CN100524140C - Polymer polymerization reaction temperature control method and device thereof - Google Patents
Polymer polymerization reaction temperature control method and device thereof Download PDFInfo
- Publication number
- CN100524140C CN100524140C CNB200710145549XA CN200710145549A CN100524140C CN 100524140 C CN100524140 C CN 100524140C CN B200710145549X A CNB200710145549X A CN B200710145549XA CN 200710145549 A CN200710145549 A CN 200710145549A CN 100524140 C CN100524140 C CN 100524140C
- Authority
- CN
- China
- Prior art keywords
- temperature
- water
- outer circulation
- circulating water
- polymerization reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The utility model provides a method used for the temperature control of the high molecule polymerization reaction. The procedures thereof are listed as a steam heated circulating water reactor is adopted in the reactor jacket of the high molecule polymerization reaction; the cooling water is poured into the reactor jacket to lower the temperature of the circulating water so as to control the temperature in the reactor. Also, the utility model provides a temperature control device for the high molecule polymerization reaction which comprises an internal circulation and an outer circulation. The utility model is used to control the temperature of the high molecule polymerization reaction, so as to increase the selectivity and the yield of the reacting substance, so that the temperature drop efficiency in the course of reaction is greatly improved. Meanwhile, the heating steam and the consumption for cooling the temperature are saved.
Description
Technical field
The present invention relates to temperature controlled method of a kind of macromolecular polymerization reaction and device, temperature-controlled process and device when particularly relating to a kind of Organic fluoride high polymer monomer neither endothermic nor exothermic is violent in homopolymerization and the polymerization process in reactor.
Background technology
Macromolecular compound is the meeting neither endothermic nor exothermic in polymerization process, and temperature controlling all has great role to the selectivity and the yield of reactive material.The Organic fluoride high molecular polymer is in course of reaction, and the induced reaction that need heat up during beginning enters a large amount of again heat releases after the course of reaction, need remove heat fast, so that control temperature of reaction well, guarantees reaction velocity, stabilized product quality.Because general Organic fluoride high molecular polymerization process all is continuous feed, and follow the course of reaction of very exothermic, conventional seperating range control method is general to adopt the control that heats up, lowers the temperature of the method for in reacting kettle jacketing feeding steam or refrigerant, this method temperature control precision is poor, the energy consumption height, the cold and hot exchange of reacting kettle jacketing is too fast in addition, and temperature variation is too big, and is influential to the life-span of reactor.
Summary of the invention
The purpose of this invention is to provide a kind of polymer polymerization reaction temperature control method, solved macromolecular compound, particularly machine fluorine monomer very exothermic reaction needed in course of reaction is removed heat fast, improve the selectivity and the yield of reactive material, control temperature of reaction well, prolong the serviceable life of reactor simultaneously.
In addition, the present invention also provides a kind of macromolecular polymerization reaction temperature control equipment.
Macromolecular polymerization reaction is to add monomer continuously, and in course of reaction, add relevant auxiliary agent, and its reaction velocity is very responsive to temperature of reaction, and temperature is high more, react fast more, heat release Shaoxing opera is strong, and temperature is more just reacted speed more, heat release is few more, therefore controlling temperature of reaction well, is controls reaction speed, improves the selectivity of reactive material and a key of yield.
A kind of polymer polymerization reaction temperature control method of the present invention, it comprises the steps:
(1) sets temperature of reaction t;
(2) heating reactor: when decomposition induction time need heat, recirculated water variable valve in the standard-sized sheet, close the outer circulation water regulating valve, open steam control valve, steam is by steam heater and the abundant Hybrid Heating recirculated water of recirculated water, recirculated water is by reacting kettle jacketing time heating reactor, after reactor temperature reaches temperature of reaction t ± 1 ℃, stops heating;
(3) in course of reaction,, determine the temperature t that reacting kettle jacketing recirculated water is required by the linear model internalarithmetic according to reaction velocity
The water inlet temperature,, calculate the temperature difference between interior temperature of reactor and the chuck chilled water, just in time to take away the reaction liberated heat promptly according to the feed rate size.With t
The water inlet temperatureBe setting value, by interior circulating water temperature PID controller, control outer circulation water valve aperture, emit the hot water in the circulation in the part from outer circulation, produce negative pressure this moment in interior circulation, and interior recirculated water and circulating water chennel form pressure reduction, from circulating water chennel, replenish equivalent cold water automatically and enter reacting kettle jacketing (siphon principle), the cold water that enters in the reacting kettle jacketing mixes rapidly with recirculated water in the original reactor chuck, and circulating water temperature in reducing fast makes the temperature of chuck recirculated water satisfy t
The water inlet temperatureWhen the temperature of interior recirculated water is higher than t
The water inlet temperatureThe time, the aperture of regulating the outer circulation water valve by interior circulating water temperature PID controller.Temperature deviation is big more, and valve opening speed is fast more, and aperture is big more, and according to siphon principle, the chilled water that is entered reacting kettle jacketing by circulating water chennel is fast more, many more, and the reacting kettle jacketing water temperature descends fast more; Otherwise valve opening speed is slow more, and aperture is more little, and the chilled water that is entered reacting kettle jacketing by circulating water chennel is slow more, few more, and the reacting kettle jacketing water temperature descends slow more.By said process, temperature remains on t ± 1 ℃ in the control reactor.
For eliminating of the influence of some uncertain factors to temperature of reaction, accurately control temperature in the reactor, by the aperture of recirculated water variable valve in changing, adjust temperature of reaction among a small circle, make it to remain in t ± 1 ℃.In the reactor and the reacting kettle jacketing chilled water has the temperature difference, the aperture by recirculated water variable valve in changing changes recirculated water flow velocity in the reacting kettle jacketing, increase or reduce the recirculated water heat transfer rate, with this as a kind of auxiliary control method, to improve control accuracy.When reactor temperature is t ± 0.2 ℃, the recirculated water control valve opening is at 60-70% in the control, and when reactor temperature is higher than t+0.2 ℃, and temperature is when rising formula, recirculated water variable valve in the standard-sized sheet, the aperture that interior circulating water temperature PID controller is regulated the outer circulation water regulating valve automatically; When reactor temperature is lower than t-0.2 ℃, and during the temperature downtrending, in the control recirculated water control valve opening 20%, outer circulation water regulating valve complete shut-down.
When the temperature of circulating water chennel outer circulation water is higher than certain value, outer circulation tank PID controller Control Circulation tank refrigerant operation valve, refrigerant is lowered the temperature through the external recirculated water of coil pipe, with the temperature that keeps outer circulation water within the specific limits, according to different products, temperature required difference, the ordinary rubber base polymer, temperature is at 35～40 ℃, the resene polymkeric substance, and temperature is at 30～35 ℃.
Polymer polymerization reaction temperature control method of the present invention, wherein in circulation be that recirculated water is successively through reacting kettle jacketing, interior recirculated water variable valve, water circulating pump, steam heater, enter reacting kettle jacketing again; Outer circulation is that recirculated water flows out from internal recycle pipeline, enters the outer circulation pipeline, and flow through outer circulation water regulating valve and circulating water chennel enter internal recycle pipeline again.
A kind of macromolecular polymerization reaction temperature control equipment, circulation and outer circulation in comprising, it is characterized in that, described in circulation comprise internal recycle pipeline that two ends are connected with reacting kettle jacketing, be installed in interior recirculated water variable valve, water circulating pump, steam heater on the internal recycle pipeline successively; Described outer circulation comprises the outer circulation pipeline that two ends are connected with internal recycle pipeline, and is installed in outer circulation water regulating valve, circulating water chennel on the outer circulation pipeline successively.
Macromolecular polymerization reaction temperature control equipment of the present invention, the linear model arithmetical unit that also comprise the material feed rate measuring instrument that is installed on the reactor feed pipe, is connected with material feed rate measuring instrument successively with interior circulating water temperature PID controller, be installed in the circulating water temperature measuring instrument on the internal recycle pipeline, the steam control valve that is connected temperature measurement instrument in the reactor on the reactor, is connected with steam heater.
Macromolecular polymerization reaction temperature control equipment of the present invention is connected with circulating water chennel temperature measuring set and circulating water chennel refrigerant operation valve on the wherein said circulating water chennel, inside is equipped with coil pipe.
The bright described macromolecular polymerization reaction temperature control equipment of this law, wherein said circulating water chennel temperature measuring set are connected with circulating water chennel refrigerant operation valve respectively with outer circulation tank temperature PID controller and are connected.
Circulating water temperature PID controller is connected with the outer circulation water regulating valve with reacting kettle jacketing import circulating water temperature measuring instrument respectively in of the present invention.
Refrigerant of the present invention can be the medium that routine is used to cool off.
In course of reaction, heat release is more violent, but the transmission of temperature is slower, and in time taking away the reaction liberated heat, the variation of reacting kettle jacketing circulating water temperature need have a lead.Feed rate is a sensitive parameter that characterizes the poly-strong degree of reaction in polyreaction, therefore set up the mathematical model relation between feed rate and the chuck circulating water temperature, in time adjust the temperature of reacting kettle jacketing chilled water, can fine control polymeric reaction temperature.Under general condition, the relation between reaction feed flow and the interior circulating water temperature is followed the linear model relation:
t
The water inlet temperature=t-f
Charging* k+t
Drift correction
Wherein:
t
The water inlet temperature: reacting kettle jacketing circulating water intake temperature, ℃.
T: temperature in the given reactor, ℃.
f
Charging: reactor material feed rate, kg/h.
t
Drift correction: the temperature difference correction of different trade mark products, ℃.
K: flux temperature coefficient, be that the reactor feed rate is to the Temperature Influence coefficient, obtain by experiment, ℃/(kg/h), the centigrade degree that circulating water temperature need descend in 1 kilogram of/hour mix monomer feed rate of promptly every increase chuck is because the Organic fluoride polymerization theory is complicated, the factor that influence is conducted heat is more, these data are generally with the control feed rate, and the method experiment of manual adjustment circulating water temperature draws, and does more and can obtain more accurate K value several times.
With t
The water inlet temperatureAs reacting kettle jacketing import circulating water temperature set-point, by the linear model internalarithmetic, automatically control the aperture of outer circulation water regulating valve by interior circulating water temperature PID controller, change and enter the round-robin cooling water inflow, reach the purpose that reduces the reacting kettle jacketing circulating water temperature.
The PID controller is ratio, integration, three kinds of combinations of regulating rule of differential, is a kind of autocontrol method of classics, and its transport function is:
G
e(s)＝K
e(1+1/T
is)+T
ds
Described PID controller relates to complicated controls such as the chain control of aperture that PID regulates computing, inside and outside circulation valve position, the judgement of temperature of reaction lifting trend and calculates, and general the recommendation waited and realized with programmable intelligent PID controller or with PLC (Programmable logic controllor), DCS (Distributed computer system).
The beneficial effect of polymer polymerization reaction temperature control method of the present invention:
Solved macromolecular compound, particularly the very exothermic reaction needed is removed heat fast in the machine fluorine monomer polymerization process, improve the selectivity and the yield of reactive material, temperature in the stable control reactor, prolong the selectivity that has improved reactive material serviceable life and the yield of reactor simultaneously, yield can improve more than 20%, has saved steam and cold and has consumed more than 15%.
Description of drawings
Fig. 1 is a macromolecular polymerization reaction temperature control chart.
Among the figure: 1 water circulating pump; 2 reacting kettle jacketings; Temperature measurement instrument in 3 reactors; Recirculated water variable valve in 4; 5 outer circulation water regulating valves; 6 circulating water chennel temperature measuring sets; 7 circulating water chennel refrigerant operation valves; 8 material feed rate measuring instruments; 9 reacting kettle jacketing import circulating water temperature measuring instruments; 10 steam heaters; Circulating water temperature PID controller in 11; 12 steam control valves; 13 internal recycle pipelines; 14 circulating water chennels; 15 linear model arithmetical unit; 16 outer circulation pipelines; 17 reactors; 18 coil pipes; 19 outer circulation tank temperature PID controllers.
Embodiment
The present invention is described further below in conjunction with accompanying drawing, but be not used for limiting the scope of the invention.
The application of embodiment 1 linear model
If interior warm t=80 ℃ of given reactor is current feed rate f
Charging=80kg/h, flux temperature coefficient k=0.4 ℃/(kg/h), current production synthetic rubber temperature deviation correction t
Drift correction=3 ℃, the temperature of chilled water in the then current reacting kettle jacketing 2:
T is intake warm=80-80*0.4+3=51 ℃
Embodiment 2 Organic fluoride macromolecular polymerization reaction temperature control equipments
Be a kind of Organic fluoride macromolecular polymerization reaction temperature control equipment that is used for as shown in Figure 1, comprise outer circulation and interior circulation, interior circulation comprises the internal recycle pipeline 13 that two ends are connected with reacting kettle jacketing 2, and is installed in interior recirculated water variable valve 4, water circulating pump 1, steam heater 10 on the internal recycle pipeline 13 successively.Described outer circulation comprises the outer circulation pipeline 16 that two ends are connected with internal recycle pipeline 13, and is installed in outer circulation water regulating valve 5, circulating water chennel 14 on the outer circulation pipeline 16 successively.Be connected with steam control valve 12 on the steam heater 10.Circulating water chennel 14 is connected with circulating water chennel temperature measuring set 6 and circulating water chennel refrigerant operation valve 7, and circulating water chennel 14 inside are equipped with coil pipe 18.In this control device, material feed rate measuring instrument 8 is installed on the feed pipe that is connected with reactor 17, linear model arithmetical unit 15 is connected with interior circulating water temperature PID controller 11 with material feed rate measuring instrument 8 respectively, interior circulating water temperature PID controller 11 respectively with outer circulation water regulating valve 5, reactor in temperature measurement instrument 3, interior recirculated water variable valve 4 be connected with reactor import circulating water temperature measuring instrument 9, outer circulation tank temperature PID controller 19 is connected with circulating water chennel temperature measuring set 6 with refrigerant operation valve 7 respectively.Reactor import circulating water temperature measuring instrument 9 is installed in internal recycle pipeline 13 near the reacting kettle jacketing entrance point, and temperature measurement instrument 3 is installed on the reactor 17 in the reactor.
The control of embodiment 3 Organic fluoride macromolecular polymerization reaction temperature
The vinylidene fluoride monomers induced reaction that must heat up before homopolymerization and the polymerization process in reactor, the reaction of present embodiment is temperature required to be set at 80 ℃.Reaction induced intensification begins, recirculated water variable valve 4 in the standard-sized sheet, close outer circulation water regulating valve 5, open steam control valve 12, the control steam flow, steam mixes with recirculated water by steam heater 10, heat cycles water, the recirculated water of heating gives reactor 17 heating by reaction chuck 2, the water that comes out from reacting kettle jacketing 2 enters steam heater 10 once more and heats through internal recycle pipeline 13, interior recirculated water variable valve 4, water circulating pump 1 successively again, so circulation, this cyclic process belongs to interior circulation.The control of steam flow with the designed capacity of steam heater 10 and do not produce the vibration be principle, The faster the better for programming rate.When temperature of reaction kettle reaches 80 ± 1 ℃, steam off operation valve 12 stops heating, interior recirculated water variable valve 4 apertures 70%, and the intensification induction period is finished.
Temperature controlling stages, open the material inlet valve, enter the macromolecular polymerization reaction stage, measure the mass flow that enters reactor by material feed rate measuring instrument 8, and add up, the signal of measuring mass flow outputs to linear model arithmetical unit 15, and circulating water temperature PID controller 11 was as the set-point of controller in the operation result of linear operator 15 outputed to, and this set-point is as current required chuck cooling water temperature t
The water inlet temperatureThe circulating water temperature of measuring when reacting kettle jacketing import circulating water temperature measuring instrument 9 is than current t
The water inlet temperatureHigh, PID controller 11 can receive signal, automatically control the aperture of outer circulation water regulating valve 5, emit the recirculated water of heat, the recirculated water of heat flow to circulating water chennel 14 through outer circulation pipeline 16, and according to siphon principle, the cold water that has equivalent in the circulating water chennel 14 enters internal recycle pipeline 13, mix rapidly with recirculated water in the original reactor chuck 2, circulating water temperature is to t in reducing fast
The water inlet temperature, when so the interior recirculated water of temperature is through reacting kettle jacketing 2, just in time take away the reaction liberated heat, reach the purpose of temperature in the control reaction.Interior circulating water temperature is different and different according to the severe degree of reaction with the temperature difference of the interior temperature of reactor, the t that its value calculates with linear model arithmetical unit 15
The water inlet temperatureAnd change.
For eliminating of the influence of some uncertain factors to temperature of reaction, accurately control temperature in the reactor, control reactor temperature at 80 ± 1 ℃ by the aperture scope of recirculated water variable valve 4 in changing.With the 3 assaying reaction temperature in the kettle of temperature measurement instrument in the reactor, when reactor temperature is 80 ± 0.2 ℃, recirculated water variable valve 4 apertures are 60-70% in regulating, when reactor temperature is higher than 80+0.2 ℃, and temperature rises when becoming formula, and recirculated water variable valve 4 in the standard-sized sheet strengthens the flow velocity by the recirculated water of reaction chuck 2, take away the reaction liberated heat fast, by interior circulating water temperature PID controller 11 automatic apertures of regulating outer circulation water regulating valve 5; When reactor temperature is lower than 80-0.2 ℃, and temperature descends when becoming formula, and interior recirculated water variable valve 4 apertures are 20%, outer circulation water regulating valve 5 complete shut-downs, slow down flow velocity, slow down and take away the speed of reaction liberated heat, keep temperature of reaction at 80 ± 1 ℃ by the recirculated water of reaction chuck 2.
In the course of reaction, the temperature that circulating water chennel temperature measuring set 6 is measured circulating water chennel recirculated water is higher than 35～40 ℃, the output measuring-signal is to outer circulation tank temperature PID controller 19, the aperture of the automatic Control Circulation tank of outer circulation tank temperature PID controller refrigerant operation valve 7, refrigerant is lowered the temperature, to keep circulating water temperature at 35～40 ℃ through 18 pairs of recirculated waters of coil pipe.
Reaction is closed the material inlet valve after finishing, and stops charging, closes circulating water chennel refrigerant operation valve 7, and discharging is prepared in circulation in recirculated water continues.
The used refrigerant of present embodiment is 5 ℃ a water.
The Organic fluoride polyreaction is the process of a homopolymerization and copolymerization, the key of product quality is the pressure and temperature of control reaction, general pressure ratio is more easy to control, temperature control is difficult, accurately control temperature by the method, the product performance index of different batches is more approaching, good reproducibility, the yield of reaction product improves more than 20%, saves cold and steam more than 15%.
Claims (15)
1, a kind of polymer polymerization reaction temperature control method, its step comprises:
A. set temperature of reaction t;
B. decomposition induction time heats reactor (17): when need heat, recirculated water variable valve (4) in the standard-sized sheet, close outer circulation water regulating valve (5), open steam control valve (12), steam is by steam heater (10) and the abundant Hybrid Heating recirculated water of recirculated water, recirculated water is by reacting kettle jacketing (2) time heating reactor (17), after reactor temperature reaches 1 ℃ on temperature of reaction bodyguard, stops heating;
C. control reactor (17) temperature: in course of reaction, determine that by linear model arithmetical unit (15) the required temperature of reacting kettle jacketing (2) recirculated water is as setting value t
The water inlet temperature, by interior circulating water temperature PID controller (11), control outer circulation water regulating valve (5) aperture makes the temperature of the interior recirculated water of reacting kettle jacketing (2) satisfy t
The water inlet temperature, the temperature in control reactor (17) is in t ± 1 ℃.
2, polymer polymerization reaction temperature control method as claimed in claim 1 is characterized in that, step C also comprises: when reactor (17) temperature was t ± 0.2 ℃, the aperture of recirculated water variable valve (4) was 60-70% in the control; When temperature is higher than t+0.2 ℃ in the reactor (17), during the temperature ascendant trend, recirculated water variable valve (4) standard-sized sheet in the control, interior circulating water temperature PID controller (11) is controlled the aperture of outer circulation water regulating valve (5) automatically; When temperature was lower than t-0.2 ℃ in the reactor (17), during the temperature downtrending, the aperture of recirculated water variable valve (4) was 20% in the control, outer circulation water regulating valve (5) complete shut-down.
3, polymer polymerization reaction temperature control method as claimed in claim 1 or 2, it is characterized in that, step C also comprises: when the temperature of circulating water chennel (14) outer circulation water is higher than certain certain value, outer circulation tank temperature PID controller (19) control is automatically opened circulating water chennel refrigerant operation valve (7), refrigerant reduces the temperature of recirculated water by coil pipe (18) cooling circulating water.
4, polymer polymerization reaction temperature control method as claimed in claim 1 or 2, it is characterized in that, circulation is that recirculated water passes through reacting kettle jacketing (2), interior recirculated water variable valve (4), water circulating pump (1), steam heater (10) successively in described, enters reacting kettle jacketing (2) again.
5, polymer polymerization reaction temperature control method as claimed in claim 3, it is characterized in that, circulation is that recirculated water passes through reacting kettle jacketing (2), interior recirculated water variable valve (4), water circulating pump (1), steam heater (10) successively in described, enters reacting kettle jacketing (2) again.
6, as claim 1,2 or 5 arbitrary described polymer polymerization reaction temperature control methods, it is characterized in that, described outer circulation is that recirculated water flows out from internal recycle pipeline (13), enter outer circulation pipeline (16), flow through outer circulation water regulating valve (5) and circulating water chennel (14) enter internal recycle pipeline (13) again.
7, polymer polymerization reaction temperature control method as claimed in claim 3, it is characterized in that, described outer circulation is that recirculated water flows out from internal recycle pipeline (13), enter outer circulation pipeline (16), flow through outer circulation water regulating valve (5) and circulating water chennel (14) enter internal recycle pipeline (13) again.
8, polymer polymerization reaction temperature control method as claimed in claim 4, it is characterized in that, described outer circulation is that recirculated water flows out from internal recycle pipeline (13), enter outer circulation pipeline (16), flow through outer circulation water regulating valve (5) and circulating water chennel (14) enter internal recycle pipeline (13) again.
9, a kind of macromolecular polymerization reaction temperature control equipment, circulation and outer circulation in comprising, it is characterized in that, described in circulation comprise internal recycle pipeline (13) that two ends are connected with reacting kettle jacketing (2), be installed in interior recirculated water variable valve (4), water circulating pump (1), steam heater (10) on the internal recycle pipeline (13) successively; Described outer circulation comprises the outer circulation pipeline (16) that two ends are connected with internal recycle pipeline (13), and is installed in outer circulation water regulating valve (5), circulating water chennel (14) on the outer circulation pipeline (16) successively.
10, macromolecular polymerization reaction temperature control equipment as claimed in claim 9, it is characterized in that, the linear model arithmetical unit (15) that described control device also comprises the material feed rate measuring instrument (8) that is installed on reactor (17) feed pipe, be connected successively with material feed rate measuring instrument (8) with interior circulating water temperature PID controller (11), be installed in the circulating water temperature measuring instrument (9) on the internal recycle pipeline (13), the steam control valve (12) that is connected temperature measurement instrument (3) in the reactor on the reactor (17), is connected with steam heater (10).
As claim 9 or 10 described macromolecular polymerization reaction temperature control equipments, it is characterized in that 11, be connected with circulating water chennel temperature measuring set (6) and circulating water chennel refrigerant operation valve (7) on the described circulating water chennel (14), inside is equipped with coil pipe (18).
As claim 9 or 10 described macromolecular polymerization reaction temperature control equipments, it is characterized in that 12, described circulating water chennel temperature measuring set (6) is connected with outer circulation tank temperature PID controller (19) respectively with circulating water chennel refrigerant operation valve (7).
13, macromolecular polymerization reaction temperature control equipment as claimed in claim 11 is characterized in that, described circulating water chennel temperature measuring set (6) is connected with outer circulation tank temperature PID controller (19) respectively with circulating water chennel refrigerant operation valve (7).
14, as claim 9,10 or 13 any described macromolecular polymerization reaction temperature control equipments, it is characterized in that described interior circulating water temperature PID controller (11) is connected with outer circulation water regulating valve (5) with reacting kettle jacketing import circulating water temperature measuring instrument (9) respectively.
15, macromolecular polymerization reaction temperature control equipment as claimed in claim 12 is characterized in that, described interior circulating water temperature PID controller (11) is connected with outer circulation water regulating valve (5) with reacting kettle jacketing import circulating water temperature measuring instrument (9) respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200710145549XA CN100524140C (en) | 2007-08-28 | 2007-08-28 | Polymer polymerization reaction temperature control method and device thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200710145549XA CN100524140C (en) | 2007-08-28 | 2007-08-28 | Polymer polymerization reaction temperature control method and device thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101109966A CN101109966A (en) | 2008-01-23 |
| CN100524140C true CN100524140C (en) | 2009-08-05 |
Family
ID=39042063
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200710145549XA Active CN100524140C (en) | 2007-08-28 | 2007-08-28 | Polymer polymerization reaction temperature control method and device thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100524140C (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101337172B (en) * | 2008-08-29 | 2010-05-12 | 河南宏业化工有限公司 | Constant temperature and constant pressure reactor |
| CN103387623B (en) * | 2012-05-07 | 2015-08-19 | 中国石油化工股份有限公司 | A kind of polymerizing reactor and application thereof |
| CN103127896B (en) * | 2013-02-28 | 2015-06-17 | 贵州开磷（集团）有限责任公司 | PVC polymerization kettle stirring dragging method |
| CN103513572B (en) * | 2013-10-25 | 2016-01-20 | 中国船舶重工集团公司第七�三研究所 | The PID change target algorithm that power function is nested with logarithm |
| CN104950960B (en) * | 2015-06-17 | 2017-12-29 | 长春工业大学 | A kind of control method of supercritical extract process temperature and pressure |
| CN106886231A (en) * | 2015-12-15 | 2017-06-23 | 上海奥星制药技术装备有限公司 | For the thermostatic control system and its operating method of pharmacy Agitation Tank |
| CN107188995B (en) * | 2016-03-14 | 2019-01-04 | 中昊晨光化工研究院有限公司 | A kind of device and its application for adjusting polytetrafluoroethylene (PTFE) reaction temperature |
| CN105749772A (en) * | 2016-03-31 | 2016-07-13 | 句容东发生活用品有限公司 | Constant-temperature proportioned wet tissue stock solution stirring barrel |
| CN107983287A (en) * | 2017-12-16 | 2018-05-04 | 河南莱帕克化工设备制造有限公司 | resin polymerization pilot experiment system |
| CN111468053B (en) * | 2020-04-17 | 2022-04-22 | 大庆市新万通科技开发有限公司 | Profile control agent/water plugging agent polymerization curing device and working method thereof |
| CN114534651B (en) * | 2022-01-13 | 2024-03-12 | 宁夏天霖新材料科技有限公司 | Reactor temperature control method |
| CN115090233A (en) * | 2022-06-29 | 2022-09-23 | 珠海市泽涛粘合制品有限公司 | Reaction kettle heat supply device and control method thereof |
| CN115121202A (en) * | 2022-09-02 | 2022-09-30 | 江苏飞宇医药科技股份有限公司 | Reaction kettle temperature control method and production process of cyclopropyl ethyl amide |
-
2007
- 2007-08-28 CN CNB200710145549XA patent/CN100524140C/en active Active
Non-Patent Citations (2)
| Title |
|---|
| 夹套反应釜温度控制浅析. 吴康明，李嘉斌.化学工程师，第4期. 2001 |
| 夹套反应釜温度控制浅析. 吴康明，李嘉斌.化学工程师，第4期. 2001 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101109966A (en) | 2008-01-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100524140C (en) | Polymer polymerization reaction temperature control method and device thereof | |
| CN1092999C (en) | Heat exchange area regulating type reaction heat control mechanism for chemical reaction apparatuses | |
| CN102156496B (en) | Blending control method for temperature of reactive kettle | |
| CN101587357A (en) | Temperature control method and temperature control system thereof | |
| CN107885259A (en) | A kind of chlorination reaction temperature control method, system and equipment | |
| CN109049591A (en) | A kind of injection mold temperature controller and its control method | |
| CN107649079A (en) | A kind of carbon fiber produces polymerization reactor control device and method | |
| CN205563299U (en) | A temperature control cascade control system for alkoxylation unit | |
| CN105487515B (en) | A kind of integrated optimization method for continuously stirring the technological design of autoclave course of reaction and control | |
| CN1864848A (en) | Method and apparatus for controlling temperature of reactor | |
| CN204380669U (en) | A kind of reactor controlling multiple organic monomer polymeric reaction temperature | |
| CN107151281B (en) | Substance law PVC polymeric reaction temperature autocontrol method | |
| CN102681565A (en) | CSTR (continuous stirred-tank reactor) temperature control system and method based on coil heat exchanger and jacketed heat exchanger | |
| CN207734999U (en) | Reaction kettle exothermic reaction temperature regulating device | |
| CN107765730A (en) | A kind of fluidized-bed temperature control method and control device | |
| CN213701728U (en) | Be used for as cast mould quick cooling system of aluminium base piston | |
| CN201011503Y (en) | Adjusting and controlling device for heat change between heat measuring system and outer cylinder | |
| CN210741236U (en) | Temperature control device | |
| CN206064385U (en) | A kind of temperature automatically controlled reactor for preparing aliphatic water reducing agent | |
| CN206184416U (en) | A reaction control system for producing chlorinated paraffin | |
| CN205700571U (en) | A kind of high-efficiency polymerization reactor | |
| CN220651143U (en) | PVC polymerization temperature control system | |
| CN111185130A (en) | Industrial online control prepolymerization kettle and method for cyanate ester resin | |
| CN116078308A (en) | Intelligent control method for reflux condenser at top of chloroethylene suspension polymerization kettle | |
| CN215389276U (en) | Automatic temperature control device of carbon fiber polymerization reaction kettle |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: ZHONGHAO CHENGUANG RESEARCH INSTITUTE OF CHEMICAL Free format text: FORMER NAME: ZHONGHAO CHENGUANG CHEMICAL RESEARCH INST. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 643201, Chenguang Road, Fu town, Fushun County, Zigong, Sichuan, 135 Patentee after: Zhonghao Chenguang Chemical Institute Co., Ltd. Address before: 643201, Chenguang Road, Fu town, Fushun County, Zigong, Sichuan, 135 Patentee before: Zhonghao Chenguang Chemical Research Inst. |