CN100371426C - Continuous chloroparaffin production apparatus - Google Patents
Continuous chloroparaffin production apparatus Download PDFInfo
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- CN100371426C CN100371426C CNB2006100254111A CN200610025411A CN100371426C CN 100371426 C CN100371426 C CN 100371426C CN B2006100254111 A CNB2006100254111 A CN B2006100254111A CN 200610025411 A CN200610025411 A CN 200610025411A CN 100371426 C CN100371426 C CN 100371426C
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Abstract
The present invention discloses a continuous chloroparaffin production device which comprises a plurality of reactors, external coolers and circulating pumps, wherein all the components are connected in series by pipelines. The present invention is characterized in that the bottom of each reactor is provided with a circulating mass and chlorine gas entering device (103), reaction mass is forcibly premixed with chlorine gas in the circulating mass and chlorine gas entering device from the bottom of each reactor and flows from bottom to top by a forced circulating pump, and simultaneously, the circulating flow of the reaction mass and mass in a reaction vessel is accelerated from bottom to top; thus, the present invention prevents chlorination reaction from causing frit phenomena because of too much local heat release so as to avoid generating industrial accidents.
Description
Technical field
The present invention relates to a kind of chloroparaffin production apparatus, relate to continuous chloroparaffin production apparatus specifically.
Background technology
Clorafin is a kind of important industrial raw material, as being used for the extender plasticizer of polyvinyl chloride, and can also be as antithrombotics, tackifier, paint stablizer etc.
Because the importance of clorafin in industrial application, so the optimization of its production equipment and production method have caused that people pay close attention to widely.
Chinese patent CN02148592.5 discloses a kind of continuous chloroparaffin production apparatus, this device adopts a plurality of placed in-line reactors, be used for serialization and produce clorafin, but, this installs existing defective is very significant, the inlet of the raw material chlorine of this device is arranged on the top of each reactor, therefore, the chlorine skewness that feeds, local chlorination phenomenon is serious, and reactor bottom " imitation frosted glass " can't effectively solve, chlorine conversion is not high, the chlorine content of carrying secretly in the hydrogen chloride tail gas that reaction produces is also higher simultaneously, thereby has influenced a pair quality product of producing hydrochloric acid, and therefore industrial accident often takes place.
Summary of the invention
The technical issues that need to address of the present invention are to disclose a kind of continuous chloroparaffin production apparatus, to overcome the above-mentioned defective that prior art exists.
The inventive system comprises a plurality of reactor, outer water cooler and recycle pumps that are connected in series by pipeline;
Said reactor comprises ultraviolet lamp, recycle stock outlet, recycle stock and chlorine access to plant, paraffin oil inlet, reacting product outlet and tail gas outlet;
Said ultraviolet lamp is installed in the said reactor, said paraffin oil inlet is arranged on the top of reactor, the recycle stock outlet is arranged on the top of reactor, and be connected with the inlet of outer water cooler by pipeline, reacting product outlet is arranged on the upper lateral part of reactor, recycle stock and chlorine access to plant are arranged on the bottom of reactor, the outlet of outer water cooler is connected with said inlet of circulating pump, outlet of circulating pump is connected with the chlorine access to plant with recycle stock, the material outlet of the reactor of upper level is connected with the paraffin oil inlet of the reactor of next stage, and the tail gas outlet is arranged on reactor head.
Device of the present invention can be used for serialization and produce clorafin, and the preparation method comprises the steps:
The paraffin oil inlet enters reactor by paraffin oil inlet successive, chlorine enters reactor by recycle stock and chlorine access to plant from reactor bottom, under the catalysis of the UV-light that ultraviolet lamp sends, carry out chlorination, the reaction product of upper level enters the reactor of next stage, continue reaction, it is refining that the reaction product of last reactor enters follow-up workshop section, and the hydrogenchloride that reaction produces enters exhaust treatment system from the tail gas outlet of reactor head;
From the reaction product that overflow on reactor top, enter the inlet of outer water cooler, be cooled to 85～90 ℃, enter recycle stock and chlorine access to plant by recycle pump then, and enter reactor after the chlorine pre-mixing.
The processing condition of reaction are as follows: temperature of reaction is 90～105 ℃, and reaction pressure is 0.02～0.04Mpa, and the volume ratio of paraffin oil and chlorine is:
Oil: chlorine=1～1.5: 560～640;
The volume ratio of recycle stock and chlorine is:
Recycle stock: chlorine=1: 17.5～20
The residence time of material in reactor is 24～38 hours,
The power of ultraviolet lamp is 3～7 kilowatts;
Material chlorinity between each reactor on average keeps 5～20% gradient, how much can adjusting of its chlorinity by the logical chlorine dose of each reactor, or regulated by the oil inlet quantity of first reactor, thereby the discharging that guarantees last reactor reaches the set quota, and its proportion of 70 ℃ is 26～28 mother-in-law U.S. degree;
Said paraffin oil is a kind of positive structure straight-chain paraffin, and its molecular weight is 170～220, is a kind of product that derives from oil;
Adopt device of the present invention to prepare clorafin, reaction mass passes through forced circulation pump, force from reactor bottom bottom-up mobile in reactor after the pre-mixing in recycle stock and chlorine access to plant again with chlorine, the bottom-up quickening of material circulates in reactor simultaneously, prevent the excessive grog phenomenon that causes of chlorination reaction localized heat release, thereby avoid taking place industrial accident.
Description of drawings
Fig. 1 is the apparatus structure synoptic diagram.
Fig. 2 is recycle stock and chlorine access to plant structural representation.
Embodiment
Referring to Fig. 1, the inventive system comprises a plurality of reactor 1, outer water cooler 2 and recycle pumps 3 that are connected in series by pipeline;
Said reactor 1 comprises ultraviolet lamp, recycle stock outlet 102, recycle stock and chlorine access to plant 103, paraffin oil inlet 104, reacting product outlet 105 and tail gas outlet 106;
Said ultraviolet lamp is installed in the reactor 1, paraffin oil inlet 104 is arranged on the top of reactor 1, recycle stock outlet 102 is arranged on the top of reactor 1, reacting product outlet 105 is arranged on the upper lateral part of reactor 1, recycle stock and chlorine access to plant 103 are arranged on the bottom of reactor 1, the inlet of said outer water cooler 2 is connected with recycle stock outlet 102, the outlet of outer water cooler 2 is connected with the import of recycle pump 3, the outlet of recycle pump 3 is connected with chlorine access to plant 103 with recycle stock, the material outlet of the reactor of upper level is connected with the paraffin oil inlet of the reactor of next stage, and tail gas outlet 106 is arranged on reactor 1 top.
Preferred 2～10 of reactor, most preferably 5;
Referring to Fig. 2, said recycle stock and chlorine access to plant 103 comprise T shape mixing tube 113 and nozzle 114, nozzle 114 is arranged on an end of T shape mixing tube 113, the intracavity inter-connection of jet exit and T shape mixing tube 113, the other end of T shape mixing tube 113 is connected with reactor, and an end again of T shape mixing tube 113 is connected with recycle pump 3;
According to the preferred scheme of the present invention, said nozzle 114 is a laddertron, and height H is 250～350mm, and upper base L1 length is 40～60mm, and the length L of going to the bottom 2 is 80～120mm.
Embodiment 1
Adopt device, the reactor of Fig. 2 and the nozzle of Fig. 3 of Fig. 1, reactor is 5, the preparation clorafin.
The laddertron height H is 300mm, and upper base L1 length is 50mm, and the length L of going to the bottom 2 is 100mm.
Paraffin oil enters reactor by paraffin oil inlet successive, chlorine enters reactor by recycle stock and chlorine access to plant from reactor bottom, under the catalysis of the UV-light that ultraviolet lamp sends, carry out chlorination, the reaction product of upper level enters the reactor of next stage, continue reaction, it is refining that the reaction product of last reactor enters follow-up workshop section, and the hydrogenchloride that reaction produces enters exhaust treatment system from the tail gas outlet from reactor head;
From the reaction product that overflow on reactor top, enter the inlet of outer water cooler, be cooled to 85 ℃, enter recycle stock and chlorine access to plant by recycle pump then, and enter reactor after the chlorine pre-mixing.
The processing condition of reaction are as follows: temperature of reaction is 90 ℃, and reaction pressure is 0.02Mpa, and the flow of paraffin oil is 1.25m
3/ h, chlorine are that flow is 700m
3/ h, the volume ratio of recycle stock and chlorine is:
Recycle stock: chlorine=1: 17.5;
The residence time of material in reactor is 38 hours,
The power of ultraviolet lamp is 5 kilowatts;
The average gradient of the material chlorinity between each reactor is 15%, can determine according to the proportion of the material of each reactor: second reactor: 3 (70 ℃ of mother-in-law U.S. degree), the 3rd reactor: 13 (70 ℃ of mother-in-law U.S. degree), the 4th reactor: 23 (70 ℃ of mother-in-law U.S. degree), the 5th reactor 27 (70 ℃ of mother-in-law U.S. degree);
The paraffin oil molecular weight is 220.Transformation efficiency is 98.5%.
Embodiment 2
Adopt the device identical with embodiment 1, prepare clorafin, reactor is selected 3 for use.
The processing condition of reaction are as follows: temperature of reaction is 105 ℃, and reaction pressure is 0.04Mpa, and the flow of paraffin oil is 1.875m
3/ h, chlorine are that flow is 800m
3/ h, the volume ratio of recycle stock and chlorine is:
Recycle stock: chlorine=1: 20;
The residence time of material in reactor is 25 hours,
The power of ultraviolet lamp is 5 kilowatts;
Material chlorinity average gradient between each reactor is 20%, thereby the discharging that guarantees last reactor reaches the set quota, and the proportion of the material of each reactor is as follows:
Second reactor: 18 (70 ℃ of mother-in-law U.S. degree), the 3rd reactor: 27 (70 ℃ of mother-in-law U.S. degree); The paraffin oil molecular weight is 200.Transformation efficiency is 99%.
Claims (5)
1. a continuous chloroparaffin production apparatus comprises a plurality of reactors that are connected in series by pipeline (1), outer water cooler (2) and recycle pump (3); It is characterized in that:
Said reactor (1) comprises ultraviolet lamp, recycle stock outlet (102), recycle stock and chlorine access to plant (103), paraffin oil inlet (104), reacting product outlet (105) and tail gas outlet (106);
Said ultraviolet lamp is installed in the reactor (1), paraffin oil inlet (104) is arranged on the top of reactor (1), recycle stock outlet (102) is arranged on the top of reactor (1), reaction product goes out the upper lateral part that (105) are arranged on reactor (1), recycle stock and chlorine access to plant (103) are arranged on the bottom of reactor (1), the inlet of said outer water cooler (2) is connected with recycle stock outlet (102), the outlet of outer water cooler (2) is connected with the import of recycle pump (3), the outlet of recycle pump (3) is connected with chlorine access to plant (103) with recycle stock, the material outlet of the reactor of upper level is connected with the paraffin oil inlet of the reactor of next stage, and tail gas outlet (106) is arranged on reactor (1) top.
2. device according to claim 1 is characterized in that, reactor is 3～7.
3. device according to claim 2 is characterized in that, reactor is 5.
4. according to claim 1,2 or 3 described devices, it is characterized in that, said recycle stock and chlorine access to plant (103) comprise T shape mixing tube (113) and nozzle (114), nozzle (114) is arranged on an end of T shape mixing tube (113), the intracavity inter-connection of jet exit and T shape mixing tube (113), the other end of T shape mixing tube (113) is connected with reactor, and an end again of T shape mixing tube (113) is connected with recycle pump (3).
5. device according to claim 4 is characterized in that, said nozzle (114) is a laddertron, and height H is 250～350mm, and upper base L1 length is 40～60mm, and the length L of going to the bottom 2 is 80～120mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100254111A CN100371426C (en) | 2006-04-03 | 2006-04-03 | Continuous chloroparaffin production apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100254111A CN100371426C (en) | 2006-04-03 | 2006-04-03 | Continuous chloroparaffin production apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1827748A CN1827748A (en) | 2006-09-06 |
| CN100371426C true CN100371426C (en) | 2008-02-27 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100254111A Expired - Fee Related CN100371426C (en) | 2006-04-03 | 2006-04-03 | Continuous chloroparaffin production apparatus |
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| CN (1) | CN100371426C (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102671593A (en) * | 2012-05-25 | 2012-09-19 | 福建致尚生物质材料发展有限公司 | Continuous chlorination fatty acid methyl ester producing device |
| CN103060000A (en) * | 2013-01-05 | 2013-04-24 | 沁阳市海世鸿工贸有限责任公司 | Chlorinated paraffin production equipment and method |
| CN103965963A (en) * | 2014-03-24 | 2014-08-06 | 辛集市三金化工有限公司 | Chlorinated paraffin production equipment and automatic control system |
| CN106010649A (en) * | 2016-08-03 | 2016-10-12 | 安徽中缘新材料科技有限公司 | Chlorinated paraffin continuous production process efficiently utilizing chlorine gas |
| CN106281457A (en) * | 2016-08-03 | 2017-01-04 | 安徽中缘新材料科技有限公司 | Chlorinated paraffin production line |
Citations (3)
| 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 |
| CN1191884A (en) * | 1998-03-17 | 1998-09-02 | 宁波市镇海区众利化工厂 | Continuous chlorinated-paraffin producing process |
| CN1424381A (en) * | 2002-12-18 | 2003-06-18 | 宁波市镇海众利化工有限公司 | Devices for continuously producing chlorinated paraffin |
-
2006
- 2006-04-03 CN CNB2006100254111A patent/CN100371426C/en not_active Expired - Fee Related
Patent Citations (3)
| 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 |
| CN1191884A (en) * | 1998-03-17 | 1998-09-02 | 宁波市镇海区众利化工厂 | Continuous chlorinated-paraffin producing process |
| CN1424381A (en) * | 2002-12-18 | 2003-06-18 | 宁波市镇海众利化工有限公司 | Devices for continuously producing chlorinated paraffin |
Also Published As
| Publication number | Publication date |
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| CN1827748A (en) | 2006-09-06 |
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Granted publication date: 20080227 Termination date: 20180403 |