CN103467636B - A kind of production technique of brominated butyl rubber - Google Patents
A kind of production technique of brominated butyl rubber Download PDFInfo
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Abstract
The invention discloses the production technique of a kind of brominated butyl rubber belonging to technical field of chemistry and chemical engineering.First this technique utilize nitrogen, as carrier gas, bromine is gasificated as bromo-nitrogen mixture in bromine vaporizer, the short mix that recycling bromination mixing tank realizes the alkane solution of bromo-nitrogen mixture and isoprene-isobutylene rubber causes bromination reaction, formed bromination reaction liquid in follow-up bromination reaction pipeline after certain hour, further with neutralizer in and mixing tank in short mix start neutralization reaction, formed multiphase mixture follow-up neutralization reaction pipeline and in and still in complete reaction process, tail gas through purification after can be recycled.The feature of this technique adopts gas phase bromine to replace traditional bromoalkane solution feed, reactant mixing velocity is fast, reaction times is short and can be controlled exactly, product brominated degree can regulate and control in 0% ~ 1.8% scope, secondary position bromine content is higher than 97%, and the index such as degree of unsaturation, mooney viscosity of products obtained therefrom is excellent.
Description
Technical field
The invention belongs to technical field of chemistry and chemical engineering, be specifically related to a kind of production technique of brominated butyl rubber.
Technical background
Brominated butyl rubber is a kind of important rubber product, in order to overcome the slow problem of conventional butyl rubbers vulcanization rate, nineteen fifty-three human research has gone out the bromination process of isoprene-isobutylene rubber, the more traditional isoprene-isobutylene rubber of brominated butyl rubber heat-resisting, acid and alkali-resistance, sulfurate activity, with other blend rubbers and regenerability in there is obvious advantage, be the main raw material of high grade air tube, the engineering automobiles inner tube of a tyre, tubeless forum air retaining wall.Along with the development of Domestic Automotive Industry, the demand at present for brominated butyl rubber constantly promotes, but China there is no ripe preparation method at present.
The bromination reaction mechanism of isoprene-isobutylene rubber is that simple substance bromine contacts with rubber to be replaced by the secondary position hydrogen atom in rubber double bond rapidly and becomes brominated butyl rubber, and react and form hydrogen bromide simultaneously, unreacted bromine simple substance and hydrogen bromide neutralize finally by alkali lye.The difficult point that butyl rubber bromide composes mainly is that reaction process characteristic and system performance characteristic exist contradiction.In response characteristic, easily occur under the environment that product brominated isoprene-isobutylene rubber exists at hydrogen bromide to replace position by the conversion of secondary position to uncle position, the double bond that the simultaneously addition of hydrogen bromide also can make Rubber loss certain, therefore the synthesis of brominated butyl rubber need to be swift in response initiation, neutralize rapidly.In system performance characteristic, the viscosity of the alkane solution of reactant isoprene-isobutylene rubber is very high (being generally greater than 70cP), the volume ratio great disparity (being generally 1/10 ~ 1/20) of traditional bromine source---bromoalkane solution and butyl rubber solution, the short mix of reactant is not easy to realize, and reaction local microenvironment is difficult to control; Neutralizer and bromination reaction liquid are immiscible profit system, and the transfer rate of product brominated hydrogen between oil solution to the aqueous solution needs to strengthen further, and these factors all drastically influence the quality product of brominated butyl rubber.
Based on the quick initiation of brominated butyl rubber building-up reactions, the ultimate principle of Quick stop, the present invention proposes to carry out bromination reaction using the mixed gas of bromo-nitrogen as bromine source, by traditional liquid liquid system being changed into the mixing process of gas-liquid system strengthening bromine and butyl rubber solution, neutralizer and bromination reaction liquid; Use the method for Hi-mixer cascade reaction pipeline strictly to control the reaction times simultaneously, utilize Kinetic differences and the time series relation thereof of bromination main reaction and transposition side reaction, reduce the probability of translocation reaction and addition reaction, thus obtain high performance brominated butyl rubber product.
Summary of the invention
The object of the invention is to the improvement to existing brominated butyl rubber production technology, middle a kind of brominated butyl rubber production technique is provided.
A kind of brominated butyl rubber production technique, this technique comprises the hybrid reaction of the bromo-nitrogen mixture of bromine vaporizing system, bromo-nitrogen mixture and butyl rubber solution, neutralizer and bromination reaction liquid hybrid reaction and tail gas separation four unit, comprises step as follows:
(1) nitrogen buffer gas passes in bromine vaporizer and contacts with bromine, utilizes the volatility of bromine to obtain the gas mixture of bromo-nitrogen;
(2) bromo-nitrogen mixed gas is passed into the Quick uniform mixing realizing mixed gas and butyl rubber solution in bromination mixing tank, start bromination reaction, the bromination reaction liquid of formation reacts in follow-up bromination reaction pipeline;
(3) by bromination reaction liquid and neutralizer in and liquid Quick uniform mixing in mixing tank, start neutralization reaction, the heterogeneous mixed stream of formation reacts in follow-up neutralization reaction pipeline;
(4) the heterogeneous mixed stream that bromination reaction liquid and neutralizer are formed enters neutralization reaction still and completes neutralization reaction, reaction mixture carries out aftertreatment from extraction at the bottom of still, tail gas (main component is nitrogen) from and the extraction of still top, after purification, can be used for circulation preparation bromo-nitrogen mixed gas or carry out emptying process.
Described bromination mixing tank and in and mixing tank be selected from microstucture mixer, static mixer, venturi mixer or jetting type mixing tank; Service temperature controls at 15 DEG C ~ 45 DEG C.
In described and still be stirring tank, service temperature controls at 15 DEG C ~ 45 DEG C.
The massfraction of described butyl rubber solution is 3% ~ 12%, and solvent is selected from normal hexane, normal heptane or octane, and temperature controls at 15 DEG C ~ 45 DEG C.
In the gas mixture of described bromo-nitrogen, the vapour pressure of bromine is 19kPa ~ 54kPa, and stagnation pressure is 100kPa ~ 300kPa; Mixture temperature controls at 15 DEG C ~ 45 DEG C.
Described neutralizer is the mixed aqueous solution of sodium hydroxide and Sodium Pyrosulfite, and wherein the massfraction of sodium hydroxide is 0.1% ~ 6%, and the massfraction of Sodium Pyrosulfite is 0.05% ~ 3%, and temperature controls at 15 DEG C ~ 45 DEG C.
In bromination reaction pipeline, the reaction times of material controls at 0.2min ~ 2min, and in bromo-nitrogen mixture, the mass ratio of bromine simple substance and isoprene-isobutylene rubber is 0.01 ~ 0.065.
In neutralization reaction pipeline, the reaction times of material controls at 0.1min ~ 1min, and in bromo-nitrogen mixture, in bromine simple substance and neutralizer, the mass ratio of sodium hydroxide is less than 1.0 ~ 1.8.
In and in still reaction times of liquid material control at more than 10min.
Beneficial effect of the present invention is: (1) replaces traditional bromobutyl solution as raw material using bromo-nitrogen mixture, utilizes gas-liquid system to strengthen bromine simple substance and butyl rubber solution, mixing process between neutralizer and bromination reaction liquid; (2) use the method for Hi-mixer cascade reaction pipeline strictly to control the reaction times, reduce the probability of translocation reaction and addition reaction.These features make novel process can obtain the brominated butyl rubber product of high-quality efficiently.Adopt new technology, product bromination degree can regulate and control in 0% ~ 1.8% scope, secondary position bromine content is greater than 97%, rubber degree of unsaturation reduces by 0% ~ 0.9% before the reaction afterwards, and mooney viscosity reduces by 0 ~ 10 before the reaction afterwards.
Accompanying drawing explanation
Fig. 1 is brominated butyl rubber production technological process;
Wherein label is: V-bromine vaporizer; R1-bromination mixing tank; R2-in and mixing tank; R3-in and still; P1-bromination reaction pipeline; P2-neutralization reaction pipeline; C-gas treating system; 1-nitrogen; 2-bromine; 3-bromo-nitrogen mixed gas; 4-butyl rubber solution; 5-neutralizer (mixing solutions of sodium hydroxide and Sodium Pyrosulfite); 6-liquid product; 7-tail gas.
Embodiment
Below by example, the present invention is further described, but content not thereby limiting the invention.
Implementation process is specially assembles reactive system by described in Fig. 1, nitrogen is passed into bromine vaporizer and form bromo-nitrogen mixed gas, alkane solution mixed being incorporated in bromination reaction pipeline in bromination mixing tank of bromo-nitrogen mixture and isoprene-isobutylene rubber carries out bromination reaction, until passing into neutralizer during bromination reaction liquid enters He after mixing tank, neutralizer and bromination reaction liquid react certain hour in neutralization reaction pipeline, finally all materials enter in and still in and retain certain hour, in and the gas that obtains of still top emptying or return nitrogen delivery system after alkaline adsorption post.Reaction product adds stablizer after liquid-phase outlet collection, through boiling water treating, open refining after make solid sample, sample bromination degree and brothers position ratio are measured by nuclear-magnetism, degree of unsaturation is measured by mooney viscosity instrument by titrimetry, mooney viscosity.Result of implementation is as follows:
Embodiment 1:
Nitrogen is passed at bromine evaporator inlet, obtaining temperature is 15 DEG C, pressure is 100kPa, bromine vapor pressure is the gas mixture of 19kPa, be flow into bromination reaction pipeline (bromine/isoprene-isobutylene rubber mass ratio is 0.04) after the isoprene-isobutylene rubber hexane solution of 15 DEG C of massfractions 3% (a kind of microstucture mixer) in a micro-channel mixer mixes by this gas mixture and temperature, the neutralizer being 25 DEG C in another Microtraps hole mixing tank (a kind of microstucture mixer) and temperature after material reacts 1min in bromination reaction pipeline mixes that (massfraction of sodium hydroxide is 1.1%, the massfraction of Sodium Pyrosulfite is 0.5%, bromine/sodium hydroxide mass ratio is 1.60), with still (temperature 18 DEG C) in flowing into after material reacts 1min in neutralization reaction pipeline, liquid material in and still in the reaction times be 10min.Product isoprene-isobutylene rubber bromination degree is 1.33%, secondary position bromine content 98.1%, and degree of unsaturation is 1.20%(initial rubber degree of unsaturation 1.9%), mooney viscosity 33(initial rubber Mooney 40).
Embodiment 2:
Nitrogen is passed at bromine evaporator inlet, obtaining temperature is 15 DEG C, pressure is 300kPa, bromine vapor pressure is the gas mixture of 19kPa, be flow into bromination reaction pipeline (bromine/isoprene-isobutylene rubber mass ratio is 0.041) after the isoprene-isobutylene rubber hexane solution of 15 DEG C of massfractions 5% mixes in a micro-channel mixer by this gas mixture and temperature, material flows into neutralizer that another micro-channel mixer and temperature are 15 DEG C and mixes that (massfraction of sodium hydroxide is 1.1% react 1min in bromination reaction pipeline after, the massfraction of Sodium Pyrosulfite is 0.5%, bromine/sodium hydroxide mass ratio is 1.8), with still (temperature 15 DEG C in flowing into after material reacts 0.1min in neutralization reaction pipeline, pressure normal pressure), liquid material in and still in the reaction times be 11min.Product isoprene-isobutylene rubber bromination degree is 1.21%, secondary position bromine content 99.4%, and degree of unsaturation is 1.31%(initial rubber degree of unsaturation 1.9%), mooney viscosity 32(initial rubber Mooney 40).
Embodiment 3:
Nitrogen is passed at bromine evaporator inlet, obtaining temperature is 25 DEG C, pressure is 200kPa, bromine vapor pressure is the gas mixture of 29kPa, be flow into bromination reaction pipeline (bromine/isoprene-isobutylene rubber mass ratio is 0.038) after the isoprene-isobutylene rubber hexane solution of 25 DEG C of massfractions 5% mixes in a Microtraps hole mixing tank by this gas mixture and temperature, material flows into neutralizer that another Microtraps hole mixing tank and temperature are 25 DEG C and mixes that (massfraction of sodium hydroxide is 1.1% react 2min in bromination reaction pipeline after, the massfraction of Sodium Pyrosulfite is 0.5%, bromine/sodium hydroxide mass ratio is 1.57), with still (temperature 25 DEG C in flowing into after material reacts 0.1min in neutralization reaction pipeline, pressure normal pressure), liquid material in and still in the reaction times be 11min.Product isoprene-isobutylene rubber bromination degree is 1.41%, secondary position bromine content 99.0%, and degree of unsaturation is 1.14%(initial rubber degree of unsaturation 1.9%), mooney viscosity 30(initial rubber Mooney 40).
Embodiment 4:
Nitrogen is passed at bromine evaporator inlet, obtaining temperature is 25 DEG C, pressure is 200kPa, bromine vapor pressure is the gas mixture of 29kPa, bromination reaction pipeline (bromine/isoprene-isobutylene rubber mass ratio is 0.01) is flowed into after the isoprene-isobutylene rubber hexane solution being 25 DEG C of massfractions 5% by this gas mixture and temperature mixes in jet mixer, material flows into neutralizer that another jet mixer and temperature are 25 DEG C and mixes that (massfraction of sodium hydroxide is 0.1% react 2min in bromination reaction pipeline after, the massfraction of Sodium Pyrosulfite is 0.05%, bromine/sodium hydroxide mass ratio is 1.0), with still (temperature 25 DEG C in flowing into after material reacts 0.3min in neutralization reaction pipeline, pressure normal pressure), liquid material in and still in the reaction times be 10min.Product isoprene-isobutylene rubber bromination degree is 0.38%, secondary position bromine content 99.7%, and degree of unsaturation is 1.58%(initial rubber degree of unsaturation 1.9%), mooney viscosity 37(initial rubber Mooney 40).
Embodiment 5:
Nitrogen is passed at bromine evaporator inlet, obtaining temperature is 25 DEG C, pressure is 300kPa, bromine vapor pressure is the gas mixture of 29kPa, be flow into bromination reaction pipeline (bromine/isoprene-isobutylene rubber mass ratio is 0.026) after the isoprene-isobutylene rubber hexane solution of 25 DEG C of massfractions 12% mixes in a Microtraps hole mixing tank by this gas mixture and temperature, it is that the neutralizer of 25 DEG C mixes that (massfraction of sodium hydroxide is 6% with temperature that material flows into react 0.2min in bromination reaction pipeline after in a static mixer, the massfraction of Sodium Pyrosulfite is 3%, bromine/sodium hydroxide mass ratio is 1.71), with still (temperature 25 DEG C in flowing into after material reacts 0.22min in neutralization reaction pipeline, pressure normal pressure), liquid material in and still in the reaction times be 15min.Product isoprene-isobutylene rubber bromination degree is 0.32%, secondary position bromine content 100%, and degree of unsaturation is 1.82%(initial rubber degree of unsaturation 1.9%), mooney viscosity 39(initial rubber Mooney 40).
Embodiment 6:
Nitrogen is passed at bromine evaporator inlet, obtaining temperature is 45 DEG C, pressure is 100kPa, bromine vapor pressure is the gas mixture of 54kPa, be flow into bromination reaction pipeline (bromine/isoprene-isobutylene rubber mass ratio is 0.065) after the isoprene-isobutylene rubber n-heptane solution of 45 DEG C of massfractions 6% mixes in a venturi mixer by this gas mixture and temperature, it is that the neutralizer of 45 DEG C mixes that (massfraction of sodium hydroxide is 0.5% with temperature that material flows into react 2min in bromination reaction pipeline after in another venturi mixer, the massfraction of Sodium Pyrosulfite is 0.25%, bromine/sodium hydroxide mass ratio is 1.41), with still (temperature 25 DEG C in flowing into after material reacts 0.12min in neutralization reaction pipeline, pressure normal pressure), liquid material in and still in the reaction times be 10min.Product isoprene-isobutylene rubber bromination degree is 1.8%, secondary position bromine content 97.1%, and degree of unsaturation is 1.02%(initial rubber degree of unsaturation 1.9%), mooney viscosity 40(initial rubber Mooney 50).
Embodiment 7:
Nitrogen is passed at bromine evaporator inlet, obtaining temperature is 45 DEG C, pressure is 300kPa, bromine vapor pressure is the gas mixture of 54kPa, be flow into bromination reaction pipeline (bromine/isoprene-isobutylene rubber mass ratio is 0.039) after the isoprene-isobutylene rubber octane solution of 45 DEG C of massfractions 5.6% mixes in a jet mixer by this gas mixture and temperature, it is that the neutralizer of 25 DEG C mixes that (massfraction of sodium hydroxide is 0.5% with temperature that material flows into react 1.1min in bromination reaction pipeline after in another jet mixer, the massfraction of Sodium Pyrosulfite is 0.25%, bromine/sodium hydroxide mass ratio is 1.4), with still (temperature 35 DEG C in flowing into after material reacts 1min in neutralization reaction pipeline, pressure normal pressure), liquid material in and still in the reaction times be 10min.Product isoprene-isobutylene rubber bromination degree is 1.35%, secondary position bromine content 97.4%, and degree of unsaturation is 1.12%(initial rubber degree of unsaturation 1.9%), mooney viscosity 42(initial rubber Mooney 50).
Claims (7)
1. a brominated butyl rubber production technique, it is characterized in that, this technique comprises the hybrid reaction of the bromo-nitrogen mixture of bromine vaporizing system, bromo-nitrogen mixture and butyl rubber solution, neutralizer and bromination reaction liquid hybrid reaction and tail gas separation four unit, comprises step as follows:
(1) nitrogen buffer gas passes in bromine vaporizer and contacts with bromine, utilizes the volatility of bromine to obtain the gas mixture of bromo-nitrogen;
(2) bromo-nitrogen mixed gas is passed into the Quick uniform mixing realizing mixed gas and butyl rubber solution in bromination mixing tank, start bromination reaction, the bromination reaction liquid of formation reacts in follow-up bromination reaction pipeline;
(3) by bromination reaction liquid and neutralizer in and Quick uniform mixing in mixing tank, start neutralization reaction, the heterogeneous mixed stream of formation reacts in follow-up neutralization reaction pipeline;
(4) the heterogeneous mixed stream that bromination reaction liquid and neutralizer are formed enters neutralization reaction still and completes neutralization reaction, reaction mixture carries out aftertreatment from extraction at the bottom of still, tail gas from and the extraction of still top, after purification, can be used for circulation preparation bromo-nitrogen mixed gas or carry out emptying process;
In described step (1) bromo-nitrogen gas mixture in the vapour pressure of bromine be 19kPa ~ 54kPa, stagnation pressure is 100kPa ~ 300kPa; Mixture temperature controls at 15 DEG C ~ 45 DEG C;
In described step (2), the massfraction of butyl rubber solution is 3% ~ 12%, and solvent is selected from normal hexane, normal heptane or octane, and temperature controls at 15 DEG C ~ 45 DEG C.
2. a kind of brominated butyl rubber production technique according to claim 1, is characterized in that: described bromination mixing tank and in and mixing tank be selected from microstucture mixer, static mixer, venturi mixer or jetting type mixing tank; Service temperature controls at 15 DEG C ~ 45 DEG C.
3. a kind of brominated butyl rubber production technique according to claim 1, is characterized in that: in described and still be stirring tank, service temperature controls at 15 DEG C ~ 45 DEG C.
4. a kind of brominated butyl rubber production technique according to claim 1, it is characterized in that: described neutralizer is the mixed aqueous solution of sodium hydroxide and Sodium Pyrosulfite, wherein the massfraction of sodium hydroxide is 0.1% ~ 6%, the massfraction of Sodium Pyrosulfite is 0.05% ~ 3%, and temperature controls at 15 DEG C ~ 45 DEG C.
5. a kind of brominated butyl rubber production technique according to claim 1, is characterized in that: in bromination reaction pipeline, the reaction times of material controls at 0.2min ~ 2min, and in bromo-nitrogen mixture, the mass ratio of bromine simple substance and isoprene-isobutylene rubber is 0.01 ~ 0.065.
6. a kind of brominated butyl rubber production technique according to claim 1, it is characterized in that: in neutralization reaction pipeline, the reaction times of material controls at 0.1min ~ 1min, in bromo-nitrogen mixture, in bromine simple substance and neutralizer, the mass ratio of sodium hydroxide is less than 1.0 ~ 1.8.
7. a kind of brominated butyl rubber production technique according to claim 1, is characterized in that: in and in still reaction times of liquid material control at more than 10min.
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| CA2940970C (en) * | 2014-02-28 | 2019-03-19 | Exxonmobil Chemical Patents Inc. | Mooney viscosity stable brominated elastomers |
| CN105218719B (en) * | 2014-06-16 | 2017-06-06 | 中国石油化工股份有限公司 | Prepare the method and thus obtained halogenated butyl rubber of halogenated butyl rubber |
| CN108794307B (en) * | 2018-07-18 | 2022-11-11 | 山东道可化学有限公司 | Micro-reaction system and method for synthesizing 4-bromo-3-methylanisole by solvent method |
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| CN102382223A (en) * | 2011-09-08 | 2012-03-21 | 北京化工大学 | Method for preparing brominated butyl rubber |
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Address after: Jiaxing City, Zhejiang province 314201 Jiaxing port East Avenue South three stage cofferdam Patentee after: Zhejiang cenway new materials Limited by Share Ltd Patentee after: Tsinghua University Address before: Jiaxing City, Zhejiang province 314201 Jiaxing port East Avenue South three stage cofferdam Patentee before: Zhejiang Xinhui Synthetic New Materials Co.,Ltd. Patentee before: Tsinghua University |