (is mainly the aromatic hydrocarbons of minute quantity in liquid wax as the product that raw material production goes out because of quality problem, basic nitrogen and moisture), color and luster can't reach the level of making of imported raw material liquid wax, general platinum cobalt look is number in the 100-120 left and right, and in the HG2092-1991 standard, the platinum cobalt look of premium grads number must not be greater than 100, use control color that the production of import liquid wax can make the clorafin product in platinum cobalt look numbers No. 80, in addition because of clorafin in process of production, chlorine can not fully react with liquid wax, carry a small amount of chlorine in the hydrogen chloride tail gas that produces in reaction process secretly and entered acid making system, cause having in the clorafin by-product hydrochloric acid more free chlorine to exist, limited the use occasion of hydrochloric acid.
Summary of the invention
The present invention seeks to for the problems referred to above, and a kind of method and apparatus that utilizes by-product hydrochloric acid continuous treating liquid wax in clorafin production that proposes.
Main technical schemes of the present invention: the method for utilizing by-product hydrochloric acid continuous treating liquid wax in clorafin production, it is characterized in that by-product hydrochloric acid and the stock liquid wax that will produce in continuous processing clorafin production process carry out continuously extraction mutually in extraction tower, improve and enter the purity that chlorinationization is answered stage liquid wax, utilize simultaneously the free chlorine in stock liquid wax and hydrochloric acid to react, reduce the concentration of by-product hydrochloric acid free chlorine.
Usually, in the method for the invention, the chlorination system of clorafin and acid making system are continuous; Under the finished product by-product hydrochloric acid, the liquid mouth is higher than extraction tower.
Described stock liquid wax and by-product hydrochloric acid are by entering extraction tower in the middle part of extraction tower, stock liquid wax and by-product hydrochloric acid are in the extraction mutually of extraction tower middle part, moisture in stock liquid wax is taken away by hydrochloric acid, aromatic hydrocarbons, basic nitrogen and other mechanical impurity and hydrochloric acid produce the reaction postprecipitation at the bottom of the extraction tower tower, and the most of free chlorine in hydrochloric acid is taken away by liquid wax; Liquid wax after extraction enters the chlorination reaction still from extraction tower top and carries out chlorination reaction, and the hydrochloric acid after the extraction free chlorine directly enters finished product hydrochloric acid tank field from the extraction tower bottom; Extraction tower top gas phase is connected with acid making system tail gas, and a small amount of waste liquid is by extraction tower bottom discharge.
The described equipment of the inventive method is extraction tower, the extraction tower middle part is provided with stock liquid wax and by-product hydrochloric acid import and the liquidometer mouth corresponding with this entrance location, the top of extraction tower is provided with the liquid wax outlet after making with extra care, the bottom of extraction tower is provided with the hydrochloric acid outlet after making with extra care, the extraction tower top is provided with gaseous phase outlet, and extraction tower bottom is provided with the valve of discharging waste liquid.
Advantage of the present invention is, mutual extraction and reaction in extraction tower reduced aromatic hydrocarbons in liquid wax by by-product hydrochloric acid and raw material liq paraffin, basic nitrogen, the content of mechanical impurity and moisture, improved the purity of liquid wax stock, and then improved the color and luster of clorafin product, platinum cobalt look number is reduced in No. 100, simultaneously stock liquid wax can with by-product hydrochloric acid in free chlorine react, reduced the free chlorine content in the by-product hydrochloric acid, improved the quality of by-product hydrochloric acid, the hydrochloric acid free chlorine content after extraction is reduced to 0.006 by 0.015 original left and right.
Description of drawings
Fig. 1 is the connection diagram of embodiment of the present invention method and apparatus.
In figure, the A-gaseous phase outlet; Liquid wax outlet after B-is refining; The import of C-by-product hydrochloric acid; The import of the original liquid wax of D-; Hydrochloric acid outlet after E-is refining; The F-valve; G1, G2-liquidometer mouth.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in detail.
Embodiment: in the present embodiment method, the chlorination system of clorafin and acid making system are continuous, and under the finished product by-product acid, the liquid mouth must be higher than extraction tower.
As shown in Figure 1, stock liquid wax enters in tower from extraction tower D mouth, by-product hydrochloric acid is entered in tower by extraction tower C mouth, stock liquid wax and by-product hydrochloric acid cross between C mouth and D mouth and extract mutually, moisture in stock liquid wax is taken away by acid, aromatic hydrocarbons and other mechanical impurity produce the reaction postprecipitation at the bottom of the extraction tower tower with hydrochloric acid here, and the most of free chlorine in hydrochloric acid is taken away by liquid wax.
Whiteruss after extraction enters the chlorination reaction still from the B mouth and carries out chlorination reaction, and the hydrochloric acid after the extraction free chlorine directly enters finished product hydrochloric acid tank field.
Extraction tower top gas phase is connected with acid making system tail gas.
Regularly open F mouth valve at the bottom of tower according to the quality of liquid wax and check what of precipitated impurities in F mouth valve lower-glass is shown on trial, and in time discharge, a small amount of waste liquid of discharge needs collect and press specially the national environmental protection standardized treatment of being correlated with.
Because the proportion of whiteruss is that the proportion of 0.75-0.79 and by-product hydrochloric acid is at 1.12-1.14, self-assembling formation monooleate separation surface after whiteruss and hydrochloric acid cross in extraction tower, this separation surface is followed according to two kinds of tintometric variations, the more stable a certain position that is between liquidometer mouth G1-G2.
In chlorination process, a small amount of aromatic hydrocarbons that contains in whiteruss and basic nitrogen generate coloring matter through series reaction, become the most important factor of clorafin color and luster that affects.By-product hydrochloric acid free chlorine content is larger, makes quality product be difficult to reach the salable product requirement.Before chlorination, in the mutual extraction process of whiteruss and by-product hydrochloric acid, aromatic hydrocarbons and free chlorine, basic nitrogen and hydrochloric acid reaction, whiteruss and by-product hydrochloric acid are all played the effect of purification, and its resultant density is all greater than the density of hydrochloric acid, therefore be easy to be sunken to tower bottom, the bottom isolate is discharged system by sewage draining exit.
Test by embodiment and show, the platinum cobalt look of the clorafin of producing with the refined whiteruss of the inventive method number is decreased to 80 ~ No. 100 by original 100 ~ No. 120, and the content of hydrochloric acid free chlorine is reduced to 0.006 by original 0.015, and quality product is improved significantly.
Claims (4)
1. method of utilizing by-product hydrochloric acid continuous treating liquid wax in clorafin production, it is characterized in that by-product hydrochloric acid and the stock liquid wax that will produce in continuous processing clorafin production process carry out continuously extraction mutually in extraction tower, improve the purity that enters chlorination reaction stage liquid wax, reduce simultaneously the concentration of by-product hydrochloric acid free chlorine.
2. the method for claim 1, is characterized in that the chlorination system of clorafin and acid making system are continuous; Under the finished product by-product hydrochloric acid, the liquid mouth is higher than extraction tower.
3. method as claimed in claim 1 or 2, it is characterized in that stock liquid wax and by-product hydrochloric acid are by entering extraction tower in the middle part of extraction tower, stock liquid wax and by-product hydrochloric acid are in the extraction mutually of extraction tower middle part, moisture in stock liquid wax is taken away by hydrochloric acid, aromatic hydrocarbons, basic nitrogen and other mechanical impurity and hydrochloric acid produce the reaction postprecipitation at the bottom of the extraction tower tower, and the most of free chlorine in hydrochloric acid is taken away by liquid wax; Liquid wax after extraction enters the chlorination reaction still from extraction tower top and carries out chlorination reaction, and the hydrochloric acid after the extraction free chlorine directly enters finished product hydrochloric acid tank field from the extraction tower bottom; Extraction tower top gas phase is connected with acid making system tail gas, and a small amount of waste liquid is by extraction tower bottom discharge.
4. equipment that utilizes by-product hydrochloric acid continuous treating liquid wax in clorafin production, it is characterized in that described equipment is extraction tower, the extraction tower middle part is provided with stock liquid wax and by-product hydrochloric acid import and the liquidometer mouth corresponding with this entrance location, the top of extraction tower is provided with the liquid wax outlet after making with extra care, the bottom of extraction tower is provided with the hydrochloric acid outlet after making with extra care, the extraction tower top is provided with gaseous phase outlet, and extraction tower bottom is provided with the valve of discharging waste liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310110616XA CN103160321A (en) | 2013-04-01 | 2013-04-01 | Method and equipment for continuously refining liquid paraffin by virtue of by-product hydrochloric acid during chlorinated paraffin production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310110616XA CN103160321A (en) | 2013-04-01 | 2013-04-01 | Method and equipment for continuously refining liquid paraffin by virtue of by-product hydrochloric acid during chlorinated paraffin production |
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| CN103160321A true CN103160321A (en) | 2013-06-19 |
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| CN201310110616XA Pending CN103160321A (en) | 2013-04-01 | 2013-04-01 | Method and equipment for continuously refining liquid paraffin by virtue of by-product hydrochloric acid during chlorinated paraffin production |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103353500A (en) * | 2013-07-12 | 2013-10-16 | 深圳信测标准技术服务股份有限公司 | Detection method for medium short-chain chlorinated paraffin in plastic and environment |
| CN105296004A (en) * | 2015-09-18 | 2016-02-03 | 丹阳市助剂化工厂有限公司 | Processing technology for chlorinated paraffin |
| CN106800950A (en) * | 2015-11-25 | 2017-06-06 | 衡阳市骏杰化工有限公司 | A kind of refined production technology of atoleine |
| CN106833743A (en) * | 2017-03-30 | 2017-06-13 | 河北大景大搪化工设备有限公司 | A kind of serialization purifies the device of Paraffin liquid heavy |
| CN108707476A (en) * | 2018-05-02 | 2018-10-26 | 南京国威化工有限公司 | The method and apparatus of by-product hydrochloric acid continuous treating liquid wax is used in a kind of chlorinated paraffin |
| 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 |
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|---|---|---|---|---|
| CN1033643A (en) * | 1987-12-18 | 1989-07-05 | 楼存宝 | Automatically circulation formula continuous processing is produced clorafin and chlorocarbon technology and main device |
| CN101054535A (en) * | 2007-05-16 | 2007-10-17 | 泸州市宏成化工有限公司 | Method for producing chloroparaffin |
| CN102145251A (en) * | 2011-01-06 | 2011-08-10 | 鲁西化工集团股份有限公司氯碱化工分公司 | Dechloridation device and process in chlorinated paraffin production process |
| CN102888245A (en) * | 2012-09-19 | 2013-01-23 | 沁阳市海世鸿工贸有限责任公司 | Method and device for refining liquid paraffin |
-
2013
- 2013-04-01 CN CN201310110616XA patent/CN103160321A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1033643A (en) * | 1987-12-18 | 1989-07-05 | 楼存宝 | Automatically circulation formula continuous processing is produced clorafin and chlorocarbon technology and main device |
| CN101054535A (en) * | 2007-05-16 | 2007-10-17 | 泸州市宏成化工有限公司 | Method for producing chloroparaffin |
| CN102145251A (en) * | 2011-01-06 | 2011-08-10 | 鲁西化工集团股份有限公司氯碱化工分公司 | Dechloridation device and process in chlorinated paraffin production process |
| CN102888245A (en) * | 2012-09-19 | 2013-01-23 | 沁阳市海世鸿工贸有限责任公司 | Method and device for refining liquid paraffin |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103353500A (en) * | 2013-07-12 | 2013-10-16 | 深圳信测标准技术服务股份有限公司 | Detection method for medium short-chain chlorinated paraffin in plastic and environment |
| CN105296004A (en) * | 2015-09-18 | 2016-02-03 | 丹阳市助剂化工厂有限公司 | Processing technology for chlorinated paraffin |
| CN105296004B (en) * | 2015-09-18 | 2017-02-01 | 丹阳市助剂化工厂有限公司 | Processing technology for chlorinated paraffin |
| CN106800950A (en) * | 2015-11-25 | 2017-06-06 | 衡阳市骏杰化工有限公司 | A kind of refined production technology of atoleine |
| CN106833743A (en) * | 2017-03-30 | 2017-06-13 | 河北大景大搪化工设备有限公司 | A kind of serialization purifies the device of Paraffin liquid heavy |
| CN108707476A (en) * | 2018-05-02 | 2018-10-26 | 南京国威化工有限公司 | The method and apparatus of by-product hydrochloric acid continuous treating liquid wax is used in a kind of chlorinated paraffin |
| 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 |
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Application publication date: 20130619 |