CN214781576U - Caprolactam rearrangement heat energy cyclic utilization device - Google Patents
Caprolactam rearrangement heat energy cyclic utilization device Download PDFInfo
- Publication number
- CN214781576U CN214781576U CN202023007249.5U CN202023007249U CN214781576U CN 214781576 U CN214781576 U CN 214781576U CN 202023007249 U CN202023007249 U CN 202023007249U CN 214781576 U CN214781576 U CN 214781576U
- Authority
- CN
- China
- Prior art keywords
- rearrangement
- distillation tower
- benzene distillation
- hot water
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a caprolactam rearrangement heat energy cyclic utilization device, including rearrangement reactor, rearrangement circulating pump, rearrangement cooler, benzene distillation column vacuum pump, benzene distillation column cooler, benzene distillation column condenser, benzene distillation column tail gas condenser and benzene distillation column circulating pump, set gradually first reboiler between the export of benzene distillation column circulating pump and the hot water import of rearrangement cooler, rearrangement hot water tank and rearrangement hot water pump, be provided with the second reboiler between the export of second tower cauldron liquid of benzene distillation column and the second circulation liquid import of benzene distillation column. The utility model has the advantages of simple structure, low energy consumption, safety and environmental protection.
Description
Technical Field
The utility model relates to a caprolactam technical field, concretely relates to caprolactam rearrangement heat energy cyclic utilization device.
Background
Caprolactam is an important organic chemical raw material, is mainly used for producing nylon 6 fibers and nylon 6 engineering plastics, is applied to spinning, tires, food packaging and other industries, and has wide application. Currently, the cyclohexanone oxime liquid phase rearrangement technology is commonly adopted in the industrial production of caprolactam, fuming sulfuric acid is used as a catalyst, the fuming sulfuric acid specification is 104.5 wt%, and the rearrangement reaction is carried out under normal pressure. The cyclohexanone oxime is transformed into caprolactam through a liquid phase rearrangement reaction, the heat release of the rearrangement reaction is 188kJ/mol of cyclohexanone oxime, and simultaneously, the fuming sulfuric acid generates solution heat after entering a rearrangement reactor, so that the total heat actually generated by the rearrangement reaction is 260kJ/mol of cyclohexanone oxime. At present, the heat of rearrangement reaction in a caprolactam production process is removed from a rearrangement reactor through external circulation with a large circulation ratio, the circulation ratio can reach 90-400, the heat of rearrangement reaction is removed through a rearrangement liquid cooler, the refrigerant adopted by the rearrangement liquid cooler is usually circulating water, and the heat of the rearrangement reaction is not considered to be recycled.
The cyclohexanone oxime liquid phase rearrangement device consists of a rearrangement reactor, a rearrangement circulating pump and a rearrangement cooler, and the basic production process comprises the following steps: catalyst fuming sulfuric acid is added from an inlet pipeline of a rearrangement circulating pump, the catalyst fuming sulfuric acid and rearrangement reaction liquid are mixed and diffused into the rearrangement reaction liquid under the high-speed rotation of an impeller of the rearrangement circulating pump, the fuming sulfuric acid is supplemented, the viscosity of the rearrangement reaction liquid is reduced, the rearrangement reaction liquid enters a rearrangement cooler for cooling, reaction heat is removed and then the rearrangement reaction liquid returns to the rearrangement reactor, cooled outer circulation reaction liquid and raw material cyclohexanone oxime are mixed in the rearrangement reactor to complete reaction, most of the reaction liquid enters the rearrangement circulating pump through a bottom outlet of the rearrangement reactor to carry out large-flow circulation cooling and supplement fuming sulfuric acid, and partial heavy liquor flows to a next process through an overflow port of the rearrangement reactor. The rearrangement reaction heat generated by the rearrangement reaction is removed from the rearrangement reactor through the large-flow external circulation reaction liquid to control the rearrangement reaction temperature, and then the large-flow rearrangement reaction liquid exchanges heat with the circulating water in the rearrangement cooler to remove the rearrangement reaction heat.
For example, Chinese patent publication No. CN110711400A discloses a system and a method for producing caprolactam by evaporating caprolactam water solution, wherein a device combining an MVR evaporation unit and an evaporation unit is adopted, a two-effect counter-current pre-evaporation unit is arranged before MVR evaporation, and the caprolactam water solution with the mass concentration of about 30 percent is evaporated to be more than 99.9 percent by adopting the two-effect counter-current pre-evaporation unit, the MVR evaporation unit, the evaporation unit and a heating flash evaporation unit; the two-effect countercurrent pre-evaporation unit pre-evaporates the caprolactam water solution by sequentially utilizing steam of the two-effect rectifying tower and hot water with low grade at 60-90 ℃ in a rearrangement reaction process, so that the process waste heat of the device is recovered to the maximum extent, and the consumption of circulating cooling water is reduced; the MVR evaporation unit realizes the recycling of steam through the mechanical compression of the steam, and reduces the using amount of circulating cooling water. The defects that the MVR technology is adopted to achieve the purpose of reducing the steam consumption, the heat energy of the rearrangement reaction is only partially used for heating the caprolactam water solution, and the heat energy of the rearrangement reaction is not fully utilized.
For example, chinese patent publication No. CN109400532A discloses a method and an apparatus for preparing caprolactam from cyclohexanone oxime. The method comprises the following steps of 1) dissolving cyclohexanone oxime in a batching tank, conveying the mixture to a reactor to contact fuming sulfuric acid, and carrying out adiabatic rearrangement reaction; 2) quickly splitting the phase of the product obtained in the step 1) in a phase splitting tank, feeding the obtained rearrangement product into a curing tank for curing, and feeding the cured rearrangement product into a subsequent caprolactam refining system; 3) and (3) exchanging heat of the oil phase from the phase separation tank through a heat exchanger, then carrying out alkali washing and water washing, partially extracting, refining in a rectifying tank, and feeding the other parts into a batching tank for batching. 4) And after the circulating solvent extracted from the heat exchanger is rectified and separated, the solvent is recycled. The method has the disadvantages that although the volume of the reactor in the rearrangement process is reduced, the heat exchange with large circulation ratio is avoided, and the safety and the efficiency of the system are increased, the full recycling of caprolactam rearrangement heat energy is not considered.
Therefore, how to recycle the rearrangement heat energy of caprolactam so as to obviously reduce energy consumption and production cost is an urgent problem to be solved.
Disclosure of Invention
The to-be-solved problem of the utility model is to above not enough, provide a simple structure, the energy consumption is low, the caprolactam rearrangement heat energy cyclic utilization device of safety ring guarantor.
For solving the above problem, the utility model discloses a technical scheme be: a caprolactam rearrangement heat energy recycling device comprises a rearrangement reactor, a rearrangement circulating pump, a rearrangement cooler, a benzene distillation tower vacuum pump, a benzene distillation tower cooler, a benzene distillation tower condenser, a benzene distillation tower tail gas condenser and a benzene distillation tower circulating pump, wherein a reaction liquid outlet of the rearrangement reactor is connected with an inlet of the rearrangement circulating pump, an outlet of the rearrangement circulating pump is connected with a circulation liquid inlet of the rearrangement cooler, a circulation liquid outlet of the rearrangement cooler is connected with a reaction liquid inlet of the rearrangement reactor, a gas phase outlet of the benzene distillation tower is connected with a gas phase inlet of the benzene distillation tower condenser, a gas phase outlet of the benzene distillation tower condenser is connected with a gas phase inlet of the benzene distillation tower tail gas condenser, and a gas phase outlet of the benzene distillation tower tail gas condenser is connected with an inlet of the benzene distillation tower vacuum pump, condensate outlets of the benzene distillation tower condenser and the benzene distillation tower tail gas condenser are respectively connected with a liquid phase inlet of the benzene distillation tower cooler, a first reboiler, a rearrangement hot water cooler, a rearrangement hot water tank and a rearrangement hot water pump are sequentially arranged between an outlet of the benzene distillation tower circulating pump and a hot water inlet of the rearrangement cooler, a second reboiler is arranged between a second tower kettle liquid outlet of the benzene distillation tower and a second circulating liquid inlet of the benzene distillation tower, a hot water outlet of the rearrangement cooler is connected with a hot water inlet of the first reboiler, a hot water outlet of the first reboiler is connected with a hot water inlet of the rearrangement hot water cooler, a hot water outlet of the rearrangement hot water cooler is connected with a hot water inlet of the rearrangement hot water tank, and a hot water outlet of the rearrangement hot water tank is connected with a hot water inlet of the rearrangement hot water pump, an outlet of the rearrangement hot water pump is connected with a hot water inlet of the rearrangement cooler, a first tower kettle liquid outlet of the benzene distillation tower is connected with an inlet of the benzene distillation tower circulating pump, an outlet of the benzene distillation tower circulating pump is connected with a circulating liquid inlet of the first reboiler, a circulating liquid outlet of the first reboiler is connected with a first circulating liquid inlet of the benzene distillation tower, a second tower kettle liquid outlet of the benzene distillation tower is connected with a circulating liquid inlet of the second reboiler, and a circulating liquid outlet of the second reboiler is connected with a second circulating liquid inlet of the benzene distillation tower.
Preferably, the rectifying section of the benzene distillation tower is a packed tower, and the stripping section is a sieve plate tower.
Preferably, the inner diameter of the benzene distillation tower is 2000-4000 mm.
Preferably, the rearrangement hot water cooler is a plate-and-frame heat exchanger.
Preferably, the benzene distillation tower vacuum pump is a liquid ring vacuum pump.
Preferably, the benzene distillation tower circulating pump is a shield pump.
The utility model discloses a caprolactam rearrangement heat energy cyclic utilization device through optimizing the device, is showing the energy consumption that has reduced the device, has saved the energy, has also reduced caprolactam manufacturing cost simultaneously.
Compared with the prior art, the utility model has the advantages of it is following:
1. rearrangement heat utilization rate is high, the energy consumption is low, the utility model discloses a caprolactam rearrangement heat energy cyclic utilization device sets gradually first reboiler through the export at benzene distillation column circulating pump and the hot water import of rearrangement cooler between, rearrange the hot water pump, rearrange the hot water tank, rearrange the hot water cooler, construct hot water circulating system, thereby introduce benzene distillation system with caprolactam rearrangement heat energy through hot water circulating system, utilize caprolactam rearrangement heat energy to provide the energy for the benzene distillation column, because the heat energy that rearranges heat energy and benzene distillation column consumed is unanimous basically, consequently furthest's recycle caprolactam rearrangement heat energy, the quantity that has simultaneously showing and reducing the circulating water, caprolactam manufacturing cost has been reduced;
2. the reaction process is safe and controllable, the caprolactam rearrangement heat energy recycling device of the utility model is characterized in that a first reboiler is sequentially arranged between the outlet of the benzene distillation tower circulating pump and the hot water inlet of the rearrangement cooler, a rearrangement hot water pump, a rearrangement hot water tank and the rearrangement hot water cooler are used for constructing a hot water circulating system, caprolactam rearrangement heat energy can be removed in time, large circulation ratio heat exchange is avoided, and the safety and the efficiency of the system are improved; meanwhile, the non-condensable gas in the gas phase of the benzene distillation tower is pumped out by a benzene distillation tower vacuum pump to form negative pressure, so that the boiling point of benzene can be effectively reduced, the overall control temperature of the benzene distillation tower is reduced, and the safety and reliability of the benzene distillation process are improved;
3. the rearrangement temperature is controlled stably, the caprolactam product quality is good, the caprolactam rearrangement heat energy recycling device of the utility model uses hot water to control the caprolactam rearrangement reaction temperature circularly, and can effectively control the rearrangement reaction temperature fluctuation, thereby reducing the generation of side reaction, obviously enhancing the reaction stability control capability, ensuring that the rearrangement reaction temperature difference is small, controlling stably, being beneficial to reducing the generation of reaction impurities, and improving the caprolactam product quality;
4. benzene distillation efficiency is high, the utility model discloses a caprolactam rearrangement heat energy cyclic utilization device sets gradually first reboiler through the export of benzene distillation tower circulating pump and rearrangement between the hot water import of cooler, rearrange the hot-water pump, rearrange the hot-water tank, rearrange the hot-water cooler, found hot water circulating system, first reboiler uses hot water as the heat source, and form forced circulation through rearranging the hot-water pump, thereby pass through hot water circulating system with caprolactam rearrangement heat energy and introduce benzene distillation system, utilize caprolactam rearrangement heat energy to improve benzene distillation tower feeding temperature, show and improve benzene distillation efficiency.
Drawings
Fig. 1 is a schematic diagram of the caprolactam rearrangement heat energy recycling device of the utility model.
In the figure, 1 is a rearrangement reactor, 2 is a rearrangement circulating pump, 3 is a rearrangement cooler, 4 is a rearrangement hot water pump, 5 is a rearrangement hot water tank, 6 is a rearrangement hot water cooler, 7 is a benzene distillation tower, 8 is a benzene distillation tower condenser, 9 is a benzene distillation tower cooler, 10 is a benzene distillation tower tail gas condenser, 11 is a benzene distillation tower circulating pump, 12 is a first reboiler, 13 is a second reboiler, and 14 is a benzene distillation tower vacuum pump.
Detailed Description
As shown in the figure, the caprolactam rearrangement heat energy recycling device of the utility model comprises a rearrangement reactor 1, a rearrangement circulating pump 2, a rearrangement cooler 3, a benzene distillation tower 7, a benzene distillation tower vacuum pump 14, a benzene distillation tower cooler 9, a benzene distillation tower condenser 8, a benzene distillation tower tail gas condenser 10 and a benzene distillation tower circulating pump 11, wherein a reaction liquid outlet of the rearrangement reactor 1 is connected with an inlet of the rearrangement circulating pump 2, an outlet of the rearrangement circulating pump 2 is connected with a circulation liquid inlet of the rearrangement cooler 3, a circulation liquid outlet of the rearrangement cooler 3 is connected with a reaction liquid inlet of the rearrangement reactor 1, a gas phase outlet of the benzene distillation tower 7 is connected with a gas phase inlet of the benzene distillation tower condenser 8, a gas phase outlet of the benzene distillation tower condenser 8 is connected with a gas phase inlet of the benzene distillation tower tail gas condenser 10, a gas phase outlet of the benzene distillation tower tail gas condenser 10 is connected with an inlet of the benzene distillation tower vacuum pump 14, a condensate outlet of a benzene distillation tower condenser 8 and a condensate outlet of a benzene distillation tower tail gas condenser 10 are respectively connected with a liquid phase inlet of a benzene distillation tower cooler 9, a first reboiler 12, a rearrangement hot water cooler 6, a rearrangement hot water tank 5 and a rearrangement hot water pump 4 are sequentially arranged between an outlet of a benzene distillation tower circulating pump 11 and a hot water inlet of a rearrangement cooler 3, a second reboiler 13 is arranged between a second tower kettle liquid outlet of the benzene distillation tower 7 and a second circulating liquid inlet of the benzene distillation tower 7, a hot water outlet of the rearrangement cooler 3 is connected with a hot water inlet of the first reboiler 12, a hot water outlet of the first reboiler 12 is connected with a hot water inlet of the rearrangement hot water cooler 6, a hot water outlet of the rearrangement hot water cooler 6 is connected with a hot water inlet of the rearrangement hot water tank 5, a hot water outlet of the rearrangement hot water tank 5 is connected with an inlet of the rearrangement hot water pump 4, an outlet of the hot water pump 4 is connected with a hot water inlet of the rearrangement cooler 3, the outlet of the first tower bottom liquid of the benzene distillation tower 7 is connected with the inlet of a benzene distillation tower circulating pump 11, the outlet of the benzene distillation tower circulating pump 11 is connected with the circulating liquid inlet of a first reboiler 12, the circulating liquid outlet of the first reboiler 12 is connected with the first circulating liquid inlet of the benzene distillation tower 7, the outlet of the second tower bottom liquid of the benzene distillation tower 7 is connected with the circulating liquid inlet of a second reboiler 13, and the circulating liquid outlet of the second reboiler 13 is connected with the second circulating liquid inlet of the benzene distillation tower 7.
The utility model discloses a caprolactam rearrangement heat energy cyclic utilization device work flow does: hot water in the rearrangement hot water tank 5 is sent to the rearrangement cooler 3 through the rearrangement hot water pump 4, heat in rearrangement reaction liquid is replaced in the rearrangement cooler 3 to enable the temperature of the hot water to be increased, the heated high-temperature hot water is sent to the shell pass of the first reboiler 12, the temperature of circulating benzene of the tube pass of the first reboiler 12 is increased by taking the high-temperature hot water as a heat source in the first reboiler 12, the cooled hot water enters the rearrangement hot water cooler 6 after coming out of the shell pass of the first reboiler 12, and the redundant heat is further removed through the rearrangement hot water cooler 6 to obtain low-temperature hot water which enters the rearrangement hot water tank 5, so that hot water circulation of caprolactam rearrangement reaction heat energy recovery is completed.
The miscellaneous benzene enters the benzene distillation tower 7 from the middle part of the benzene distillation tower 7 and is heated by benzene steam rising in the tower, part of vaporized benzene steam enters the benzene distillation tower condenser 8 through the tower top, most of the benzene steam is condensed in the benzene distillation tower condenser 8, uncondensed benzene and noncondensable gas enter the benzene distillation tower tail gas condenser 10 from a gas phase outlet of the benzene distillation tower condenser 8 for further condensation, the noncondensable gas enters the benzene distillation tower vacuum pump 14 from a gas phase outlet of the benzene distillation tower tail gas condenser 10 after the benzene is condensed, the benzene distillation tower vacuum pump 14 pumps the noncondensable gas to perform vacuum pumping operation on the benzene distillation tower 7, and the benzene condensed by the benzene distillation tower condenser 8 and the benzene distillation tower tail gas condenser 10 enters the benzene distillation tower cooler 9 for cooling and recovery. The benzene and the impurities which are not gasified in the benzene distillation tower 7 downwards enter the tower kettle of the benzene distillation tower 7, one part of the benzene and the impurities passes through a first tower kettle liquid outlet of the benzene distillation tower 7 and is sent into a first reboiler 12 through a benzene distillation tower circulating pump 11, and the part of the benzene and the impurities is heated by high-temperature hot water in the first reboiler 12 and then enters the benzene distillation tower 7 again for distillation and separation; the other part of the non-gasified miscellaneous benzene and the impurities enter a second reboiler 13 through a second tower bottom liquid outlet of the benzene distillation tower 7, are heated by steam in the second reboiler 13 and are vaporized and then enter the benzene distillation tower 7 again for distillation and separation.
The present invention is described in further detail below with reference to specific examples, it being understood that the examples described herein are for the purpose of illustration and explanation only and are not intended to be limiting.
Example 1
A caprolactam rearrangement heat energy recycling device comprises a rearrangement reactor 1, a rearrangement circulating pump 2, a rearrangement cooler 3, a benzene distillation tower 7 (phi 2800, a rectifying section is a packed tower, a stripping section is a combined distillation tower of a sieve plate tower), a benzene distillation tower vacuum pump 14 (a liquid ring vacuum pump), a benzene distillation tower cooler 9, a benzene distillation tower condenser 8, a benzene distillation tower tail gas condenser 10 and a benzene distillation tower circulating pump 11 (a shielding pump), wherein a reaction liquid outlet of the rearrangement reactor 1 is connected with an inlet of the rearrangement circulating pump 2, an outlet of the rearrangement circulating pump 2 is connected with a circulation liquid inlet of the rearrangement cooler 3, a circulation liquid outlet of the rearrangement cooler 3 is connected with a reaction liquid inlet of the rearrangement reactor 1, a gas phase outlet of the benzene distillation tower 7 is connected with a gas phase inlet of the benzene distillation tower condenser 8, a gas phase outlet of the benzene distillation tower condenser 8 is connected with a gas phase inlet of the benzene distillation tower tail gas condenser 10, a gas phase outlet of a benzene distillation tower tail gas condenser 10 is connected with an inlet of a benzene distillation tower vacuum pump 14, condensate outlets of a benzene distillation tower condenser 8 and the benzene distillation tower tail gas condenser 10 are respectively connected with a liquid phase inlet of a benzene distillation tower cooler 9, a first reboiler 12, a rearrangement hot water cooler 6 (a plate-frame type heat exchanger), a rearrangement hot water tank 5 and a rearrangement hot water pump 4 are sequentially arranged between an outlet of a benzene distillation tower circulating pump 11 and a hot water inlet of a rearrangement cooler 3, a second reboiler 13 is arranged between a second tower bottom liquid outlet of the benzene distillation tower 7 and a second circulating liquid inlet of the benzene distillation tower 7, a hot water outlet of the rearrangement cooler 3 is connected with a hot water inlet of the first reboiler 12, a hot water outlet of the first reboiler 12 is connected with a hot water inlet of the rearrangement hot water cooler 6, a hot water outlet of the rearrangement hot water cooler 6 is connected with a hot water inlet of the rearrangement hot water tank 5, the hot water outlet of the rearrangement hot water tank 5 is connected with the inlet of the rearrangement hot water pump 4, the outlet of the rearrangement hot water pump 4 is connected with the hot water inlet of the rearrangement cooler 3, the first tower kettle liquid outlet of the benzene distillation tower 7 is connected with the inlet of the benzene distillation tower circulating pump 11, the outlet of the benzene distillation tower circulating pump 11 is connected with the circulating liquid inlet of the first reboiler 12, the circulating liquid outlet of the first reboiler 12 is connected with the first circulating liquid inlet of the benzene distillation tower 7, the second tower kettle liquid outlet of the benzene distillation tower 7 is connected with the circulating liquid inlet of the second reboiler 13, and the circulating liquid outlet of the second reboiler 13 is connected with the second circulating liquid inlet of the benzene distillation tower 7.
Example 2
A caprolactam rearrangement heat energy recycling device comprises a rearrangement reactor 1, a rearrangement circulating pump 2, a rearrangement cooler 3, a benzene distillation tower 7 (phi 3000, a rectifying section is a packed tower, a stripping section is a combined distillation tower of a sieve plate tower), a benzene distillation tower vacuum pump 14 (a liquid ring vacuum pump), a benzene distillation tower cooler 9, a benzene distillation tower condenser 8, a benzene distillation tower tail gas condenser 10 and a benzene distillation tower circulating pump 11 (a shielding pump), wherein a reaction liquid outlet of the rearrangement reactor 1 is connected with an inlet of the rearrangement circulating pump 2, an outlet of the rearrangement circulating pump 2 is connected with a circulation liquid inlet of the rearrangement cooler 3, a circulation liquid outlet of the rearrangement cooler 3 is connected with a reaction liquid inlet of the rearrangement reactor 1, a gas phase outlet of the benzene distillation tower 7 is connected with a gas phase inlet of the benzene distillation tower condenser 8, a gas phase outlet of the benzene distillation tower condenser 8 is connected with a gas phase inlet of the benzene distillation tower tail gas condenser 10, a gas phase outlet of a benzene distillation tower tail gas condenser 10 is connected with an inlet of a benzene distillation tower vacuum pump 14, condensate outlets of a benzene distillation tower condenser 8 and the benzene distillation tower tail gas condenser 10 are respectively connected with a liquid phase inlet of a benzene distillation tower cooler 9, a first reboiler 12, a rearrangement hot water cooler 6 (a plate-frame type heat exchanger), a rearrangement hot water tank 5 and a rearrangement hot water pump 4 are sequentially arranged between an outlet of a benzene distillation tower circulating pump 11 and a hot water inlet of a rearrangement cooler 3, a second reboiler 13 is arranged between a second tower bottom liquid outlet of the benzene distillation tower 7 and a second circulating liquid inlet of the benzene distillation tower 7, a hot water outlet of the rearrangement cooler 3 is connected with a hot water inlet of the first reboiler 12, a hot water outlet of the first reboiler 12 is connected with a hot water inlet of the rearrangement hot water cooler 6, a hot water outlet of the rearrangement hot water cooler 6 is connected with a hot water inlet of the rearrangement hot water tank 5, the hot water outlet of the rearrangement hot water tank 5 is connected with the inlet of the rearrangement hot water pump 4, the outlet of the rearrangement hot water pump 4 is connected with the hot water inlet of the rearrangement cooler 3, the first tower kettle liquid outlet of the benzene distillation tower 7 is connected with the inlet of the benzene distillation tower circulating pump 11, the outlet of the benzene distillation tower circulating pump 11 is connected with the circulating liquid inlet of the first reboiler 12, the circulating liquid outlet of the first reboiler 12 is connected with the first circulating liquid inlet of the benzene distillation tower 7, the second tower kettle liquid outlet of the benzene distillation tower 7 is connected with the circulating liquid inlet of the second reboiler 13, and the circulating liquid outlet of the second reboiler 13 is connected with the second circulating liquid inlet of the benzene distillation tower 7.
Example 3
A caprolactam rearrangement heat energy recycling device comprises a rearrangement reactor 1, a rearrangement circulating pump 2, a rearrangement cooler 3, a benzene distillation tower 7 (phi 3600, a rectifying section is a packed tower, a stripping section is a combined distillation tower of a sieve plate tower), a benzene distillation tower vacuum pump 14 (a liquid ring vacuum pump), a benzene distillation tower cooler 9, a benzene distillation tower condenser 8, a benzene distillation tower tail gas condenser 10 and a benzene distillation tower circulating pump 11 (a shielding pump), wherein a reaction liquid outlet of the rearrangement reactor 1 is connected with an inlet of the rearrangement circulating pump 2, an outlet of the rearrangement circulating pump 2 is connected with a circulation liquid inlet of the rearrangement cooler 3, a circulation liquid outlet of the rearrangement cooler 3 is connected with a reaction liquid inlet of the rearrangement reactor 1, a gas phase outlet of the benzene distillation tower 7 is connected with a gas phase inlet of the benzene distillation tower condenser 8, a gas phase outlet of the benzene distillation tower condenser 8 is connected with a gas phase inlet of the benzene distillation tower tail gas condenser 10, a gas phase outlet of a benzene distillation tower tail gas condenser 10 is connected with an inlet of a benzene distillation tower vacuum pump 14, condensate outlets of a benzene distillation tower condenser 8 and the benzene distillation tower tail gas condenser 10 are respectively connected with a liquid phase inlet of a benzene distillation tower cooler 9, a first reboiler 12, a rearrangement hot water cooler 6 (a plate-frame type heat exchanger), a rearrangement hot water tank 5 and a rearrangement hot water pump 4 are sequentially arranged between an outlet of a benzene distillation tower circulating pump 11 and a hot water inlet of a rearrangement cooler 3, a second reboiler 13 is arranged between a second tower bottom liquid outlet of the benzene distillation tower 7 and a second circulating liquid inlet of the benzene distillation tower 7, a hot water outlet of the rearrangement cooler 3 is connected with a hot water inlet of the first reboiler 12, a hot water outlet of the first reboiler 12 is connected with a hot water inlet of the rearrangement hot water cooler 6, a hot water outlet of the rearrangement hot water cooler 6 is connected with a hot water inlet of the rearrangement hot water tank 5, the hot water outlet of the rearrangement hot water tank 5 is connected with the inlet of the rearrangement hot water pump 4, the outlet of the rearrangement hot water pump 4 is connected with the hot water inlet of the rearrangement cooler 3, the first tower kettle liquid outlet of the benzene distillation tower 7 is connected with the inlet of the benzene distillation tower circulating pump 11, the outlet of the benzene distillation tower circulating pump 11 is connected with the circulating liquid inlet of the first reboiler 12, the circulating liquid outlet of the first reboiler 12 is connected with the first circulating liquid inlet of the benzene distillation tower 7, the second tower kettle liquid outlet of the benzene distillation tower 7 is connected with the circulating liquid inlet of the second reboiler 13, and the circulating liquid outlet of the second reboiler 13 is connected with the second circulating liquid inlet of the benzene distillation tower 7.
Claims (6)
1. A caprolactam rearrangement heat energy recycling device comprises a rearrangement reactor, a rearrangement circulating pump, a rearrangement cooler, a benzene distillation tower vacuum pump, a benzene distillation tower cooler, a benzene distillation tower condenser, a benzene distillation tower tail gas condenser and a benzene distillation tower circulating pump, wherein a reaction liquid outlet of the rearrangement reactor is connected with an inlet of the rearrangement circulating pump, an outlet of the rearrangement circulating pump is connected with a circulation liquid inlet of the rearrangement cooler, a circulation liquid outlet of the rearrangement cooler is connected with a reaction liquid inlet of the rearrangement reactor, a gas phase outlet of the benzene distillation tower is connected with a gas phase inlet of the benzene distillation tower condenser, a gas phase outlet of the benzene distillation tower condenser is connected with a gas phase inlet of the benzene distillation tower tail gas condenser, and a gas phase outlet of the benzene distillation tower tail gas condenser is connected with an inlet of the benzene distillation tower vacuum pump, condensate outlets of the benzene distillation tower condenser and the benzene distillation tower tail gas condenser are respectively connected with a liquid phase inlet of the benzene distillation tower cooler, and the benzene distillation tower tail gas condenser is characterized in that a first reboiler, a rearrangement hot water cooler, a rearrangement hot water tank and a rearrangement hot water pump are sequentially arranged between an outlet of the benzene distillation tower circulating pump and a hot water inlet of the rearrangement cooler, a second reboiler is arranged between a second tower kettle liquid outlet of the benzene distillation tower and a second circulating liquid inlet of the benzene distillation tower, a hot water outlet of the rearrangement cooler is connected with a hot water inlet of the first reboiler, a hot water outlet of the first reboiler is connected with a hot water inlet of the rearrangement hot water cooler, a hot water outlet of the rearrangement hot water cooler is connected with a hot water inlet of the rearrangement hot water tank, and a hot water outlet of the rearrangement hot water tank is connected with an inlet of the hot water rearrangement hot water pump, an outlet of the rearrangement hot water pump is connected with a hot water inlet of the rearrangement cooler, a first tower kettle liquid outlet of the benzene distillation tower is connected with an inlet of the benzene distillation tower circulating pump, an outlet of the benzene distillation tower circulating pump is connected with a circulating liquid inlet of the first reboiler, a circulating liquid outlet of the first reboiler is connected with a first circulating liquid inlet of the benzene distillation tower, a second tower kettle liquid outlet of the benzene distillation tower is connected with a circulating liquid inlet of the second reboiler, and a circulating liquid outlet of the second reboiler is connected with a second circulating liquid inlet of the benzene distillation tower.
2. The caprolactam rearrangement heat energy recycling device of claim 1, wherein the rectifying section of the benzene distillation column is a packed column and the stripping section is a sieve plate column.
3. The caprolactam rearrangement heat energy recycling device of claim 1, wherein the benzene distillation tower has an inner diameter of 2000-4000 mm.
4. The caprolactam rearrangement heat energy recycling device of claim 1, wherein the rearrangement hot water cooler is a plate and frame heat exchanger.
5. The caprolactam rearrangement heat energy recycling device of claim 1, wherein the benzene distillation column vacuum pump is a liquid ring vacuum pump.
6. The caprolactam rearrangement heat energy recycling device of claim 1, wherein the benzene distillation tower circulating pump is a canned pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023007249.5U CN214781576U (en) | 2020-12-15 | 2020-12-15 | Caprolactam rearrangement heat energy cyclic utilization device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023007249.5U CN214781576U (en) | 2020-12-15 | 2020-12-15 | Caprolactam rearrangement heat energy cyclic utilization device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214781576U true CN214781576U (en) | 2021-11-19 |
Family
ID=78711439
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202023007249.5U Active CN214781576U (en) | 2020-12-15 | 2020-12-15 | Caprolactam rearrangement heat energy cyclic utilization device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214781576U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114605323A (en) * | 2022-03-31 | 2022-06-10 | 湖北三宁化工股份有限公司 | Process for separating caprolactam from caprolactam sulfate |
-
2020
- 2020-12-15 CN CN202023007249.5U patent/CN214781576U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114605323A (en) * | 2022-03-31 | 2022-06-10 | 湖北三宁化工股份有限公司 | Process for separating caprolactam from caprolactam sulfate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106588536B (en) | Preparation method and system of cyclohexanone | |
| CN104817481B (en) | Technological method for recovering DMSO from DMSO aqueous solution | |
| CN114031580B (en) | Refining device and refining method for low-energy PBAT byproduct tetrahydrofuran | |
| CN205398514U (en) | Cyclohexanone refining plant in cyclohexanone production process | |
| CN110467595A (en) | A kind of no sulfuric acid process metaformaldehyde synthesizer and its synthesis route | |
| CN214781576U (en) | Caprolactam rearrangement heat energy cyclic utilization device | |
| CN112142618B (en) | Low-concentration dimethylformamide wastewater recovery system and method | |
| CN111233690A (en) | DMAc thermal coupling refining and recycling system and method | |
| CN103524478A (en) | Device and method for shortening ketalation time in ibuprofen synthesis process | |
| CN212102639U (en) | Device for refining cyclohexanone by cyclohexanol dehydrogenation | |
| CN111821821A (en) | Fusel oil recycling device and method in methanol production | |
| CN102887816A (en) | Method for preparing dichloropropanol with chemical reaction-pervaporation coupling method | |
| CN105669367A (en) | Method of raising decomposition yield of cumyl hydroperoxide | |
| CN216808188U (en) | System for improving water quality of dewatering tower of purified terephthalic acid device | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN112920018B (en) | Method for producing mixture of cyclohexanol and cyclohexanone by oxidizing cyclohexane | |
| CN114768278A (en) | Energy-saving efficient DOTP continuous production device and production process thereof | |
| CN205152115U (en) | Cyclohexanone and cyclohexanol separation economizer in cyclohexene method cyclohexanone production process | |
| CN113121314A (en) | Device and method for recycling tertiary butanol by using dividing wall rectifying tower and combining heat pump technology | |
| CN114763318B (en) | Method and device for preparing cyclohexanone from crude cyclohexanol obtained by esterification hydrogenation method | |
| CN110711400A (en) | Energy-saving caprolactam production system and method by evaporating caprolactam water solution | |
| CN114526564B (en) | Method and device for recycling latent heat of acetic acid removal tower of isopropyl acetate device based on heat pump system | |
| CN215712710U (en) | Device for recovering tert-butanol by using dividing wall rectifying tower combined with open or closed heat pump | |
| CN219743939U (en) | Energy-saving tetrahydrofuran aqueous solution rectifying system | |
| CN212594874U (en) | Fusel oil cyclic utilization device in methanol production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |