CN205182678U - Novel catalyst feed arrangement in carbonic acid ester workshop - Google Patents
Novel catalyst feed arrangement in carbonic acid ester workshop Download PDFInfo
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- CN205182678U CN205182678U CN201520978774.1U CN201520978774U CN205182678U CN 205182678 U CN205182678 U CN 205182678U CN 201520978774 U CN201520978774 U CN 201520978774U CN 205182678 U CN205182678 U CN 205182678U
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Abstract
The utility model provides a novel catalyst feed arrangement in carbonic acid ester workshop, catalyst feed arrangement is including treating into cavity and constant temperature exhaust apparatus, treat to be equipped with the batch feeding end into cavity top, the below is equipped with the feed end, the feeding end connection reation kettle top, constant temperature exhaust apparatus be located treat in the cavity, constant temperature exhaust apparatus connect reation kettle, the catalyst is carried through the batch feeding end by the reaction rectifying column and is into treated into the cavity, react by the speed into its entering of cavity regulation and control reation kettle of treating again, by the top to reation kettle middle part operation, the catalyst distributes downwards from the top, make catalyst and the reverse exchange of raw materials, feed valve gate control catalyst conveying speed, avoid extravagant, the temperature cavity that exhausts with constant temperature keeps reation kettle in the makeup water vapour in, the reactant directly can be in reation kettle bottom extraction, the top of the tower extraction is followed to the accessory substance, the utilization ratio of rectifier unit has been improved, purity also obtains to improve with the productivity.
Description
Technical field
The utility model belongs to a kind of chemical mechanical equipment field, is specifically related to a kind of new catalyst feed arrangement of carbonic ester workshop.
Background technology
Usually the catalyst used in the esterification reaction has liquid acid and solid acid two class, high concentrated acid usually adopts airtight tubing to feed in raw material or adds grease phase with after alcohol dilution, but these two kinds of modes all exist disadvantage: directly add high concentrated acid and grease can be caused because of localized contact concentrated acid to occur the destruction such as carbonization, coking oil component phenomenon; The mode fed intake after being first diluted to finite concentration with alcohol then avoids local grease and contacts with concentrated acid and produce the phenomenon such as carbonization, coking, but the process hazard of dilution is high, concentrated acid can produce a large amount of heat when coordinating with alcohol, control difficulty during cooperation is high, be easy to occur security incident, and the corrosivity of diluted acid to equipment after coordinating is extremely strong, therefore there is high requirement to the material of the device of condiment and conveying, pipeline, pump valve; The main manual type that adopts at present that feeds intake of solid acids directly drops into reactor, the defect of this feeding mode is: feed intake all needs to open feeding intake of reactor and cover property again and feed intake at every turn, and in the process of feeding intake, gas in reactor can be emerged from dog-house, therefore there is certain potential safety hazard, and can air be polluteed.
Methyl ethyl carbonate EMC is the chemical products of the high added value of rising in recent years, and it is a kind of asymmetric carbonic ester, in organic synthesis, medicine, agricultural chemicals, solvent, additive etc., have extensive use.May be used for many Disposal degree batteries, as lithium metal battery, as the cosolvent of its non-aqueous electrolyte, the performance of battery can be improved, as improved its energy density, increase discharge capability, improve stability in use and security, and because it has methyl and ethyl simultaneously, have the characteristic of dimethyl carbonate DMC, diethyl carbonate DEC concurrently, also be the solvent of extraordinary spices and intermediate, therefore have broad application prospects.
The synthetic method of current EMC mainly contains phosgenation, oxidative carbonylation and ester-interchange method, and wherein ester-interchange method is the EMC synthetic method comparatively commonly used.Wherein ester-interchange method mainly contains three kinds of approach, is respectively DMC and DEC ester exchange, DEC and methyl alcohol ester exchange, DMC and ethanol ester exchange.Wherein EMC is synthesized in DMC and ethanol ester exchange is reversible reaction, the catalyst DMC of this reaction and ethanol are the catalyst be comparatively easy to get, and product methyl alcohol can also as the catalyst producing DMC, this product toxicity is little, course of reaction is without " three wastes ", equipment investment is little, and technique is simple, and production purity is high.But for adopting dimethyl carbonate and ethanol to be the device of Catalyst Production methyl ethyl carbonate in prior art, in original production technology, methyl ethyl carbonate can only pass through intermittent reaction, batch fractionating, and methyl ethyl carbonate low conversion rate; From production to product, turnover tank needs, through multiple tracks interval operation and device systems, cannot meet the needs of existing high yield preparation of industrialization methyl ethyl carbonate methyl ethyl carbonate.
Utility model content
In order to solve the problem, the utility model provides a kind of new catalyst feed arrangement of carbonic ester workshop, described catalyst charge device comprises cavity to be entered and constant temperature exhaust apparatus, batch feeding end is provided with above cavity described to be entered, below is provided with feed end, described feed end coupled reaction still top, cavity to be entered described in described constant temperature exhaust apparatus is positioned at, described constant temperature exhaust apparatus connects described reactor;
Further, described constant temperature exhaust apparatus comprises constant temperature exhaust cavity and steam transmitting pipe, described constant temperature exhaust cavity is column structure, and described constant temperature exhaust cavity bottom is positioned at reactor through cavity to be entered, and described exhaust cavity top is through the cavity connects external world to be entered;
Further, described constant temperature exhaust cavity side is provided with opening and connects described steam transmitting pipe by opening, and described steam transmitting pipe is provided with defeated steam valve;
Further, described feed end comprises charging sealing surface, charging aperture and material inlet valve, described charging aperture is arranged on described charging sealing surface, and described material inlet valve is positioned at described charging aperture, and described charging occluding surface extends to the plane that reactor formed for sides all in the middle part of cavity to be entered;
Further, described batch feeding end comprises closed top layer, batching hole and material inlet valve switch, described material inlet valve switch-linear hybrid is on the surface of closed top layer in contrast to the opposite side of cavity to be entered, described material inlet valve switch is connected with described material inlet valve, and described batching hole is arranged on described closed top layer;
Further, a kind of catalyst reaction device of carbonic ester workshop, described catalyst reaction device comprises catalyst charge device, reactor and feedstock device, and described feedstock device connects described catalyst charge device by described reactor;
Further, described catalyst charge device connects described reactor top, and connects described reactor inner chamber by described feed end;
Further, described constant temperature exhaust cavity bottom height is less than described feedstock device height;
The beneficial effects of the utility model are as follows:
1) catalyst is delivered into cavity to be entered by reactive distillation column through batch feeding end, regulate and control its speed entering reactor by cavity to be entered again to react, run in the middle part of reactor by top, catalyst distributes downwards from top, make catalyst and the reverse exchange of raw material, add reaction compartment, react more abundant;
2) material inlet valve and material inlet valve switches are worked in coordination, and can control catalyst transport speed, avoid waste according to real reaction situation;
3) the full of catalyst shortens the raw material reaction time in a kettle.;
4) constant temperature exhaust cavity keeps the temperature in reactor at supplementing water steam, allows raw material and catalyst exist mainly with gaseous state with this, and water droplet can mix coproduct ethanol discharge simultaneously;
5) constant temperature exhaust cavity upper end is higher than feed end to ensure that accessory substance does not affect catalyst, and constant temperature exhaust cavity lower end is positioned at below feedstock device, and the least possible to ensure the raw material of discharging, accessory substance is many as far as possible;
6) reactant directly can in the extraction of reactor bottom, and accessory substance, from overhead extraction, improves the utilization rate of rectifier unit, and purity and productive rate also obtain raising.
Accompanying drawing explanation
Fig. 1 is the structure chart of the utility model catalyst reaction device;
Fig. 2 is the structure chart of the utility model catalyst charge device batch feeding end;
Fig. 3 is the top view of the utility model catalyst charge device feed end.
Detailed description of the invention
In order to make the purpose of this utility model, technical scheme and advantage clearly understand, below in conjunction with drawings and Examples, the utility model is explained in further detail.Should be appreciated that specific embodiment described herein only for explaining the utility model, and be not used in restriction the utility model.On the contrary, the utility model is contained any by the substituting of making on marrow of the present utility model and scope of defining of claim, amendment, equivalent method and scheme.Further, in order to make the public have a better understanding to the utility model, in hereafter details of the present utility model being described, detailedly describe some specific detail sections.Do not have the description of these detail sections can understand the utility model completely for a person skilled in the art yet.
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail, but not as to restriction of the present utility model.Most preferred embodiment is enumerated below for of the present utility model:
As shown in Figure 1-Figure 3, a kind of catalyst reaction device of carbonic ester workshop, described catalyst reaction device comprises catalyst charge device 1, reactor 2 and feedstock device 3, described feedstock device 3 connects described catalyst charge device 1 by described reactor 2, described catalyst charge device 1 connects described reactor 2 top, and connecting described reactor 2 inner chamber by described feed end 13, described feedstock device 3 is arranged on outside in the middle part of described reactor 2.
A kind of new catalyst feed arrangement 1 of carbonic ester workshop, described catalyst charge device 1 comprises cavity 11 to be entered and constant temperature exhaust apparatus 12, cavity 11 to be entered described in described constant temperature exhaust apparatus 12 is positioned at, described constant temperature exhaust apparatus 12 connects described reactor 2.
Batch feeding end 13 is provided with above cavity 11 described to be entered, below is provided with feed end 14, described feed end 13 coupled reaction still 2 top, described feed end 14 comprises charging sealing surface 141, charging aperture 142 and material inlet valve 143, described charging aperture 142 is arranged on described charging sealing surface 141, described material inlet valve 143 is positioned at described charging aperture 142, described charging occluding surface 141 extends to the plane that reactor 2 formed for all sides in the middle part of cavity 11 to be entered, described batch feeding end 13 comprises closed top layer 131, batching hole 132 and material inlet valve switch 133, described material inlet valve switch 133 is arranged on described closed top layer 131 in contrast on the surface of the opposite side of cavity 11 to be entered, described material inlet valve switch 133 is connected with described material inlet valve 143, described batching hole 132 is arranged on described closed top layer 131.
Described constant temperature exhaust apparatus 12 comprises constant temperature exhaust cavity 121 and steam transmitting pipe 122, described constant temperature exhaust cavity 121 is column structure, described constant temperature exhaust cavity 121 bottom is positioned at reactor 2 through cavity 11 to be entered, described constant temperature exhaust cavity 121 top is communicated with the external world through cavity 11 to be entered, described constant temperature exhaust cavity 121 side is provided with opening 123 and connects described steam transmitting pipe 122 by opening 123, described steam transmitting pipe 122 is provided with defeated steam valve 124, and described constant temperature exhaust cavity 121 bottom height is less than described feedstock device 3 height.
The utility model in use, catalyst ethanol and dimethyl carbonate enter reactor 2 at the medium position of reactor 2 from feedstock device 3 with gaseous form, catalyst enters in cavity 11 to be entered from the top of reactor 2 by batching hole 132, material inlet valve 143 on charging aperture 142 controls the speed that catalyst enters reactor 2, catalyst distributes downwards from reactor 2 top, whole reactor 2 is made to be covered with catalyst, after two kinds of raw materials after vaporization enter reactor 2, upwards run through middle part, through the effect of catalyst, produce reverse exchange, at once fully fast reaction, constant temperature exhaust cavity 121 bottom coupled reaction still 2, top connects extraneous, by byproduct of reaction methyl alcohol from reactor 2 top extraction, defeated steam valve 124 controls steam and enters steam transmitting pipe 122 simultaneously, steam transmitting pipe 122 connects constant temperature exhaust cavity 121, after steam enters constant temperature exhaust cavity 121, keep the temperature in cavity 11 to be entered and reactor 2 on the one hand, distilled water hybrid reaction by-product carbinol is got rid of on the other hand, product methyl ethyl carbonate is extracted out at the bottom of still, complete production.
Above-described embodiment, the just one of the utility model more preferably detailed description of the invention, the usual change that those skilled in the art carries out within the scope of technical solutions of the utility model and replacing all should be included in protection domain of the present utility model.
Claims (8)
1. the new catalyst feed arrangement (1) in a carbonic ester workshop, described catalyst charge device (1) is arranged on reactor (2) top, it is characterized in that, described catalyst charge device (1) comprises cavity to be entered (11) and constant temperature exhaust apparatus (12), cavity described to be entered (11) top is provided with batch feeding end (13), below is provided with feed end (14), described feed end (13) coupled reaction still (2) top, cavity to be entered (11) described in described constant temperature exhaust apparatus (12) is positioned at, described constant temperature exhaust apparatus (12) connects described reactor (2).
2. catalyst charge device (1) according to claim 1, it is characterized in that, described constant temperature exhaust apparatus (12) comprises constant temperature exhaust cavity (121) and steam transmitting pipe (122), described constant temperature exhaust cavity (121) is column structure, described constant temperature exhaust cavity (121) bottom is positioned at reactor (2) through cavity to be entered (11), and described constant temperature exhaust cavity (121) top is communicated with extraneous through cavity to be entered (11).
3. catalyst charge device (1) according to claim 2, it is characterized in that, described constant temperature exhaust cavity (121) side is provided with opening (123) and connects described steam transmitting pipe (122) by opening (123), and described steam transmitting pipe (122) is provided with defeated steam valve (124).
4. catalyst charge device (1) according to claim 2, it is characterized in that, described feed end (14) comprises charging sealing surface (141), charging aperture (142) and material inlet valve (143), described charging aperture (142) is arranged on described charging sealing surface (141), described material inlet valve (143) is positioned at described charging aperture (142), and described charging sealing surface (141) extends to the plane that reactor (2) formed for all sides, cavity to be entered (11) middle part.
5. catalyst charge device (1) according to claim 4, it is characterized in that, described batch feeding end (13) comprises closed top layer (131), batching hole (132) and material inlet valve switch (133), described material inlet valve switch (133) is arranged on described closed top layer (131) in contrast on the surface of the opposite side of cavity to be entered (11), described material inlet valve switch (133) is connected with described material inlet valve (143), and described batching hole (132) is arranged on described closed top layer (131).
6. the catalyst reaction device in a carbonic ester workshop, based on the catalyst charge device (1) described in the claims 1-5, it is characterized in that, described catalyst reaction device comprises catalyst charge device (1), reactor (2) and feedstock device (3), and described feedstock device (3) connects described catalyst charge device (1) by described reactor (2).
7. catalyst reaction device according to claim 6, is characterized in that, described catalyst charge device (1) connects described reactor (2) top, and connects described reactor (2) inner chamber by described feed end (13).
8. catalyst reaction device according to claim 6, is characterized in that, described feedstock device (3) is arranged on outside, described reactor (2) middle part, and described constant temperature exhaust cavity (121) bottom height is less than described feedstock device (3) highly.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520978774.1U CN205182678U (en) | 2015-11-30 | 2015-11-30 | Novel catalyst feed arrangement in carbonic acid ester workshop |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520978774.1U CN205182678U (en) | 2015-11-30 | 2015-11-30 | Novel catalyst feed arrangement in carbonic acid ester workshop |
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| Publication Number | Publication Date |
|---|---|
| CN205182678U true CN205182678U (en) | 2016-04-27 |
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|---|---|---|---|
| CN201520978774.1U Expired - Fee Related CN205182678U (en) | 2015-11-30 | 2015-11-30 | Novel catalyst feed arrangement in carbonic acid ester workshop |
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2015
- 2015-11-30 CN CN201520978774.1U patent/CN205182678U/en not_active Expired - Fee Related
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160427 Termination date: 20201130 |