CN105296004A - Processing technology for chlorinated paraffin - Google Patents
Processing technology for chlorinated paraffin Download PDFInfo
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- CN105296004A CN105296004A CN201510615260.4A CN201510615260A CN105296004A CN 105296004 A CN105296004 A CN 105296004A CN 201510615260 A CN201510615260 A CN 201510615260A CN 105296004 A CN105296004 A CN 105296004A
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Abstract
The invention relates to a processing technology for chlorinated paraffin. A chlorinated paraffin product is obtained by using wax oil and chlorine as raw materials and adopting a seven-stage continuous photo-thermal catalytic chlorination process and a bubbling degassing technology. The processing technology for the chlorinated paraffin, which is disclosed by the invention, comprises the following steps of: liquid chlorine gasification, chlorination and chlorinated tail gas adsorption. The processing technology which is disclosed by the invention is simple, is short in reaction time, and is high in conversion rate; production cost is reduced; economic benefits of enterprises are increased.
Description
Technical field
The present invention relates to a kind of preparation method of auxiliary agent, specifically a kind of complete processing of clorafin.
Background technology
Clorafin is the chlorinated derivatives of paraffinic hydrocarbon, advantages such as having low volatility, fire-retardant, electrical insulating property is good, be inexpensive, be widely used in production CABLE MATERIALS, the goods such as plate, flexible pipe, leatheroid, rubber.At present, domestic production technology of chlorinated paraffin mainly contains 3 kinds: thermal chlorination, catalysis method, photocatalytic method, but often kind of method just can obtain clorafin finished product after all needing multiple step reaction, and long reaction time, cost are high, and complex process.
Summary of the invention
In order to solve the problem, the invention provides one and utilizing wax oil and chlorine to be raw material, by 7 grades of continuous photo-thermal catalytic chlorination techniques, bubbling Degassing Technology obtains the complete processing of clorafin product.
In order to achieve the above object, the present invention is achieved by the following technical solutions:
The present invention is a kind of complete processing of clorafin, and described complete processing comprises the steps:
(1) liquid chlorine vaporizing: open liquid chlorine gasifier capable inlet valve, add water to full liquid level, open steam heating water, control water temperature not higher than 45 DEG C, open liquid chlorine tank car liquid outlet valve, liquid chlorine passes into liquid chlorine gasifier capable and gasifies, and gasification chlorine enters Chlorine Buffer Vessel, controlling Chlorine Buffer Vessel pressure is 0.35Mpa, and in surge tank, chlorine is for chloridizing unit;
(2) chlorination reaction: from the raw material wax oil of tank area, workshop wax oil scale tank is squeezed into through wax oil discharging pump, three grades of stills of checking on are squeezed into again through workshop wax oil pump, three grades of stills of checking on utilize the liquid level discrepancy in elevation to flow to check on still, one-level of secondary from three grades of stills of checking on successively and to check on still and extract clean washing tower, carry out intersecting mixing with the concentrated hydrochloric acid in the clean washing tower of extraction, the micro-hydrochloric acid in extraction wax oil, clean washing tower is suitable for reading to be flow in the first chlorination tank by extracting to extract wax oil in clean washing tower, wax oil scale tank discharging pump between opening vehicle, wax oil enters three grades of stills of checking on through under meter, the liquid level discrepancy in elevation is utilized to flow into the first chlorination tank, wax oil flows into the second chlorination tank from the first chlorination tank, tri-chlorination still is flowed into again from the second chlorination tank, the 4th chlorination tank is flowed into again from tri-chlorination still, phosphoric still is flowed into again from the 4th chlorination tank, the 6th chlorination tank is flowed into again from phosphoric still, the 7th chlorination tank is flowed into again from the 6th chlorination tank, 7th chlorination tank clorafin enters clorafin Receiving bin,
Open chlorine feed valve, control the first chlorination tank chlorine flowrate, second chlorination tank chlorine flowrate, tri-chlorination still chlorine flowrate, 4th chlorination tank chlorine flowrate, phosphoric still chlorine flowrate, 6th chlorination tank chlorine flowrate, 7th chlorination tank chlorine flowrate, the tri-chlorination of routine test simultaneously still, phosphoric still, 7th chlorination tank chlorine density, control density at 1.21 ~ 1.23g/ml, according to the logical chlorine dose of density adjustment, control chlorination tank temperature at 95 DEG C ~ 110 DEG C, when more than 110 DEG C, turn down chlorine feed amount, and reduce wax oil inlet amount simultaneously, regulate cooling water circulation amount simultaneously,
The hydrogen chloride gas produced in production process and do not complete reaction chlorine after the first cyclonic separator is separated, liquid enters the 7th chlorination tank, gas removes one-level graphite film-falling absorption tower absorbing hydrogen chloride gas, one-level graphite film-falling absorption tower gas out enters one-level and checks in still and absorb chlorine, one-level check on still gas out through second cyclonic separator be separated after enter secondary graphite film-falling absorption tower absorbing hydrogen chloride gas, secondary graphite film-falling absorption tower gas out by squirt pump enter secondary check on still absorb chlorine, secondary still gas out of checking on enters one-level packed absorber absorbing hydrogen chloride gas, one-level packed absorber gas out enters three grades of stills of checking on by squirt pump and absorbs chlorine, three grades of still gases out of checking on enter dilute acid bath absorbing hydrogen chloride gas by squirt pump, dilute acid bath gas out enters secondary packing tower absorbing hydrogen chloride gas, and secondary packing tower gas is out by emptying,
Open discharge pump, the clorafin in clorafin Receiving bin is squeezed into degassed still, after about 90 minutes, adds stablizer, obtained finished product clorafin, degassed still gas is out through degassed tempering tower, and enter three grades of packing towers and absorb, finished product clorafin squeezes into finished product storage tank through discharge pump.
Further improvement of the present invention is: hydrogen chloride tail gas of the present invention absorbs the technique being mainly divided into two covers different:
The chlorine produced in clorafin production process absorbs through one-level graphite film-falling absorption tower through hydrogen chloride tail gas, secondary graphite film-falling absorption tower absorbs, one-level packing tower absorbs, secondary packing tower absorbs, three grades of packing towers absorb and obtain byproduct hydrochloric acid, and by-product hydrochloric acid squeezes into hydrochloric acid tank through concentrated hydrochloric acid pump;
Or the hydrogen chloride gas produced in clorafin production process and unreacted chlorine remove one-level rinse bath after the second cyclonic separator is separated, after washing, liquid removes the first chlorination tank, tail gas removes secondary rinse bath, liquid after washing is beaten to one-level washing tower through washing pump, tail gas absorbs through one-level graphite film-falling absorption tower, secondary graphite film-falling absorption tower absorbs, one-level packing tower absorbs, secondary packing tower absorbs, three grades of packing towers absorb and obtain byproduct hydrochloric acid, and by-product hydrochloric acid part squeezes into hydrochloric acid tank through concentrated hydrochloric acid pump.
The invention has the beneficial effects as follows: clorafin provided by the invention only needs an one-step chlorination reaction namely to obtain finished product, and its reaction principle is as follows: reaction equation:
with wax oil and chlorine for raw material, adopt 7 grades of continuous photo-thermal catalytic chlorination techniques, bubbling Degassing Technology, obtain clorafin product, preparation process comprises liquid chlorine vaporizing, chlorination reaction and chlorinated exhaust and absorbs, the production of clorafin have employed the continuous production processes that the whole nation is more advanced at present, 7 chlorination tanks are adopted to be cascaded, utilize the principle of liquid level differential pressure, starting material paraffin oil flows to the second chlorination tank from the first chlorination tank, until flow to the 7th chlorination tank, and the 7th chlorination tank is finished product clorafin; 7 chlorination tanks all lead to the chlorine of different flow, react with the paraffin oil in chlorination tank, until the paraffin oil in the 7th chlorination tank reaches the quality standard of product, the discharge method of finished product clorafin becomes continuity discharging; The absorption of chlorinated exhaust is also the domestic more advanced principle of absorption adopted at present, be called three grades check on, Pyatyi absorb, check on as 3m3,4m3,6m3 tri-enamel reaction stills for three grades, mainly play the chlorine absorbing non-complete reaction in chlorinated exhaust, accomplish chlorine qualified discharge; Pyatyi is absorbed as two graphite falling film absorption and three packing material absorbings, and absorption agent is tap water, absorbs the hydrogen chloride gas that chlorination reaction goes out, and makes technical hydrochloric acid, accomplishes hydrogen chloride gas qualified discharge.The discharge method of hydrochloric acid becomes continuity discharging.
Complete processing of the present invention is simple, and the reaction times is short, and transformation efficiency is high, reduces production cost, improves the economic benefit of enterprise.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
In order to deepen the understanding of the present invention, be described in further detail the present invention below in conjunction with drawings and Examples, this embodiment, only for explaining the present invention, not forming protection scope of the present invention and limiting.
As shown in Figure 1, the present invention is a kind of complete processing of clorafin, and described complete processing comprises the steps:
(1) liquid chlorine vaporizing: open liquid chlorine gasifier capable inlet valve, add water to full liquid level, open steam heating water, control water temperature not higher than 45 DEG C, open liquid chlorine tank car liquid outlet valve, liquid chlorine passes into liquid chlorine gasifier capable, namely coil pipe gasifier gasifies, gasification chlorine enters Chlorine Buffer Vessel, and controlling Chlorine Buffer Vessel pressure is 0.35Mpa, and in surge tank, chlorine is for chloridizing unit;
(2) chlorination reaction: from the raw material wax oil of tank area, workshop wax oil scale tank is squeezed into through wax oil discharging pump, three grades of stills of checking on are squeezed into again through workshop wax oil pump, three grades of stills of checking on utilize the liquid level discrepancy in elevation to flow to check on still, one-level of secondary from three grades of stills of checking on successively and to check on still and extract clean washing tower, carry out intersecting mixing with the concentrated hydrochloric acid in the clean washing tower of extraction, the micro-hydrochloric acid in extraction wax oil, clean washing tower is suitable for reading to be flow in the first chlorination tank by extracting to extract wax oil in clean washing tower, wax oil scale tank discharging pump between opening vehicle, wax oil enters three grades of stills of checking on through under meter, the liquid level discrepancy in elevation is utilized to flow into the first chlorination tank, wax oil flows into the second chlorination tank from the first chlorination tank, tri-chlorination still is flowed into again from the second chlorination tank, the 4th chlorination tank is flowed into again from tri-chlorination still, phosphoric still is flowed into again from the 4th chlorination tank, the 6th chlorination tank is flowed into again from phosphoric still, the 7th chlorination tank is flowed into again from the 6th chlorination tank, 7th chlorination tank clorafin enters clorafin Receiving bin,
Open chlorine feed valve, control the first chlorination tank chlorine flowrate, second chlorination tank chlorine flowrate, tri-chlorination still chlorine flowrate, 4th chlorination tank chlorine flowrate, phosphoric still chlorine flowrate, 6th chlorination tank chlorine flowrate, 7th chlorination tank chlorine flowrate, the tri-chlorination of routine test simultaneously still, phosphoric still, 7th chlorination tank chlorine density, control density at 1.21 ~ 1.23g/ml, according to the logical chlorine dose of density adjustment, control chlorination tank temperature at 95 DEG C ~ 110 DEG C, when more than 110 DEG C, turn down chlorine feed amount, and reduce wax oil inlet amount simultaneously, regulate cooling water circulation amount simultaneously,
The hydrogen chloride gas produced in production process and do not complete reaction chlorine after the first cyclonic separator is separated, liquid enters the 7th chlorination tank, gas removes one-level graphite film-falling absorption tower absorbing hydrogen chloride gas, one-level graphite film-falling absorption tower gas out enters one-level and checks in still and absorb chlorine, one-level check on still gas out through second cyclonic separator be separated after enter secondary graphite film-falling absorption tower absorbing hydrogen chloride gas, secondary graphite film-falling absorption tower gas out by squirt pump enter secondary check on still absorb chlorine, secondary still gas out of checking on enters one-level packed absorber absorbing hydrogen chloride gas, one-level packed absorber gas out enters three grades of stills of checking on by squirt pump and absorbs chlorine, three grades of still gases out of checking on enter dilute acid bath absorbing hydrogen chloride gas by squirt pump, dilute acid bath gas out enters secondary packing tower absorbing hydrogen chloride gas, and secondary packing tower gas is out by emptying,
Open discharge pump, clorafin in clorafin Receiving bin is squeezed into degassed still, degassed still can be that two degassed stills be set up in parallel carry out simultaneously, stablizer is added after about 90 minutes, obtained finished product clorafin, degassed still gas is out through degassed tempering tower, and enter three grades of packing towers and absorb, finished product clorafin squeezes into finished product storage tank through discharge pump.
In clorafin machining process of the present invention, hydrogen chloride tail gas absorbs the device being divided into two covers different, specific as follows:
The chlorine produced in clorafin production process absorbs through one-level graphite film-falling absorption tower through hydrogen chloride tail gas, secondary graphite film-falling absorption tower absorbs, one-level packing tower absorbs, secondary packing tower absorbs, three grades of packing towers absorb and obtain byproduct hydrochloric acid, and by-product hydrochloric acid squeezes into hydrochloric acid tank through concentrated hydrochloric acid pump;
Or the hydrogen chloride gas produced in clorafin production process and unreacted chlorine remove one-level rinse bath after the second cyclonic separator is separated, after washing, liquid removes the first chlorination tank, tail gas removes secondary rinse bath, liquid after washing is beaten to one-level washing tower through washing pump, tail gas absorbs through one-level graphite film-falling absorption tower, secondary graphite film-falling absorption tower absorbs, one-level packing tower absorbs, secondary packing tower absorbs, three grades of packing towers absorb and obtain byproduct hydrochloric acid, and by-product hydrochloric acid part squeezes into hydrochloric acid tank through concentrated hydrochloric acid pump.
Claims (2)
1. a complete processing for clorafin, is characterized in that: described complete processing comprises the steps:
(1) liquid chlorine vaporizing: open liquid chlorine gasifier capable inlet valve, add water to full liquid level, open steam heating water, control water temperature not higher than 45 DEG C, open liquid chlorine tank car liquid outlet valve, liquid chlorine passes into liquid chlorine gasifier capable and gasifies, and gasification chlorine enters Chlorine Buffer Vessel, controlling Chlorine Buffer Vessel pressure is 0.35Mpa, and in surge tank, chlorine is for chloridizing unit;
(2) chlorination reaction: from the raw material wax oil of tank area, workshop wax oil scale tank is squeezed into through wax oil discharging pump, three grades of stills of checking on are squeezed into again through workshop wax oil pump, three grades of stills of checking on utilize the liquid level discrepancy in elevation to flow to check on still, one-level of secondary from three grades of stills of checking on successively and to check on still and extract clean washing tower, carry out intersecting mixing with the concentrated hydrochloric acid in the clean washing tower of extraction, the micro-hydrochloric acid in extraction wax oil, clean washing tower is suitable for reading to be flow in the first chlorination tank by extracting to extract wax oil in clean washing tower, wax oil scale tank discharging pump between opening vehicle, wax oil enters three grades of stills of checking on through under meter, the liquid level discrepancy in elevation is utilized to flow into the first chlorination tank, wax oil flows into the second chlorination tank from the first chlorination tank, tri-chlorination still is flowed into again from the second chlorination tank, the 4th chlorination tank is flowed into again from tri-chlorination still, phosphoric still is flowed into again from the 4th chlorination tank, the 6th chlorination tank is flowed into again from phosphoric still, the 7th chlorination tank is flowed into again from the 6th chlorination tank, 7th chlorination tank clorafin enters clorafin Receiving bin,
Open chlorine feed valve, control the first chlorination tank chlorine flowrate, second chlorination tank chlorine flowrate, tri-chlorination still chlorine flowrate, 4th chlorination tank chlorine flowrate, phosphoric still chlorine flowrate, 6th chlorination tank chlorine flowrate, 7th chlorination tank chlorine flowrate, the tri-chlorination of routine test simultaneously still, phosphoric still, 7th chlorination tank chlorine density, control density at 1.21 ~ 1.23g/ml, according to the logical chlorine dose of density adjustment, control chlorination tank temperature at 95 DEG C ~ 110 DEG C, when more than 110 DEG C, turn down chlorine feed amount, and reduce wax oil inlet amount simultaneously, regulate cooling water circulation amount simultaneously,
The hydrogen chloride gas produced in production process and do not complete reaction chlorine after the first cyclonic separator is separated, liquid enters the 7th chlorination tank, gas removes one-level graphite film-falling absorption tower absorbing hydrogen chloride gas, one-level graphite film-falling absorption tower gas out enters one-level and checks in still and absorb chlorine, one-level check on still gas out through second cyclonic separator be separated after enter secondary graphite film-falling absorption tower absorbing hydrogen chloride gas, secondary graphite film-falling absorption tower gas out by squirt pump enter secondary check on still absorb chlorine, secondary still gas out of checking on enters one-level packed absorber absorbing hydrogen chloride gas, one-level packed absorber gas out enters three grades of stills of checking on by squirt pump and absorbs chlorine, three grades of still gases out of checking on enter dilute acid bath absorbing hydrogen chloride gas by squirt pump, dilute acid bath gas out enters secondary packing tower absorbing hydrogen chloride gas, and secondary packing tower gas is out by emptying,
Open discharge pump, the clorafin in clorafin Receiving bin is squeezed into degassed still, after about 90 minutes, adds stablizer, obtained finished product clorafin, degassed still gas is out through degassed tempering tower, and enter three grades of packing towers and absorb, finished product clorafin squeezes into finished product storage tank through discharge pump.
2. the complete processing of a kind of clorafin according to claim 1, it is characterized in that: the chlorine produced in clorafin production process absorbs through one-level graphite film-falling absorption tower through hydrogen chloride tail gas, secondary graphite film-falling absorption tower absorbs, one-level packing tower absorbs, secondary packing tower absorbs, three grades of packing towers absorb and obtain byproduct hydrochloric acid, and by-product hydrochloric acid squeezes into hydrochloric acid tank through concentrated hydrochloric acid pump;
Or the hydrogen chloride gas produced in clorafin production process and unreacted chlorine remove one-level rinse bath after the second cyclonic separator is separated, after washing, liquid removes the first chlorination tank, tail gas removes secondary rinse bath, liquid after washing is beaten to one-level washing tower through washing pump, tail gas absorbs through one-level graphite film-falling absorption tower, secondary graphite film-falling absorption tower absorbs, one-level packing tower absorbs, secondary packing tower absorbs, three grades of packing towers absorb and obtain byproduct hydrochloric acid, and by-product hydrochloric acid part squeezes into hydrochloric acid tank through concentrated hydrochloric acid pump.
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106362555A (en) * | 2016-09-12 | 2017-02-01 | 江苏必康制药股份有限公司 | Process gas purification treatment method |
| CN107142124A (en) * | 2017-06-26 | 2017-09-08 | 柳州市隆达丰化工科技有限公司 | A kind of method that thermal chlorination is combined production chlorinated paraffin 52 with photocatalytic method |
| CN108159786A (en) * | 2018-02-12 | 2018-06-15 | 丹阳市助剂化工厂有限公司 | Chlorcosane tail gas pre-processing device |
| CN108201739A (en) * | 2018-02-12 | 2018-06-26 | 丹阳市助剂化工厂有限公司 | Chlorinated paraffin pretreatment equipment |
| CN108315054A (en) * | 2018-02-12 | 2018-07-24 | 丹阳市助剂化工厂有限公司 | Chlorinated paraffin continuous production processes |
| CN109022035A (en) * | 2018-08-15 | 2018-12-18 | 安徽绿色谷创客空间股份有限公司 | A kind of efficient process units and production method of chlorinated paraffin |
| WO2019114739A1 (en) * | 2017-12-12 | 2019-06-20 | 宁波镇洋化工发展有限公司 | Production process for chlorinated paraffin |
| CN110420611A (en) * | 2019-09-06 | 2019-11-08 | 丹阳市助剂化工厂有限公司 | A kind of chlorination tank producing chlorinated paraffin |
| CN110422825A (en) * | 2019-09-09 | 2019-11-08 | 丹阳市助剂化工厂有限公司 | A kind of HCl recovery Processes and apparatus in chlorinated paraffin production process |
| CN110523226A (en) * | 2019-09-09 | 2019-12-03 | 丹阳市助剂化工厂有限公司 | A kind of Chlorcosane tail gas treatment process and absorption equipment |
| CN111589292A (en) * | 2020-05-28 | 2020-08-28 | 山东振曦新材料科技有限公司 | Non-alkalization treatment process for tail gas of methyl chloride fatty acid |
| CN111589293A (en) * | 2020-05-28 | 2020-08-28 | 山东振曦新材料科技有限公司 | Chlorinated fatty acid methyl ester tail gas non-alkalization treatment system |
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| CN106362555B (en) * | 2016-09-12 | 2019-06-28 | 江苏九九久科技有限公司 | Process gas purifying treatment method |
| CN106362555A (en) * | 2016-09-12 | 2017-02-01 | 江苏必康制药股份有限公司 | Process gas purification treatment method |
| CN107142124A (en) * | 2017-06-26 | 2017-09-08 | 柳州市隆达丰化工科技有限公司 | A kind of method that thermal chlorination is combined production chlorinated paraffin 52 with photocatalytic method |
| WO2019114739A1 (en) * | 2017-12-12 | 2019-06-20 | 宁波镇洋化工发展有限公司 | Production process for chlorinated paraffin |
| CN108201739A (en) * | 2018-02-12 | 2018-06-26 | 丹阳市助剂化工厂有限公司 | Chlorinated paraffin pretreatment equipment |
| CN108315054A (en) * | 2018-02-12 | 2018-07-24 | 丹阳市助剂化工厂有限公司 | Chlorinated paraffin continuous production processes |
| CN108159786A (en) * | 2018-02-12 | 2018-06-15 | 丹阳市助剂化工厂有限公司 | Chlorcosane tail gas pre-processing device |
| CN108201739B (en) * | 2018-02-12 | 2024-01-02 | 丹阳市助剂化工厂有限公司 | Chlorinated paraffin raw material pretreatment equipment |
| CN108159786B (en) * | 2018-02-12 | 2024-01-30 | 丹阳市助剂化工厂有限公司 | Chlorinated paraffin tail gas pretreatment equipment |
| CN109022035A (en) * | 2018-08-15 | 2018-12-18 | 安徽绿色谷创客空间股份有限公司 | A kind of efficient process units and production method of chlorinated paraffin |
| CN110420611A (en) * | 2019-09-06 | 2019-11-08 | 丹阳市助剂化工厂有限公司 | A kind of chlorination tank producing chlorinated paraffin |
| CN110422825A (en) * | 2019-09-09 | 2019-11-08 | 丹阳市助剂化工厂有限公司 | A kind of HCl recovery Processes and apparatus in chlorinated paraffin production process |
| CN110523226A (en) * | 2019-09-09 | 2019-12-03 | 丹阳市助剂化工厂有限公司 | A kind of Chlorcosane tail gas treatment process and absorption equipment |
| CN111589292A (en) * | 2020-05-28 | 2020-08-28 | 山东振曦新材料科技有限公司 | Non-alkalization treatment process for tail gas of methyl chloride fatty acid |
| CN111589293A (en) * | 2020-05-28 | 2020-08-28 | 山东振曦新材料科技有限公司 | Chlorinated fatty acid methyl ester tail gas non-alkalization treatment system |
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Effective date of registration: 20210408 Address after: 332000 Jinshawan Industrial Park, Hukou County, Jiujiang City, Jiangxi Province Patentee after: JIANGXI SUXING MATERIAL Co.,Ltd. Address before: No. 60, Riverside South Road, Jiangshu Town, huangtang Town, Danyang City, Zhenjiang City, Jiangsu Province Patentee before: DANYANG CITY AUXILIARIES CHEMICAL PLANT Co.,Ltd. |