CN212741186U - Pinacolone continuous production system - Google Patents
Pinacolone continuous production system Download PDFInfo
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- CN212741186U CN212741186U CN202022024339.9U CN202022024339U CN212741186U CN 212741186 U CN212741186 U CN 212741186U CN 202022024339 U CN202022024339 U CN 202022024339U CN 212741186 U CN212741186 U CN 212741186U
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Abstract
The utility model relates to a pinacolone serialization production system, its characterized in that: comprises a continuous addition reaction module and a continuous condensation reaction module; the utility model discloses addition reaction takes place for isoamylene and hydrochloric acid in the raw materials of pinacolone, and the reinforced of isoamylene and hydrochloric acid is all cooled through the cooler, then under the pump sending of addition reaction circulating pump, carries out the endless addition reaction, adopts excessive hydrochloric acid and two-stage addition reactor, guarantees the abundant reaction of isoamylene, adopts the control of circulation serialization, can realize the conversion rate of isoamylene more than 99%; the output end of the buffer tank and the output end of the formaldehyde are directly connected in parallel and cooled through a condensation cooler, then the cyclic condensation reaction is carried out under the cyclic pumping of the condensation reaction, the sufficient reaction of the diisopentane dichloride is ensured by adopting the excessive formaldehyde, the control of cyclic serialization is adopted, the conversion rate of the diisopentane dichloride is more than 99 percent, the conversion efficiency of the product is improved, and the continuous production is realized.
Description
Technical Field
The utility model relates to a pinacolone production technical field especially relates to a pinacolone serialization production system.
Background
Pinacolone, i.e. 3, 3-dimethyl-2-butanone, is an important raw material for producing pesticides such as triadimefon and multi-effect wakame and is an intermediate for producing various fine chemical products such as medicines and dyes. In a general pinacolone production process, isoamylene and hydrochloric acid are added to generate 2-chloroisopentane, and then the 2-chloroisopentane and formaldehyde are subjected to a condensation reaction to produce pinacolone and hydrochloric acid;
in the general addition reaction and condensation reaction of pinacolone, the degree of automatic continuity is low, which causes the problem of low conversion rate of isoamylene to pinacolone.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a pinacolone serialization production system, adopt independent reinforced mode in can solving general pinacolone's the production, the intermediate product need be transported, fails to carry out effectual circulation reaction, leads to the problem that serialization degree is low.
In order to solve the technical problem, the utility model adopts the technical scheme that: a continuous pinacolone production system has the innovation points that: comprises a continuous addition reaction module and a continuous condensation reaction module;
the continuous addition reaction module comprises an isoamylene storage tank, a hydrochloric acid storage tank, an isoamylene cooler, a byproduct hydrochloric acid cooling tower, a falling film reaction tower, a primary addition reactor, a secondary addition reactor, an addition reaction cooler, an addition reaction circulating pump, a continuous delayer and a buffer tank;
isoamylene is stored in the isoamylene storage tank, the output end of the isoamylene storage tank is connected to an isoamylene cooler through a pipeline, and the isoamylene in the isoamylene storage tank is output to the isoamylene cooler to realize the cooling of the isoamylene; the output end of the isoamylene cooler is connected to the falling film reaction tower through a pipeline; the falling film reaction tower is also connected to a byproduct hydrochloric acid cooling tower through a pipeline, and a byproduct hydrochloric acid of a condensation reaction in the pinacolone production is cooled by the byproduct hydrochloric acid cooling tower and sent to the falling film reaction tower; the output end of the falling film reaction tower is connected with the primary addition reactor in series, so that isoamylene and by-product hydrochloric acid generated by condensation reaction enter the primary addition reactor;
hydrochloric acid is stored in the hydrochloric acid storage tank, the output end of the hydrochloric acid storage tank is connected to an addition reaction cooler through a pipeline, the output end of the addition reaction cooler is connected to a primary addition reactor, and an addition reaction circulating pump is arranged between the addition reaction cooler and the hydrochloric acid storage tank; pumping hydrochloric acid in a hydrochloric acid storage tank through an addition reaction circulating pump, cooling the hydrochloric acid by an addition reaction cooler, then allowing the hydrochloric acid to enter a primary addition reactor, and performing primary addition reaction on cooled isoamylene and cooled byproduct hydrochloric acid which are input into the primary addition reactor in a falling film reaction tower;
the output end of the first-stage addition reactor is connected to the second-stage addition reactor, and hydrochloric acid, isoamylene and part of generated dichloroisopentane in the first-stage addition reactor are input into the second-stage addition reactor; a circulating output port is arranged on the second-stage addition reactor and is connected to the input end of the addition reaction circulating pump through a pipeline, so that the circulating reaction of the materials in the second-stage addition reactor through the first-stage addition reactor and the second-stage addition reactor is realized; the secondary addition reactor is also provided with a discharge port, the discharge port is connected to the continuous delayer through a pipeline, and the materials after reaction in the secondary addition reactor are input into the continuous delayer for continuous layering; the output end of the continuous delayer is connected to the buffer tank through a pipeline, so that the dichloroisopentane in the continuous delayer is conveyed to the buffer tank for standby;
the continuous condensation reaction module comprises a formaldehyde storage tank, a condensation reactor, a condensation reaction circulating pump, a light component removal tower, a condensation cooler, a discharging cooler, a continuous separator, a crude pinacolone storage tank and a dilute hydrochloric acid storage tank;
the output end of the dichloro isopentane in the buffer tank is connected to a condensation reaction circulating pump through a pipeline, the output end of the condensation reaction circulating pump is connected to a condensation cooler through a pipeline, and the output end of the condensation cooler is connected to a condensation reactor through a pipeline; a circulating pipeline connected with the output end of the buffer tank is arranged on the condensation reactor, and the circulation of materials in the condensation reactor is realized through a condensation reaction circulating pump; the condensation reaction circulating pump, the condensation cooler and the condensation reactor are provided with two groups, the two groups are independently connected with the output end of the buffer tank to form circulation, and the condensation reactors in the two groups of connected circulation structures are communicated through a pipeline to realize the series connection of the two groups of condensation reactors;
the formaldehyde storage tank stores 36% formaldehyde, and the output end of the formaldehyde storage tank is connected in parallel with the output end of the buffer tank through a pipeline;
the discharge cooler is connected to the condensation reactor to realize the output of the product after the condensation reaction in the condensation reactor; the output end of the discharge cooler is provided with a continuous separator, so that the materials after reaction in the condensation reactor are continuously layered in the continuous separator, and the output end of the continuous separator is connected to a crude pinacoline storage tank through a pipeline so as to output the crude pinacoline; the output end of the continuous separator is connected with a dilute hydrochloric acid storage tank through a pipeline to realize the output of the byproduct dilute hydrochloric acid;
the top of the light component removal tower is provided with a condenser, and the bottom of the light component removal tower is respectively connected with the output ends of the condensation reactor and the buffer tank, so that the raw materials evaporated by condensation reaction in the condensation reactor enter the light component removal tower to be cooled and refluxed, and the refluxed components enter the condensation reaction circulation.
Furthermore, the byproduct hydrochloric acid cooling tower is connected with the light component removal tower through a pipeline, so that the hydrochloric acid adsorbed in the light component removal tower enters the byproduct hydrochloric acid cooling tower to provide part of raw materials for the pinacolone addition reaction.
Furthermore, the two-stage addition reactor, the continuous delayer and the buffer tank are all provided with tail gas discharge ports, and the tail gas discharge ports are connected with a tail gas absorption tower through pipelines.
Furthermore, a hydrochloric acid return pipeline is arranged on the continuous delayer and provided with two pipelines, one pipeline is connected with the output end of the hydrochloric acid storage tank in series, so that cyclic utilization is realized, and the other pipeline is used for recovering dilute hydrochloric acid.
Furthermore, a nitrogen output pipeline is connected in parallel on a pipeline connected between the first-stage addition reactor and the second-stage addition reactor, and the end part of the pipeline is connected with a nitrogen source.
Furthermore, the side of the light component removal tower is also provided with a volatilization absorption pipeline connected with the condensation reactor, the discharge cooler and the continuous separator, and the volatilization absorption pipeline is also connected with a tail gas treatment unit.
The utility model has the advantages that:
1) the utility model discloses addition reaction takes place for isoamylene and hydrochloric acid in the raw materials of pinacolone, and the reinforced of isoamylene and hydrochloric acid is all cooled through the cooler, then under the pump sending of addition reaction circulating pump, carries out the endless addition reaction, adopts excessive hydrochloric acid and two-stage addition reactor, guarantees the abundant reaction of isoamylene, adopts the control of circulation serialization, can realize the conversion rate of isoamylene more than 99%; the output end of the buffer tank and the output end of the formaldehyde are directly connected in parallel and cooled through a condensation cooler, then the cyclic condensation reaction is carried out under the cyclic pumping of the condensation reaction, the sufficient reaction of the diisopentane dichloride is ensured by adopting the excessive formaldehyde, the control of cyclic serialization is adopted, the conversion rate of the diisopentane dichloride is more than 99 percent, the conversion efficiency of the product is improved, and the continuous production is realized.
Drawings
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
Fig. 1 is a structural diagram of the continuous pinacolone production system of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention, as generally described and illustrated in the figures herein, may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate the position or positional relationship based on the position or positional relationship shown in the drawings, or the position or positional relationship which is usually placed when the product of the present invention is used, and are only for convenience of description and simplification of the description, but do not indicate or imply that the device or element referred to must have a specific position, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal", "vertical" and the like do not imply that the components are required to be absolutely horizontal or pendant, but rather may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
A continuous pinacolone production system as shown in fig. 1, which comprises a continuous addition reaction module 1 and a continuous condensation reaction module 2.
The continuous addition reaction module 1 comprises an isoamylene storage tank 3, a hydrochloric acid storage tank 4, an isoamylene cooler 5, a byproduct hydrochloric acid cooling tower 6, a falling film reaction tower 7, a primary addition reactor 8, a secondary addition reactor 9, an addition reaction cooler 10, an addition reaction circulating pump 11, a continuous delayer 12 and a buffer tank 13.
Isoamylene is stored in the isoamylene storage tank 3, the output end of the isoamylene storage tank 3 is connected to an isoamylene cooler 5 through a pipeline, and the isoamylene in the isoamylene storage tank 3 is output to the isoamylene cooler 5 to realize the cooling of the isoamylene; the output end of the isoamylene cooler 5 is connected to the falling film reaction tower 7 through a pipeline; the falling film reaction tower 7 is also connected to a byproduct hydrochloric acid cooling tower 6 through a pipeline, and the byproduct hydrochloric acid of the condensation reaction in the pinacolone production is cooled by the byproduct hydrochloric acid cooling tower 6 and sent to the falling film reaction tower 7; the output end of the falling film reaction tower 7 is connected with the primary addition reactor 8 in series, so that isoamylene and by-product hydrochloric acid generated by condensation reaction enter the primary addition reactor 8.
Hydrochloric acid is stored in the hydrochloric acid storage tank 4, the output end of the hydrochloric acid storage tank 4 is connected to the addition reaction cooler 10 through a pipeline, the output end of the addition reaction cooler 10 is connected to the primary addition reactor 8, and an addition reaction circulating pump 11 is arranged between the addition reaction cooler 10 and the hydrochloric acid storage tank 4; hydrochloric acid in the hydrochloric acid storage tank 2 is pumped by an addition reaction circulating pump 11 to pass through an addition reaction cooler 10 to be cooled and then enter a primary addition reactor 8, and the cooled isoamylene and cooled byproduct hydrochloric acid input into the primary addition reactor 8 in the falling film reaction tower 7 are subjected to primary addition reaction.
The output end of the first-stage addition reactor 8 is connected to the second-stage addition reactor 9, and the hydrochloric acid, the isoamylene and part of the generated dichloroisopentane in the first-stage addition reactor 8 are input into the second-stage addition reactor 9; a circulating output port is arranged on the secondary addition reactor 9 and is connected to the input end of an addition reaction circulating pump 11 through a pipeline, so that the circulating reaction of the materials in the secondary addition reactor 9 through the primary addition reactor 8 and the secondary addition reactor 9 is realized; the secondary addition reactor 9 is also provided with a discharge port which is connected to the continuous delayer 12 through a pipeline, and the materials after reaction in the secondary addition reactor 9 are input into the continuous delayer 12 for continuous delamination; the output end of the continuous delayer 12 is connected to the buffer tank 13 through a pipeline, so that the dichloroisopentane in the continuous delayer 12 is conveyed to the buffer tank 13 for standby.
The continuous condensation reaction module 2 comprises a formaldehyde storage tank 14, a condensation reactor 15, a condensation reaction circulating pump 16, a light component removal tower 17, a condensation cooler 18, a discharge cooler 19, a continuous separator 20, a crude pinacolone storage tank 21 and a dilute hydrochloric acid storage tank 22.
The output end of the dichloroisopentane in the buffer tank 13 is connected to a condensation reaction circulating pump 16 through a pipeline, the output end of the condensation reaction circulating pump 16 is connected to a condensation cooler 18 through a pipeline, and the output end of the condensation cooler 18 is connected to a condensation reactor 15 through a pipeline; a circulating pipeline connected with the output end of the buffer tank 13 is arranged on the condensation reactor 15, and the circulation of materials in the condensation reactor 15 is realized through a condensation reaction circulating pump 16; condensation reaction circulating pump 16, condensation cooler 18, condensation reactor 15 have two sets ofly, and all independent connections form the circulation at the output of buffer tank 13, and lead to through the pipeline between the condensation reactor 15 in this two sets of circulation structures of connecting, realize the series connection of two sets of condensation reactors.
The formaldehyde storage tank 14 stores 36% formaldehyde, and the output end of the formaldehyde storage tank 14 is connected in parallel with the output end of the buffer tank 13 through a pipeline.
The discharging cooler 19 is connected to the condensation reactor 15 to realize the output of the product after the condensation reaction in the condensation reactor 15; the output end of the discharging cooler 19 is provided with a continuous separator 20 to realize continuous layering of the reacted materials in the condensation reactor 15 in the continuous separator 20, and the output end of the continuous separator 20 is connected to a crude pinacolone storage tank 21 through a pipeline to realize the output of the crude pinacolone; the output end of the continuous separator 20 is connected with a dilute hydrochloric acid storage tank 22 through a pipeline, so that the output of the byproduct dilute hydrochloric acid is realized.
The top of the light component removal tower 17 is provided with a condenser, and the bottom end of the light component removal tower 17 is respectively connected with the condensation reactor 15 and the output end of the buffer tank 13, so that the raw materials evaporated by condensation reaction in the condensation reactor 15 enter the light component removal tower 17 for cooling reflux, and the refluxed components enter the condensation reaction circulation.
The byproduct hydrochloric acid cooling tower 6 is connected with the light component removal tower 17 through a pipeline, so that the hydrochloric acid adsorbed in the light component removal tower 17 enters the byproduct hydrochloric acid cooling tower 6 to provide part of raw materials for the pinacolone addition reaction.
And tail gas discharge ports are arranged on the secondary addition reactor 9, the continuous delayer 12 and the buffer tank 13 and are connected with a tail gas absorption tower 23 through pipelines.
The continuous delayer 12 is provided with a hydrochloric acid return pipeline 24, the hydrochloric acid return pipeline 24 is provided with two pipelines, one pipeline is connected with the output end of the hydrochloric acid storage tank 4 in series to realize cyclic utilization, and the other pipeline is used for recovering dilute hydrochloric acid.
A nitrogen output pipeline is connected in parallel on the pipeline connected between the first-stage addition reactor 8 and the second-stage addition reactor 9, and the end part of the pipeline is connected with a nitrogen source 25.
The side of the light component removing tower 17 is also provided with a volatilization absorption pipeline 26 connected with the condensation reactor 15, the discharge cooler 19 and the continuous separator 20, and the volatilization absorption pipeline 26 is also connected with a tail gas treatment unit 27.
It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the foregoing embodiments and descriptions are provided only to illustrate the principles of the present invention without departing from the spirit and scope of the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (6)
1. A pinacolone serialization production system which characterized in that: comprises a continuous addition reaction module and a continuous condensation reaction module;
the continuous addition reaction module comprises an isoamylene storage tank, a hydrochloric acid storage tank, an isoamylene cooler, a byproduct hydrochloric acid cooling tower, a falling film reaction tower, a primary addition reactor, a secondary addition reactor, an addition reaction cooler, an addition reaction circulating pump, a continuous delayer and a buffer tank;
isoamylene is stored in the isoamylene storage tank, the output end of the isoamylene storage tank is connected to an isoamylene cooler through a pipeline, and the isoamylene in the isoamylene storage tank is output to the isoamylene cooler to realize the cooling of the isoamylene; the output end of the isoamylene cooler is connected to the falling film reaction tower through a pipeline; the falling film reaction tower is also connected to a byproduct hydrochloric acid cooling tower through a pipeline, and a byproduct hydrochloric acid of a condensation reaction in the pinacolone production is cooled by the byproduct hydrochloric acid cooling tower and sent to the falling film reaction tower; the output end of the falling film reaction tower is connected with the primary addition reactor in series, so that isoamylene and by-product hydrochloric acid generated by condensation reaction enter the primary addition reactor;
hydrochloric acid is stored in the hydrochloric acid storage tank, the output end of the hydrochloric acid storage tank is connected to an addition reaction cooler through a pipeline, the output end of the addition reaction cooler is connected to a primary addition reactor, and an addition reaction circulating pump is arranged between the addition reaction cooler and the hydrochloric acid storage tank; pumping hydrochloric acid in a hydrochloric acid storage tank through an addition reaction circulating pump, cooling the hydrochloric acid by an addition reaction cooler, then allowing the hydrochloric acid to enter a primary addition reactor, and performing primary addition reaction on cooled isoamylene and cooled byproduct hydrochloric acid which are input into the primary addition reactor in a falling film reaction tower;
the output end of the first-stage addition reactor is connected to the second-stage addition reactor, and hydrochloric acid, isoamylene and part of generated dichloroisopentane in the first-stage addition reactor are input into the second-stage addition reactor; a circulating output port is arranged on the second-stage addition reactor and is connected to the input end of the addition reaction circulating pump through a pipeline, so that the circulating reaction of the materials in the second-stage addition reactor through the first-stage addition reactor and the second-stage addition reactor is realized; the secondary addition reactor is also provided with a discharge port, the discharge port is connected to the continuous delayer through a pipeline, and the materials after reaction in the secondary addition reactor are input into the continuous delayer for continuous layering; the output end of the continuous delayer is connected to the buffer tank through a pipeline, so that the dichloroisopentane in the continuous delayer is conveyed to the buffer tank for standby;
the continuous condensation reaction module comprises a formaldehyde storage tank, a condensation reactor, a condensation reaction circulating pump, a light component removal tower, a condensation cooler, a discharging cooler, a continuous separator, a crude pinacolone storage tank and a dilute hydrochloric acid storage tank;
the output end of the dichloro isopentane in the buffer tank is connected to a condensation reaction circulating pump through a pipeline, the output end of the condensation reaction circulating pump is connected to a condensation cooler through a pipeline, and the output end of the condensation cooler is connected to a condensation reactor through a pipeline; a circulating pipeline connected with the output end of the buffer tank is arranged on the condensation reactor, and the circulation of materials in the condensation reactor is realized through a condensation reaction circulating pump; the condensation reaction circulating pump, the condensation cooler and the condensation reactor are provided with two groups, the two groups are independently connected with the output end of the buffer tank to form circulation, and the condensation reactors in the two groups of connected circulation structures are communicated through a pipeline to realize the series connection of the two groups of condensation reactors;
the formaldehyde storage tank stores 36% formaldehyde, and the output end of the formaldehyde storage tank is connected in parallel with the output end of the buffer tank through a pipeline;
the discharge cooler is connected to the condensation reactor to realize the output of the product after the condensation reaction in the condensation reactor; the output end of the discharge cooler is provided with a continuous separator, so that the materials after reaction in the condensation reactor are continuously layered in the continuous separator, and the output end of the continuous separator is connected to a crude pinacoline storage tank through a pipeline so as to output the crude pinacoline; the output end of the continuous separator is connected with a dilute hydrochloric acid storage tank through a pipeline to realize the output of the byproduct dilute hydrochloric acid;
the top of the light component removal tower is provided with a condenser, and the bottom of the light component removal tower is respectively connected with the output ends of the condensation reactor and the buffer tank, so that the raw materials evaporated by condensation reaction in the condensation reactor enter the light component removal tower to be cooled and refluxed, and the refluxed components enter the condensation reaction circulation.
2. The continuous pinacolone production system according to claim 1, wherein: the byproduct hydrochloric acid cooling tower is connected with the light component removal tower through a pipeline, so that the hydrochloric acid adsorbed in the light component removal tower enters the byproduct hydrochloric acid cooling tower to provide part of raw materials for the pinacolone addition reaction.
3. The continuous pinacolone production system according to claim 1, wherein: and the secondary addition reactor, the continuous delayer and the buffer tank are all provided with tail gas discharge ports, and the tail gas discharge ports are connected with a tail gas absorption tower through pipelines.
4. The continuous pinacolone production system according to claim 1, wherein: the continuous delayer is provided with a hydrochloric acid return pipeline, the hydrochloric acid return pipeline is provided with two pipelines, one pipeline is connected with the output end of the hydrochloric acid storage tank in series, recycling is achieved, and the other pipeline is used for recovering dilute hydrochloric acid.
5. The continuous pinacolone production system according to claim 1, wherein: and a nitrogen output pipeline is connected in parallel on a pipeline connected between the first-stage addition reactor and the second-stage addition reactor, and the end part of the pipeline is connected with a nitrogen source.
6. The continuous pinacolone production system according to claim 1, wherein: and the side edge of the light component removal tower is also provided with a volatilization absorption pipeline connected with the condensation reactor, the discharge cooler and the continuous separator, and the volatilization absorption pipeline is also connected with a tail gas treatment unit.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113061076A (en) * | 2021-04-02 | 2021-07-02 | 开封银河日化有限责任公司 | Preparation method of chloro-tert-pentane |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113061076A (en) * | 2021-04-02 | 2021-07-02 | 开封银河日化有限责任公司 | Preparation method of chloro-tert-pentane |
| CN113061076B (en) * | 2021-04-02 | 2023-09-26 | 开封银河日化有限责任公司 | Preparation method of chloroterpentane |
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