CN105498633A - 2,6-di-tert-butyl-p-cresol antioxidant alkylation reaction device and method - Google Patents
2,6-di-tert-butyl-p-cresol antioxidant alkylation reaction device and method Download PDFInfo
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- CN105498633A CN105498633A CN201610084502.6A CN201610084502A CN105498633A CN 105498633 A CN105498633 A CN 105498633A CN 201610084502 A CN201610084502 A CN 201610084502A CN 105498633 A CN105498633 A CN 105498633A
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- 239000003963 antioxidant agent Substances 0.000 title claims abstract description 21
- 230000003078 antioxidant effect Effects 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000005804 alkylation reaction Methods 0.000 title claims abstract description 18
- NLZUEZXRPGMBCV-UHFFFAOYSA-N Butylhydroxytoluene Chemical compound CC1=CC(C(C)(C)C)=C(O)C(C(C)(C)C)=C1 NLZUEZXRPGMBCV-UHFFFAOYSA-N 0.000 title abstract 3
- 235000010354 butylated hydroxytoluene Nutrition 0.000 title abstract 3
- 238000006243 chemical reaction Methods 0.000 claims abstract description 111
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims abstract description 71
- 238000004064 recycling Methods 0.000 claims abstract description 9
- IWDCLRJOBJJRNH-UHFFFAOYSA-N p-cresol Chemical compound CC1=CC=C(O)C=C1 IWDCLRJOBJJRNH-UHFFFAOYSA-N 0.000 claims abstract description 8
- JOXIMZWYDAKGHI-UHFFFAOYSA-N toluene-4-sulfonic acid Chemical compound CC1=CC=C(S(O)(=O)=O)C=C1 JOXIMZWYDAKGHI-UHFFFAOYSA-N 0.000 claims abstract description 7
- 230000035484 reaction time Effects 0.000 claims description 26
- SKDGWNHUETZZCS-UHFFFAOYSA-N 2,3-ditert-butylphenol Chemical compound CC(C)(C)C1=CC=CC(O)=C1C(C)(C)C SKDGWNHUETZZCS-UHFFFAOYSA-N 0.000 claims description 18
- YXFVVABEGXRONW-UHFFFAOYSA-N toluene Substances CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 18
- 230000029936 alkylation Effects 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 9
- 238000007664 blowing Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 230000006837 decompression Effects 0.000 claims description 4
- 238000009834 vaporization Methods 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- MIJKYXHQIOTHGT-UHFFFAOYSA-N C(C)(C)(C)C=1C(=C(C=CC1)O)C(C)(C)C.CC1=CC=CC=C1 Chemical compound C(C)(C)(C)C=1C(=C(C=CC1)O)C(C)(C)C.CC1=CC=CC=C1 MIJKYXHQIOTHGT-UHFFFAOYSA-N 0.000 claims description 3
- 238000004804 winding Methods 0.000 claims description 3
- 238000004891 communication Methods 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 50
- 238000004519 manufacturing process Methods 0.000 description 11
- 239000000463 material Substances 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- -1 alkyl phenol Chemical compound 0.000 description 1
- 230000002152 alkylating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000001427 coherent effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000018612 quorum sensing Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/04—Pressure vessels, e.g. autoclaves
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/11—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by reactions increasing the number of carbon atoms
- C07C37/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by reactions increasing the number of carbon atoms by addition reactions, i.e. reactions involving at least one carbon-to-carbon unsaturated bond
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a 2,6-di-tert-butyl-p-cresol antioxidant alkylation reaction device and method. The device comprises multiple reaction units, each reaction unit comprises a reaction kettle, a constant-temperature heating stirrer is fixedly installed in each reaction kettle, each reaction kettle is communicated with a tail gas recycle inlet and a gas outlet in a sealed mode, each gas outlet is communicated with an automatic switch in a sealed mode, each reaction kettle is further communicated with a pressure sensor for controlling switch on and off of the corresponding automatic switch, and a communication pipe is communicated between the tail gas recycling inlet of one reaction kettle and the automatic switch of another reaction kettle in a sealed mode. When a recycling device for tail gas generated in a 2,6-di-tert-butyl-p-cresol antioxidant alkylation reaction is used, p-cresol and p-toluenesulfonic acid which are measured standardly are firstly added into the first reaction kettle, vacuumizing and pressure reducing are performed after the first reaction kettle is sealed, and then vaporized isobutene is introduced; when the reaction in the first reaction kettle is nearly full, positive pressure is generated in the reaction kettle and the pressure continuously rises, isobutene introducing is stopped.
Description
Technical field
The present invention relates to the Apparatus and method for of a kind of tail gas recycle recycling, particularly relate to a kind of Apparatus and method for of 2,6-toluene di-tert-butyl phenol antioxidant alkylated reaction.
Background technology
2,6-toluene di-tert-butyl phenol antioxidant (is called for short 2,6,4) be the one of alkyl phenol, it is domestic and international widely used oil-soluble inhibitor, its oxidation resistance is comparatively strong, and heat-resisting and good stability, can be used as the process stabilizing agent etc. after feed antioxidant, rubber antioxidant and synthetic rubber.
At present, a kind of method of producing 2,6-toluene di-tert-butyl phenol is: with isobutene and paracresol be raw material, with p-methyl benzenesulfonic acid for catalyst, under uniform temperature and pressure, carry out alkylated reaction, obtain the mixing material containing 2,6-toluene di-tert-butyl phenol.Need in existing alkylation process to pass into excessive isobutene, to guarantee the complete reaction of paracresol, containing a large amount of unreacted isobutene gas and other hydrocarbon impurities gas in the tail gas produced after alkylated reaction, such gas outer row need could enter atmospheric environment after charcoal absorption process is up to standard.
Therefore, existing production 2, both the waste of part raw material (isobutene) had been caused in the process of 6-toluene di-tert-butyl phenol, also increase the cost of waste gas pollution control and treatment, after especially production scale expands, above problem is even more serious simultaneously, make 2, the production cost of 6-toluene di-tert-butyl phenol increases, and seriously constrains the production-scale expansion of 2,6-toluene di-tert-butyl phenol.
Summary of the invention
The object of this invention is to provide a kind ofly can reduce production cost, the Apparatus and method for of 2, the 6-toluene di-tert-butyl phenol antioxidant alkylated reactions that alleviate environmental pollution.
For achieving the above object, the technical solution used in the present invention is:
A kind of 2, the equipment of 6-toluene di-tert-butyl phenol antioxidant alkylated reaction, it is characterized in that, comprise the reaction member of multiple mutual series winding, each reaction member comprises reactor, reactor internal fixtion is provided with heated at constant temperature agitator, reactor is airtight is communicated with tail gas recycle entrance and gas outlet, gas outlet is airtight is communicated with automatic switch, reactor is also airtight is communicated with the pressure inductor controlling automatic switch break-make, tail gas recycle entrance on one of them reactor and airtightly between the automatic switch on another reactor be communicated with communicating pipe, airtightly on communicating pipe be connected with unilaterally connected valve.
According to the equipment of 2,6-described toluene di-tert-butyl phenol antioxidant alkylated reactions, it is characterized in that, this equipment comprises three described reaction members.
A kind of method of 2,6-toluene di-tert-butyl phenol antioxidant alkylated reaction, is characterized in that, the equipment of the tail gas recycle recycling using above-mentioned 2,6-toluene di-tert-butyl phenol antioxidant alkylated reactions to produce, and step is as follows:
First measured for standard meter paracresol and p-methyl benzenesulfonic acid are added in first reactor, after airtight, vacuumize decompression, pass into the isobutene of vaporization; When reaction in first reactor close to completely, there is malleation in reactor and pressure durations rises time, stop passing into isobutene; The alkylated reaction time controling of second reactor and first reactor, the 3rd reactor and second reactor is staggered half reaction time, after half reaction time is carried out in first reactor reaction, second reactor starts to carry out alkylated reaction, after half reaction time is carried out in second reactor reaction, 3rd reactor starts to carry out alkylated reaction, the like, circulation is carried out.
When the pressure in first reactor reaches 0.08 ~ 0.10MPa, the automatic switch that the pressure inductor be attached thereto controls is opened, on-condensible gas containing isobutene in first reactor flows into second reactor being in negative pressure state by unilaterally connected valve, isobutene wherein participates in reaction as the raw material of second reactor, the like.
When the gas pressure in first reactor drops to 0 ~ 0.001MPa, the automatic switch that the pressure inductor be attached thereto controls cuts out, and second reactor continues reaction; Second reactor reaction close to time complete, the 3rd reactor reaction proceeds to half reaction time, the like.
Second reactor half-reaction week after date to the 3rd reactor the half-reaction cycle during, the alkylation liquid obtained in first reactor completes cooling, exhaust and blowing, and complete the fill process of second time alkylated reaction, start second time alkylated reaction, the like.
The present invention is provided with three reactors, first with second reactor, second with the 3rd reactor, the 3rd stagger successively half reaction time with the alkylated reaction of first reactor, after the alkylated reaction time in first reactor arrives half reaction time, the alkylated reaction in second reactor starts; When the pressure in first reactor reaches 0.08 ~ 0.10MPa, the automatic switch that the pressure inductor be attached thereto controls is opened, and the on-condensible gases such as the isobutene contained in first reactor are entered in second reactor by the unidirectional connection valve be attached thereto and participate in reaction; When the gas pressure in first reactor drops to 0 ~ 0.001MPa, the automatic switch that the pressure inductor be attached thereto controls cuts out; When the pressure in second reactor reaches 0.08 ~ 0.10MPa, the automatic switch that the pressure inductor be attached thereto controls is opened, and the on-condensible gases such as the isobutene contained in second reactor are entered in the 3rd reactor by the unidirectional connection valve be attached thereto and participate in reaction; When the gas pressure in second reactor drops to 0 ~ 0.001MPa, the automatic switch that the pressure inductor be attached thereto controls cuts out; Circular response so successively.
Second reactor half-reaction week after date to the 3rd reactor the half-reaction cycle during, the alkylation liquid obtained in first reactor completes cooling, exhaust, blowing, and complete the fill process of second time alkylated reaction, start second time alkylated reaction, the like.
This equipment using three reactors as a production unit, stagger successively half reaction time between every two reactors during production, the alkylation tail gas that each reactor has reacted rear generation by the communicating pipe between two reactors by isobutene recycling wherein, to reach the object reducing production cost.
Beneficial effect of the present invention is as follows:
By the recycling to tail gas in alkylation process, significantly can reduce the discharge capacity of alkylation tail gas, the isobutene tail gas of recovery can be used as raw material and enters course of reaction, has therefore saved raw material, also save the correlative charges for the treatment of tail gas simultaneously, thus reduce production cost.
Compared with prior art, adopt equipment of the present invention and method can shorten the alkylated reaction cycle and be about 1.5h, can material stream passed be accelerated, thus increase economic efficiency.
Compared with prior art, often produce 1 ton 2,6-toluene di-tert-butyl phenol antioxidant product can recycle isobutene about 0.023 ton, according to charcoal absorption tail gas, then can reduce the use amount about 0.05 ton of active carbon, reduce the isobutene 0.0012 ton that outer row enters atmospheric environment simultaneously, alleviate the pollution to environment.
Accompanying drawing explanation
Fig. 1 is the structural representation of equipment of the present invention, and in figure, arrow is depicted as the direction that the clear and coherent sequence of tail gas stream and reaction cycle are carried out.
In accompanying drawing:
1, tail gas recycle entrance; 2, reactor; 3, heated at constant temperature agitator; 4, pressure inductor; 5, gas outlet; 6, automatic switch; 7, unilaterally connected valve; 8, communicating pipe.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the invention will be further described:
A kind of 2, the equipment of 6-toluene di-tert-butyl phenol antioxidant alkylated reaction, as shown in Figure 1, comprise the reaction member of multiple mutual series winding, each reaction member comprises reactor 2, reactor 2 internal fixtion is provided with heated at constant temperature agitator 3, reactor 2 is airtight is communicated with tail gas recycle entrance 1 and gas outlet 5, gas outlet 5 is airtight is communicated with automatic switch 6, reactor 2 is also airtight is communicated with the pressure inductor 4 controlling automatic switch 6 break-make, tail gas recycle entrance 1 on one of them reactor 2 and airtightly between the automatic switch 6 on another reactor 2 be communicated with communicating pipe 8, airtightly on communicating pipe 8 be connected with unilaterally connected valve 7.In the present embodiment, this equipment comprises three described reaction members.
A kind of method of 2,6-toluene di-tert-butyl phenol antioxidant alkylated reaction, the equipment of the tail gas recycle recycling using 2,6-above-mentioned toluene di-tert-butyl phenol antioxidant alkylated reactions to produce, step is as follows:
First measured for standard meter paracresol and p-methyl benzenesulfonic acid are added in first reactor, after airtight, vacuumize decompression, pass into the isobutene of vaporization; When reaction in first reactor close to completely, there is malleation in reactor and pressure durations rises time, stop passing into isobutene; The alkylated reaction time controling of second reactor and first reactor, the 3rd reactor and second reactor is staggered half reaction time, after half reaction time is carried out in first reactor reaction, second reactor starts to carry out alkylated reaction, after half reaction time is carried out in second reactor reaction, 3rd reactor starts to carry out alkylated reaction, the like, circulation is carried out.
When the pressure in first reactor reaches 0.08 ~ 0.10MPa, the automatic switch that the pressure inductor be attached thereto controls is opened, on-condensible gas containing isobutene in first reactor flows into second reactor being in negative pressure state by unilaterally connected valve, isobutene wherein participates in reaction as the raw material of second reactor, the like.
When the gas pressure in first reactor drops to 0 ~ 0.001MPa, the automatic switch that the pressure inductor be attached thereto controls cuts out, and second reactor continues reaction; Second reactor reaction close to time complete, the 3rd reactor reaction proceeds to half reaction time, the like.
Second reactor half-reaction week after date to the 3rd reactor the half-reaction cycle during, the alkylation liquid obtained in first reactor completes cooling, exhaust and blowing, and complete the fill process of second time alkylated reaction, start second time alkylated reaction, the like.
The present invention has three reactors in alkylated reaction operation, using three alkylated reaction stills as a production unit, often devise a communicating pipe of passing through for isobutene between adjacent two reactors, often the charging time of adjacent two reactors controls to be staggered successively half reaction time.
First measured for standard meter paracresol and p-methyl benzenesulfonic acid are added in first reactor during production, after airtight, vacuumize decompression, pass into the isobutene of vaporization.For fast reaction speed, the present invention adopts heated at constant temperature agitator to replace having at present the agitator of single agitating function, to shorten the alkylating reaction time.When reaction in first reactor close to completely, there is malleation in reactor and pressure durations rises time, stop passing into isobutene.
The alkylated reaction time controling of second reactor and first reactor, the 3rd reactor and second reactor is staggered half reaction time, and reaction principle is constant.After half reaction time is carried out in first reactor reaction, second reactor starts to carry out alkylated reaction, and after half reaction time is carried out in second reactor reaction, the 3rd reactor starts to carry out alkylated reaction, the like, circulation is carried out.
When the pressure in first reactor reaches 0.08 ~ 0.10MPa, the automatic switch that the pressure inductor be attached thereto controls is opened, on-condensible gas containing isobutene in first reactor flows into second reactor being in negative pressure state by unilaterally connected valve, isobutene wherein participates in reaction as the raw material of second reactor, the like.
When the gas pressure in first reactor drops to 0 ~ 0.001MPa, the automatic switch that the pressure inductor be attached thereto controls cuts out, and second reactor continues reaction; Second reactor reaction close to time complete, the 3rd reactor reaction proceeds to half reaction time, the like.Second reactor half-reaction week after date to the 3rd reactor the half-reaction cycle during, the alkylation liquid obtained in first reactor completes cooling, exhaust and blowing, and complete the fill process of second time alkylated reaction, start second time alkylated reaction, the like.
When there is malleation in second reactor and pressure durations rises, stop passing into isobutene, when the pressure in second reactor reaches 0.08 ~ 0.10MPa, the automatic switch that the pressure inductor be attached thereto controls is opened, and the on-condensible gas containing isobutene in second reactor flows into the 3rd just ongoing at alkylated reaction, to be in negative pressure state reactor by the unilaterally connected valve be attached thereto; When the gas pressure in second reactor drops to 0 ~ 0.001MPa, the automatic switch that the pressure inductor be attached thereto controls cuts out, circular response successively, reclaim communication apparatus (communicating pipe) by unidirectional isobutene recyclable and utilize the excess isobutylene gas passed in alkylation process, effectively reduce the discharge of isobutene in alkylation tail gas.
In the present invention, the heated at constant temperature agitator in each reaction member and reactor one_to_one corresponding, the communicating pipe between three reactors is upper is unilaterally connected valve, and automatic switch is controlled by pressure inductor, pressure inductor reactor one_to_one corresponding.At a set temperature, heated at constant temperature agitator heats the reactant in reactor, stirs simultaneously, accelerates material reaction speed, and after reaction stops, heating and stirring operation synchronously stop.The alkylation tail gas produced in reactor through the unidirectional outflow of unilaterally connected valve, enters the tail gas recycle entrance of the next reactor be connected with this reactor along tube connector.Air pressure in pressure inductor Quorum Sensing still, when air pressure reaches the force value of setting, the automatic switch that pressure inductor controls to be attached thereto carries out break-make.Automatic switch is connected with pressure inductor, controls open and-shut mode by the pressure change in reactor.Unilaterally connected valve is arranged on the communicating pipe between the tail gas recycle entrance of adjacent reaction still and gas outlet, and its direction is consistent with the direction of exhaust gas flow, and the direction flowing of tail gas along setting is guaranteed in its effect.Communicating pipe is the tail gas recycle entrance and the gas outlet pipeline that are communicated with adjacent reaction still.
The present invention in alkylation process along with the change of reacting kettle inner pressure, the opening and closing of automatic switch is controlled by pressure inductor, by the unilaterally connected valve between three reactors, guarantee that the flowing of the on-condensible gas containing isobutene flows to low-pressure area by higher-pressure region, make the isobutene contained in alkylation tail gas enter next reactor successively as raw material.The present invention can save material to the recycling of alkylation tail gas, saves the correlative charges for the treatment of tail gas, reduces production cost, decreases the pollution of exhaust emissions to environment simultaneously; And the present invention can shorten the alkylated reaction cycle and is about 1.5h, can material stream passed be accelerated, thus can increase economic efficiency.
Claims (3)
1. one kind 2, the equipment of 6-toluene di-tert-butyl phenol antioxidant alkylated reaction, it is characterized in that, comprise the reaction member of multiple mutual series winding, each reaction member comprises reactor (2), reactor (2) internal fixtion is provided with heated at constant temperature agitator (3), reactor (2) is airtight is communicated with tail gas recycle entrance (1) and gas outlet (5), gas outlet (5) is airtight is communicated with automatic switch (6), reactor (2) is also airtight is communicated with the pressure inductor (4) controlling automatic switch (6) break-make, tail gas recycle entrance (1) on one of them reactor (2) and airtightly between the automatic switch (6) on another reactor (2) be communicated with communicating pipe (8), communicating pipe (8) is upper is airtightly connected with unilaterally connected valve (7).
2. the equipment of 2,6-toluene di-tert-butyl phenol antioxidant alkylated reactions according to claim 1, it is characterized in that, this equipment comprises three described reaction members.
3. the method for a toluene di-tert-butyl phenol antioxidant alkylated reaction, is characterized in that, the equipment of the tail gas recycle recycling using 2,6-toluene di-tert-butyl phenol antioxidant alkylated reactions described in claim 1 or 2 to produce, and step is as follows:
First measured for standard meter paracresol and p-methyl benzenesulfonic acid are added in first reactor, after airtight, vacuumize decompression, pass into the isobutene of vaporization; When reaction in first reactor close to completely, there is malleation in reactor and pressure durations rises time, stop passing into isobutene; The alkylated reaction time controling of second reactor and first reactor, the 3rd reactor and second reactor is staggered half reaction time, after half reaction time is carried out in first reactor reaction, second reactor starts to carry out alkylated reaction, after half reaction time is carried out in second reactor reaction, 3rd reactor starts to carry out alkylated reaction, the like, circulation is carried out;
When the pressure in first reactor reaches 0.08 ~ 0.10MPa, the automatic switch that the pressure inductor be attached thereto controls is opened, on-condensible gas containing isobutene in first reactor flows into second reactor being in negative pressure state by unilaterally connected valve, isobutene wherein participates in reaction as the raw material of second reactor, the like;
When the gas pressure in first reactor drops to 0 ~ 0.001MPa, the automatic switch that the pressure inductor be attached thereto controls cuts out, and second reactor continues reaction; Second reactor reaction close to time complete, the 3rd reactor reaction proceeds to half reaction time, the like;
Second reactor half-reaction week after date to the 3rd reactor the half-reaction cycle during, the alkylation liquid obtained in first reactor completes cooling, exhaust and blowing, and complete the fill process of second time alkylated reaction, start second time alkylated reaction, the like.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610084502.6A CN105498633B (en) | 2016-02-14 | 2016-02-14 | 2,6 toluene di-tert-butyl phenol antioxidant alkylated reaction device and method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610084502.6A CN105498633B (en) | 2016-02-14 | 2016-02-14 | 2,6 toluene di-tert-butyl phenol antioxidant alkylated reaction device and method |
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| CN105498633B CN105498633B (en) | 2017-08-11 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106631705A (en) * | 2016-10-28 | 2017-05-10 | 江苏迈达新材料股份有限公司 | Manufacturing process for alkylating 2, 6-di-tert-butyl-4-methylphenol antioxidants |
| CN111393266A (en) * | 2020-02-21 | 2020-07-10 | 江苏迈达新材料股份有限公司 | BHT alkylation tail gas isobutene recovery process |
| CN113636916A (en) * | 2021-09-17 | 2021-11-12 | 陕西万汇能聚科技有限公司 | Method for synthesizing 2,4, 6-tri-tert-butylphenol |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3940451A (en) * | 1974-09-06 | 1976-02-24 | Heliodoro Monroy | Process of recovering BHT values from mother liquors of the crystallization of BHT obtained by alkylating p-cresol with isobutylene |
| CN1215042A (en) * | 1998-08-25 | 1999-04-28 | 义县精细化工总厂 | Process for pressing preparation of 2,6-di-tert-butyl-p-cresol |
| CN103706298A (en) * | 2012-09-28 | 2014-04-09 | 天津百科生物化学有限公司 | Pressurization reaction kettle |
| CN104496758A (en) * | 2014-12-02 | 2015-04-08 | 安徽海华科技股份有限公司 | M-cresol and p-cresol alkylated continuous reaction method |
| CN205361265U (en) * | 2016-02-14 | 2016-07-06 | 马振英 | Two tert -butyl groups of 2, 6 - are to cresol anti -oxidant alkylation reaction's equipment |
-
2016
- 2016-02-14 CN CN201610084502.6A patent/CN105498633B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3940451A (en) * | 1974-09-06 | 1976-02-24 | Heliodoro Monroy | Process of recovering BHT values from mother liquors of the crystallization of BHT obtained by alkylating p-cresol with isobutylene |
| CN1215042A (en) * | 1998-08-25 | 1999-04-28 | 义县精细化工总厂 | Process for pressing preparation of 2,6-di-tert-butyl-p-cresol |
| CN103706298A (en) * | 2012-09-28 | 2014-04-09 | 天津百科生物化学有限公司 | Pressurization reaction kettle |
| CN104496758A (en) * | 2014-12-02 | 2015-04-08 | 安徽海华科技股份有限公司 | M-cresol and p-cresol alkylated continuous reaction method |
| CN205361265U (en) * | 2016-02-14 | 2016-07-06 | 马振英 | Two tert -butyl groups of 2, 6 - are to cresol anti -oxidant alkylation reaction's equipment |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106631705A (en) * | 2016-10-28 | 2017-05-10 | 江苏迈达新材料股份有限公司 | Manufacturing process for alkylating 2, 6-di-tert-butyl-4-methylphenol antioxidants |
| CN111393266A (en) * | 2020-02-21 | 2020-07-10 | 江苏迈达新材料股份有限公司 | BHT alkylation tail gas isobutene recovery process |
| CN113636916A (en) * | 2021-09-17 | 2021-11-12 | 陕西万汇能聚科技有限公司 | Method for synthesizing 2,4, 6-tri-tert-butylphenol |
| CN113636916B (en) * | 2021-09-17 | 2023-08-29 | 陕西万汇能聚科技有限公司 | Method for synthesizing 2,4, 6-tri-tert-butylphenol |
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| CN105498633B (en) | 2017-08-11 |
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Effective date of registration: 20191204 Address after: 226400 Nine Groups of Gangcheng Village, Changsha Town, Rudong County, Nantong City, Jiangsu Province Patentee after: Jiangsu furida new materials Co.,Ltd. Address before: 277800 room 710, comprehensive building, environmental protection bureau, Guangming Avenue, Xuecheng District, Shandong, Zaozhuang Patentee before: Ma Zhenying |
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Denomination of invention: Equipment and method for alkylation reaction of 2,6-di-tert-butyl-p-cresol antioxidant Granted publication date: 20170811 Pledgee: Jiangsu Rudong Rural Commercial Bank Co.,Ltd. Changsha Branch Pledgor: Jiangsu furida new materials Co.,Ltd. Registration number: Y2024980023561 |