CN212025228U - Cyclohexanol refining system - Google Patents
Cyclohexanol refining system Download PDFInfo
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- CN212025228U CN212025228U CN202020365797.6U CN202020365797U CN212025228U CN 212025228 U CN212025228 U CN 212025228U CN 202020365797 U CN202020365797 U CN 202020365797U CN 212025228 U CN212025228 U CN 212025228U
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Abstract
The utility model discloses defect to prior art zhonghuan cyclohexanol refining system provides a cyclohexanol refining system, including cyclohexanol knockout tower and cyclohexanol rectifying column, the bottom of cyclohexanol knockout tower is equipped with the cyclohexanol pipeline of roughning that is used for discharging roughly cyclohexanol, the upper portion of cyclohexanol rectifying column is equipped with the outer row pipeline of refined cyclohexanol that is used for discharging refined back cyclohexanol, roughly cyclohexanol pipeline establishes ties in proper order and is equipped with first evaporimeter and second evaporimeter, the top of second evaporimeter is equipped with the main intermediate pipe way that is used for discharging evaporation back cyclohexanol, the end intercommunication of main intermediate pipe way to the upper portion of cyclohexanol rectifying column, just it is equipped with the demister to establish ties on the main intermediate pipe way, the demister is located the top of first evaporimeter and second evaporimeter. The utility model discloses a ally oneself with of evaporimeter and use, carry out the secondary evaporation circulation, reduced the outer discharge of cyclohexanol, and improved the purity of cyclohexanol.
Description
Technical Field
The utility model belongs to the technical field of the cyclohexanol preparation, especially, relate to a cyclohexanol refining system.
Background
Cyclohexanol is in the preparation process, the outer purity that improves cyclohexanol is arranged with the outer mode of arranging of cyclohexanol tower bottom pump to the outer row of the outer steam of the general adoption among the prior art, but this kind of refined mode can cause the excessive emission of cyclohexanol usually, lead to the waste of cyclohexanol, the productivity has been reduced, the unit consumption of cyclohexanol distillation column has also been increased in addition, the evaporimeter is when using simultaneously, because cyclohexanol and hydration catalyst thick liquid stew jointly and can lead to mixed hydraulic densification, and then produce and solidify, and the viscosity of this mixed liquid is high, when the temperature is low, block up the bottom pump easily, be unfavorable for the outer row of impurity, consequently, need to overcome the above-mentioned defect of cyclohexanol refined system now.
SUMMERY OF THE UTILITY MODEL
The utility model discloses to prior art zhonghuan cyclohexanol refining system's defect, provide a cyclohexanol refining system, through the ally oneself with of evaporimeter, carry out the secondary evaporation circulation, reduced the outer discharge of cyclohexanol, and improved the purity of cyclohexanol.
The utility model adopts the following technical scheme:
the utility model provides a cyclohexanol refining system, includes cyclohexanol separating tower and cyclohexanol rectifying column, the bottom of cyclohexanol separating tower is equipped with the rough cyclohexanol pipeline that is used for discharging rough cyclohexanol, the upper portion of cyclohexanol rectifying column is equipped with the outer row pipeline of refined cyclohexanol that is used for discharging refined back cyclohexanol, rough cyclohexanol pipeline establishes ties in proper order and is equipped with first evaporimeter and second evaporimeter, the top of second evaporimeter is equipped with the main intermediate pipe who is used for discharging evaporation back cyclohexanol, the terminal intercommunication of main intermediate pipe extremely the upper portion of cyclohexanol rectifying column, just establish ties on the main intermediate pipe and be equipped with the demister, the demister is located the top of first evaporimeter and second evaporimeter.
Preferably, the number of the demister is two or more, and the two or more defoamers are arranged in parallel and are communicated with each other.
Preferably, the top end of the first evaporator is provided with a secondary intermediate pipeline, and the top end of the secondary intermediate pipeline is communicated to the bottom end of the demister.
Preferably, the main intermediate pipe is provided with a branch intermediate pipe and a tip end of the branch intermediate pipe is communicated to the first evaporator.
Preferably, a power transmission pipeline is arranged at the bottom of the first evaporator, the tail end of the power transmission pipeline is communicated to the second evaporator, and a pump is arranged on the power transmission pipeline.
Preferably, the bottom of the second evaporator is provided with a first heavy component discharging pipe for discharging the heavy component at the bottom of the second evaporator.
Preferably, the second evaporator is vertically arranged, and a heating coil which spirals from bottom to top is arranged inside the second evaporator.
Preferably, a cooler is arranged on the refined cyclohexanol discharge pipeline.
Preferably, the bottom of the cyclohexanol distillation column is provided with a second heavy component discharge pipeline for discharging heavy components at the bottom of the cyclohexanol distillation column.
Preferably, the cyclohexanol distillation column is provided with a thermometer and a pressure gauge for monitoring temperature and pressure in the cyclohexanol distillation column.
The utility model has the advantages as follows:
1. the utility model discloses a set up first evaporimeter and second evaporimeter and carry out the evaporation circulation, the evaporation is effectual, has improved the concentration of refined cyclohexanol, has reduced the waste of arranging outward effectively, removes the little liquid drop that contains in the cyclohexanol through first demister and second demister simultaneously, and first demister and second demister link to each other, and the two link up each other, remove the foam and integrate, remove impurity effectively;
2. the spiral heat transfer coil is arranged in the second evaporator, and the second evaporator is vertically arranged, so that the heat transfer efficiency of the second evaporator is effectively increased, and the separation efficiency of cyclohexanol is improved on the basis of low energy consumption;
3. set up manometer and thermometer in the cyclohexanol rectifying column, pressure and temperature in the reboiler adjustable cyclohexanol rectifying column of rethread setting below it, through the synchro control of pressure and temperature, guarantee the rectification effect of cyclohexanol, improve the purity of the cyclohexanol that obtains.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly introduced below, it is obvious that the drawings in the following description are only some embodiments described in the present application, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts;
FIG. 1 is a schematic structural view of example 1;
in the figure: 1. cyclohexanol knockout tower, 101, first pump, 2, first evaporimeter, 201, crude cyclohexanol pipeline, 202, power pipeline, 203, middle pipeline of the left side, 204, middle pipeline of the right side, 205, branch middle pipeline, 3, second evaporimeter, 301, main middle pipeline, 302, second pump, 303, heating coil, 304, first heavy component eduction tube outward, 4, first demister, 5, second demister, 6, cyclohexanol rectifying column, 601, tower bottom circulating line, 602, third pump, 603, manometer, 604, thermometer, 7, reboiler, 8, cooler, 801, fourth pump, 802, refined cyclohexanol efflux pipeline, 9, cyclohexanol storage tank, 10, heavy component storage tank.
Detailed Description
In order to make the technical purpose, technical solution and advantageous effects of the present invention clearer, the technical solution of the present invention is further described below with reference to the accompanying drawings and specific embodiments.
As shown in fig. 1, a cyclohexanol refining system comprises a cyclohexanol separation tower 1 and a cyclohexanol distillation tower 6, wherein a crude cyclohexanol conveying pipeline 201 for discharging crude cyclohexanol is arranged at the bottom of the cyclohexanol separation tower 1, a first pump 101 for providing a cyclohexanol reaction liquid transportation power is arranged on the crude cyclohexanol conveying pipeline 201, and a plurality of check valves for preventing steam from flowing backwards are further arranged on the crude cyclohexanol conveying pipeline 201; first evaporimeter 2 and second evaporimeter 3 are equipped with in proper order in series on the rough cyclohexanol conveying pipe 201, the top of second evaporimeter 3 is equipped with the main intermediate pipe 301 that is used for discharging behind the evaporation cyclohexanol, the terminal intercommunication of main intermediate pipe 301 is to the upper portion of cyclohexanol rectifying column 6, just it is equipped with two demister to establish ties on the main intermediate pipe 301, first demister 4 and second demister 5 promptly, first demister 4 and second demister 5 all are located the top of first evaporimeter and second evaporimeter, first demister 4 and second demister 5 set up in parallel and communicate each other. The upper portion of cyclohexanol rectifying column 6 is equipped with refined cyclohexanol outer discharge pipe 802 that is used for discharging refined cyclohexanol, be equipped with cooler 8 and fourth pump 801 on the outer discharge pipe 802 of refined cyclohexanol, the end of outer discharge pipe of refined cyclohexanol is equipped with cyclohexanol storage tank 9.
Wherein, be equipped with level indicator in the cooler 8, level indicator can help monitoring the condensation effect of cyclohexanol, avoids because the bad phenomenon of condensation that heat transfer surface pollutes etc. and cause.
The cyclohexanol reaction liquid separated by the cyclohexanol separation tower 1 is firstly conveyed into the first evaporator 2 for primary evaporation through a rough cyclohexanol conveying pipeline 201, then enters the second evaporator 3 for secondary evaporation, after the secondary evaporation, the concentration of cyclohexanol contained in a gas-liquid mixture in the top of the second evaporator 3 reaches the rectification requirement, at the moment, the cyclohexanol reaction liquid is conveyed into the first demister 4 and the second demister 5 through a main middle pipeline 301, defoaming is simultaneously carried out, gas components after defoaming enter a cyclohexanol rectifying tower 6 for rectification, and high-purity cyclohexanol obtained after rectification is cooled through a cooler 8 and then is discharged through a refined cyclohexanol discharge pipeline 802 and stored in a cyclohexanol storage tank 9.
For the evaporation effect who improves second evaporimeter 3, the vertical setting of second evaporimeter 3, just the inside of second evaporimeter 3 is equipped with heating coil 303 of spiral from bottom to top, can increase the heat transfer face, improves heat transfer efficiency.
In this embodiment, in order to avoid the waste of cyclohexanol and improve the purity of the cyclohexanol mixture before rectification, the top end of the first evaporator is provided with a left-secondary intermediate pipe 203 connected to the bottom end of the first demister 4 and a right-secondary intermediate pipe 204 connected to the bottom end of the second demister 5. The main intermediate pipe 301 is provided with a branch intermediate pipe 205 and the end of the branch intermediate pipe 205 is connected to the first evaporator 2. The left-time intermediate pipe 203 and the right-time intermediate pipe 204 are used for discharging the liquid components at the bottoms of the first demister 4 and the second demister 5 back to the first evaporator 2, respectively, to enter the circulating evaporation again; the left secondary middle pipeline 203 and the right secondary middle pipeline 204 are respectively provided with a check valve for preventing steam from flowing backwards; the branched intermediate pipe 205 is used to discharge the liquid component descending by gravity in the cyclohexanol gas-liquid mixture back into the first evaporator 2 to enter the circulation evaporation again.
Due to the increase of the liquid component discharged back, the heavy component in the first evaporator 2 increases, and in order to prevent deposition blockage, a power transmission pipeline 202 is arranged at the bottom of the first evaporator 2, the tail end of the power transmission pipeline 202 is communicated to the second evaporator 3, and a second pump 302 for providing transmission power is arranged on the power transmission pipeline 202. Be equipped with the thermometer that is used for monitoring the temperature in power transmission pipeline 202, make things convenient for the technical staff to master temperature data at any time to prevent to lead to mixing liquid densification solidification because the temperature reduces, can rationally regulate and control the circulation flow of second pump 302 according to the temperature of the mixed liquid of thermometer control and thick condition from this, the energy can be saved.
In this embodiment, a first heavy component external discharge pipe 304 for discharging heavy components at the bottom of the second evaporator 3 is arranged at the bottom of the second evaporator 3, the first heavy component external discharge pipe 304 is provided with a stop valve, the stop valve is in a normally closed state, the stop valve is opened to discharge the heavy components only when the system is shut down, the first heavy component external discharge pipe 304 and the power transmission pipe 202 can share the second pump 302, and the discharged heavy components are stored in the heavy component storage tank 10;
wherein, the power transmission pipeline 202 is provided with check valves for preventing steam from flowing back before and after the intersection point of the first recombination outer discharge pipeline 304 and the power transmission pipeline 202.
In this embodiment, a second heavy component discharge pipe for discharging heavy components at the bottom of the cyclohexanol distillation column 6 is disposed at the bottom of the cyclohexanol distillation column 6, a third pump 602 is disposed on the second heavy component discharge pipe, and a terminal of the second heavy component discharge pipe is communicated to the heavy component storage tank 10.
In this embodiment, a reboiler 7 is disposed at the bottom of the cyclohexanol distillation column 6, and the cyclohexanol distillation column 6 is further provided with a thermometer 604 and a pressure gauge 603 for monitoring the temperature and pressure in the cyclohexanol distillation column 6.
Heavy components produced in the cyclohexanol rectifying tower 6 are continuously discharged by the third pump 602 to increase the purity of cyclohexanol, a weir is arranged in the third pump 602, the diaphragm type reciprocating pump is adopted, heavy components and impurities generated by effective discharge reaction can be effectively discharged, a back pressure valve is further arranged at the outlet of the third pump 602, safety and reliability are realized, detection is known, in the refining system adopting evaporation circulation, the cyclohexanol rectifying tower 6 can realize continuous discharge, the temperature of the cyclohexanol rectifying tower 6 is controlled by the reboiler 7, the obtained cyclohexanol is high in purity and small in loss amount, the original intermittent discharge mode is changed, the production efficiency and the purity of cyclohexanol are effectively improved, the purity of the cyclohexanol is improved to 99.9% from 99.3%, the purity is high, the quality is good, and the production cost is reduced.
The refining process of the utility model is mainly as follows: the cyclohexanol reaction liquid separated from the cyclohexanol separation tower 1 is firstly conveyed into a first evaporator 2 for primary evaporation through a rough cyclohexanol conveying pipeline 201, then enters a second evaporator 3 for secondary evaporation, after the secondary evaporation, the concentration of cyclohexanol contained in a gas-liquid mixture in the top of the second evaporator 3 reaches the rectification requirement, at the moment, the cyclohexanol reaction liquid is conveyed into a first demister 4 and a second demister 5 through a main middle pipeline 301, defoaming is simultaneously carried out, gas components after defoaming enter a cyclohexanol rectifying tower 6 for rectification, and high-purity cyclohexanol obtained after rectification is cooled through a refined cyclohexanol discharge pipeline 802 and a cooler 8 and then is stored in a cyclohexanol storage tank 9; in order to further improve the purity of cyclohexanol before rectification, liquid drops (mainly as heavy components) contained in the gas-liquid mixture output by the second evaporator 3 and the heavy components separated from the demister return to the evaporation circulation system again, secondary evaporation is carried out through the first evaporator 2 and the second evaporator 3 in sequence, finally the heavy components are continuously discharged from the bottom of the cyclohexanol rectifying tower 6, and the heavy components at the bottom of the second evaporator 3 are discharged out of the system through a first heavy component outer discharge pipeline when the system is stopped.
The utility model discloses a set up first evaporimeter and second evaporimeter and carry out the evaporation circulation, the evaporation is effectual, has improved the concentration of refined cyclohexanol, has reduced the waste of arranging outward effectively, removes the little liquid drop that contains in the cyclohexanol through first demister and second demister simultaneously, and first demister and second demister link to each other, and the two link up each other, remove the foam and integrate, the effectual impurity of detaching;
finally, it should be noted that: the above-mentioned embodiments are only used for illustrating but not limiting the technical solution of the present invention, and any equivalent replacement and modification or partial replacement which do not depart from the spirit and scope of the present invention should be covered within the protection scope of the claims of the present invention.
Claims (10)
1. The utility model provides a cyclohexanol refining system, includes cyclohexanol separating tower and cyclohexanol rectifying column, the bottom of cyclohexanol separating tower is equipped with the rough cyclohexanol conveying pipeline who is used for discharging rough cyclohexanol, the upper portion of cyclohexanol rectifying column is equipped with the outer pipeline of arranging of refined cyclohexanol that is used for discharging refined back cyclohexanol, its characterized in that: the rough cyclohexanol conveying pipeline is sequentially provided with a first evaporator and a second evaporator in series, the top of the second evaporator is provided with a main middle pipeline used for discharging evaporated cyclohexanol, the tail end of the main middle pipeline is communicated to the upper part of the cyclohexanol rectifying tower, a demister is arranged on the main middle pipeline in series, and the demister is positioned above the first evaporator and the second evaporator.
2. The cyclohexanol refining system of claim 1, wherein: the number of demister is more than two, more than two demister sets up in parallel and communicates each other.
3. The cyclohexanol refining system of claim 2, wherein: and a secondary intermediate pipeline is arranged at the top end of the first evaporator, and the top end of the secondary intermediate pipeline is communicated to the bottom end of the demister.
4. The cyclohexanol refining system of claim 1, wherein: the main intermediate pipeline is provided with a branch intermediate pipeline, and the tail end of the branch intermediate pipeline is communicated to the first evaporator.
5. Cyclohexanol purification system according to any one of claims 1 to 4, characterised in that: the bottom of the first evaporator is provided with a power conveying pipeline, the tail end of the power conveying pipeline is communicated to the second evaporator, and a pump is arranged on the power conveying pipeline.
6. The cyclohexanol refining system of claim 5, wherein: and a first heavy component outer discharge pipeline for discharging heavy components at the bottom of the second evaporator is arranged at the bottom of the second evaporator.
7. The cyclohexanol refining system of claim 5, wherein: the second evaporator is vertically arranged, and a heating coil which is spiral from bottom to top is arranged in the second evaporator.
8. The cyclohexanol refining system of claim 1, wherein: and a cooler is arranged on the refined cyclohexanol discharge pipeline.
9. The cyclohexanol refining system of claim 1, wherein: and a second heavy component discharge pipeline for discharging the heavy components at the bottom of the rectifying tower is arranged at the bottom of the rectifying tower.
10. The cyclohexanol refining system of claim 1, wherein: the rectifying tower is provided with a thermometer and a pressure gauge for monitoring the temperature and the pressure in the rectifying tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020365797.6U CN212025228U (en) | 2020-03-21 | 2020-03-21 | Cyclohexanol refining system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020365797.6U CN212025228U (en) | 2020-03-21 | 2020-03-21 | Cyclohexanol refining system |
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| Publication Number | Publication Date |
|---|---|
| CN212025228U true CN212025228U (en) | 2020-11-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020365797.6U Active CN212025228U (en) | 2020-03-21 | 2020-03-21 | Cyclohexanol refining system |
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| CN (1) | CN212025228U (en) |
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- 2020-03-21 CN CN202020365797.6U patent/CN212025228U/en active Active
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