CN209685643U

CN209685643U - New heat energy utilization system in a kind of cyclohexanol production

Info

Publication number: CN209685643U
Application number: CN201820844575.5U
Authority: CN
Inventors: 李洪震
Original assignee: Individual
Current assignee: Individual
Priority date: 2018-06-01
Filing date: 2018-06-01
Publication date: 2019-11-26
Anticipated expiration: 2028-06-01

Abstract

The utility model discloses heat energy utilization systems new in a kind of cyclohexanol production, including benzene recovery tower heat energy utilization unit, cyclohexene recovery tower heat energy utilization unit, decylization hexene tower heat energy utilization unit and hexamethylene treating column heat energy utilization unit；New heat energy utilization system in the cyclohexanol production of the utility model, it can utilize to greatest extent, process heat in recovery system, reduce Boiler Steam consumption, the usage amount of industrial circulating water is reduced simultaneously, reduce the consumption of recirculated water and the consumption of electric energy, new heat energy utilization system in the cyclohexanol production of the utility model, according to the taste of plant capacity each in cyclohexanol production height, devise reasonable heat recovery approach and heat exchange equipment, it realizes energy-saving to greatest extent, 2.0 ~ 2.5 tons can be reduced using the steam consumption of cyclohexanol per ton after the technique and equipment of the utility model, the dosage of recirculated water reduces by 200 ~ 250 tons, reduce by 350 ~ 425 yuan/ton of production cost.

Description

New heat energy utilization system in a kind of cyclohexanol production

Technical field

The utility model relates to cyclohexanol production technical field, new heat energy utilization in specifically a kind of cyclohexanol production System.

Background technique

The production of cyclohexanol is usually to carry out selective hydrogenation first by benzene, obtains benzene, cyclohexene and hexamethylene Mixture obtains cyclohexene by four tower extracting rectifyings, and then cyclohexene carries out hydration reaction and obtains cyclohexanol；In entire technique It needs to need benzene knockout tower, benzene recovery tower during a series of equipment, such as benzene separation and recovery in the process；Cyclohexene separates back Cyclohexene knockout tower, cyclohexene recovery tower etc. are needed during receiving；Hexamethylene treating column, ring are needed in the subtractive process of hexamethylene Hexane treating column gas phase condenser etc.；Cyclohexanol knockout tower, decylization hexene tower etc. are needed in the subtractive process of cyclohexanol, existing In each technique unit material heating and cooling device, there are the unreasonable problems of more heat utilization, cause heat utilization Rate is low, heat waste, energy consumption are high, and heat needed for each equipment is all by the external world in the production of current entire cyclohexanol What steam provided, the process waste of links is all much to use industrial circulating water, is not carried out links heat Efficient circulation utilizes, and causes the waste of heat and remaining high for production cost, specific:

One, 150 DEG C of benzene recovery tower or so of DMAC kettle liquid, state-of-the-art at present is to be gone out to separate to cyclohexanol by its kettle pumping 80 DEG C of tower or so of kettle liquid is heated, and then goes the charging of heating benzene knockout tower, the also relatively high DMAC of temperature is again through recycling Enter benzene knockout tower cyclic absorption benzene after water is cooling, entire technical process heat utilization efficiency is very low；Two, 150 DEG C of cyclohexene recovery tower The DMAC kettle liquid of left and right, state-of-the-art at present added by the kettle liquid that its kettle pumping goes out to 80 DEG C of cyclohexanol knockout tower or so Then heat goes to heat the material cyclohexene into hydration reactor, temperature or relatively high DMAC are laggard through circulating water again Enter cyclohexene knockout tower cyclic absorption cyclohexene, entire technical process heat utilization efficiency is also relatively low；Three, decylization hexene tower side line is adopted 155 DEG C or so of cyclohexanol gas out is heated directly to the lower cyclohexanol reactor feed heater of temperature and with recycling After water condensation, preheated by cyclohexanol pump extraction to cyclohexanol reactor feed cyclohexene, then send through circulating water to cyclohexanol Intermediate products storage tank, entire technical process heat utilization efficiency are lower；Four, 90 DEG C or so of hexamethylene of hexamethylene treating column top exit Alkane steam directly goes hexamethylene treating column gas phase condenser to be condensed with recirculated water, and more high-grade thermal energy is caused to waste； Five, the kettle liquid of hexamethylene treating column needs to be kept for 85~110 DEG C, and cyclohexanol separation tower bottoms needs to be kept for 80 DEG C or so, hexamethylene The charging cyclohexene of alcohol reactor is also required to external steam and endlessly heats.

Summary of the invention

To solve the above problems, the purpose of the utility model is to provide heat energy utilization systems new in a kind of cyclohexanol production System reduces Boiler Steam consumption to greatest extent using the process heat in recovery system, while reducing making for industrial circulating water Dosage reduces the consumption of recirculated water and the consumption of electric energy.

The utility model to achieve the above object, is achieved through the following technical solutions:

New heat energy utilization system in a kind of cyclohexanol production, including the recycling of benzene recovery tower heat energy utilization unit, cyclohexene Tower heat energy utilization unit, decylization hexene tower heat energy utilization unit and hexamethylene treating column heat energy utilization unit；

Wherein benzene recovery tower heat energy utilization unit includes benzene recovery tower, benzene recycling tower reactor pumps, benzene separation tower bottoms efficiently changes Hot device, the first kettle liquid of hexamethylene treating column high-performance heat exchanger, the first kettle liquid of cyclohexanol knockout tower high-performance heat exchanger, benzene knockout tower into Expect heater, benzene knockout tower extractant cooler, benzene knockout tower, benzene separation tower reactor pump；

Cyclohexene recovery tower heat energy utilization unit includes cyclohexene recovery tower, cyclohexene recycling tower reactor pump, cyclohexene separation Tower bottoms high-performance heat exchanger, the second kettle liquid of hexamethylene treating column high-performance heat exchanger, cyclohexanol knockout tower the second kettle liquid high efficient heat exchanging Device, cyclohexanol reactor feed high-performance heat exchanger, cyclohexene knockout tower extractant cooler and cyclohexene knockout tower, cyclohexene point It is pumped from tower reactor；

Decylization hexene tower heat energy utilization unit includes that decylization hexene tower, cyclohexanol separation tower bottoms evaporator, cyclohexanol are anti- Answer device third feed heater, cyclohexanol condenser, cyclohexanol pump, the first feed heater of cyclohexanol reactor, cyclohexanol cold But device, cyclohexanol intermediate products tank, the second feed heater of cyclohexanol reactor, decylization hexene tower feed cooler, decylization oneself Alkene tower feed surge tank；

Hexamethylene treating column heat energy utilization unit includes hexamethylene treating column, cyclohexanol knockout tower charging high efficient heat recovery Device, hexamethylene treating column gas phase condenser, hexamethylene treating column return tank and cyclohexanol knockout tower；

Tower reactor pump and benzene knockout tower are recycled by benzene in the outlet of benzene recovery tower bottoms material in benzene recovery tower heat energy utilization unit The shell-side inlet of kettle liquid high-performance heat exchanger connects, and benzene separates the shell-side outlet and hexamethylene treating column the of tower bottoms high-performance heat exchanger The shell-side inlet of one kettle liquid high-performance heat exchanger is connected by pipeline, and the shell-side of hexamethylene treating column the first kettle liquid high-performance heat exchanger goes out Mouth is connect with the shell-side inlet of cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger by pipeline, the first kettle liquid of cyclohexanol knockout tower The shell-side outlet of high-performance heat exchanger is connect with benzene knockout tower feed heater heating medium inlet by pipeline, the charging of benzene knockout tower Heater Crude product input is connect with the shell-side inlet of benzene knockout tower extractant cooler by pipeline, benzene knockout tower extractant The shell-side outlet of cooler is connect with benzene knockout tower extractant entrance by pipeline, and benzene knockout tower outlet at bottom passes through benzene knockout tower Kettle pump is connect with the material inlet of benzene recovery tower；

Tower reactor is recycled by cyclohexene in the outlet of cyclohexene recovery tower bottoms material in cyclohexene recovery tower heat energy utilization unit The shell-side of the shell-side inlet of pump connection cyclohexene knockout tower kettle liquid high-performance heat exchanger, cyclohexene separation tower bottoms high-performance heat exchanger goes out Mouth connects the shell-side inlet of the second kettle liquid of hexamethylene treating column high-performance heat exchanger by pipeline, and the second kettle liquid of hexamethylene treating column is high The shell-side outlet for imitating heat exchanger connects the shell-side inlet of the second kettle liquid of cyclohexanol knockout tower high-performance heat exchanger, cyclohexanol by pipeline The shell-side outlet of knockout tower the second kettle liquid high-performance heat exchanger connects the shell of cyclohexanol reactor feed high-performance heat exchanger by pipeline The shell-side outlet of side entrance, cyclohexanol reactor feed high-performance heat exchanger connects the cooling of cyclohexene knockout tower extractant by pipeline The shell-side inlet of device, the shell-side outlet of cyclohexene knockout tower extractant cooler connect the extraction of cyclohexene knockout tower by pipeline The outlet at bottom of agent entrance, cyclohexene knockout tower separates tower reactor pump connection cyclohexene recovery tower material inlet by cyclohexene；

The side take-off mouth of decylization hexene tower connects cyclohexanol separation by pipeline in decylization hexene tower heat energy utilization unit The heating medium inlet of tower bottoms evaporator, the Crude product input that cyclohexanol separates tower bottoms evaporator pass through pipeline connection ring The pipe side outlet of the pipe side entrance of hexanol reactor third feed heater, cyclohexanol reactor third feed heater passes through ring The shell-side inlet of hexanol pump connection the first feed heater of cyclohexanol reactor, the shell of the first feed heater of cyclohexanol reactor Side outlet is connect by pipeline with the shell-side inlet of cyclohexanol cooler, among the shell-side outlet and cyclohexanol of cyclohexanol cooler Products pot is connected by pipeline；Cyclohexanol condenser is connected in parallel with cyclohexanol reactor third feed heater；Cyclohexanol point Gaseous phase outlet from tower bottoms evaporator is connect by pipeline with the pipe side entrance of the second feed heater of cyclohexanol reactor, ring The pipe side outlet of the second feed heater of hexanol reactor is connect by pipeline with decylization hexene tower feed surge tank, decylization hexene Tower feed cooler is connected in parallel with the second feed heater of cyclohexanol reactor；

Hexamethylene treating column heat energy utilization unit cyclohexane treating column top gas phase outlet with cyclohexanol knockout tower into Expect high efficient heat recovery device shell-side inlet connection, cyclohexanol knockout tower feed high efficient heat recovery device shell-side lower end outlet with The entrance of hexamethylene treating column gas phase condenser connects, and the liquid-phase outlet and hexamethylene of hexamethylene treating column gas phase condenser refine The connection of tower return tank, liquid-phase outlet that cyclohexanol knockout tower feeds high efficient heat recovery device and top gas phase outlet are and cyclohexanol Knockout tower connection；

Hexamethylene treating column the first kettle liquid high-performance heat exchanger and the second kettle liquid high-performance heat exchanger parallel connection of hexamethylene treating column connect It connects；Cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger and cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger are connected in parallel.

Preferably, cyclohexanol knockout tower feeds high efficient heat recovery device, including gas-liquid separator and heat exchanger, gas-liquid separation Device is connected by the first connecting pipe with the second connecting pipe with heat exchanger；The gas-liquid separator top position offers gas Body outlet, for gas to be passed through cyclohexanol knockout tower after gas-liquid separation；The side of gas-liquid separator opens up material inlet, uses It is fed in receiving cyclohexanol knockout tower；Liquidometer is installed on the downside of the material inlet, the upper end of the liquidometer passes through Liquidometer upper orifice is communicated with gas-liquid separator, and the lower end of liquidometer is communicated by liquidometer lower nozzle with gas-liquid separator, institute State liquidometer can real-time display go out the liquid level of material in gas-liquid separator；The side of the gas-liquid separator bottom position opens up object Material exports, and installs control valve after material outlet, can control the flow of material outflow gas-liquid separator, the liquids after gas-liquid separation Material is passed through in cyclohexanol knockout tower via material outlet；Liquid outlet, liquid are equipped at the gas-liquid separator bottom centre position Body outlet is communicated with the first connecting pipe；The gas-liquid separator inner upper installs wire mesh demister, and wire mesh demister is used for Remove the mist carried secretly in separation gas；Gas-liquid separator lower inside installs anti-swirl baffle, and anti-swirl baffle is located at liquid Outlet top；

The other end of first connecting pipe connects liquid-inlet, and liquid-inlet is located at the bottom of heat exchanger；It is described to change Hot device includes several efficient heat-exchanging pipes of heat exchanger shell and internal setting, installs two tube sheets up and down inside the heat exchanger, Heat exchanger is divided into three chambers by two tube sheets, and upper and lower two chambers are connected by efficient heat-exchanging pipe, and intermediate cavity is for efficiently changing The heat exchange of heat pipe and heat gas is equipped with heat gas import in the side on heat exchanger shell top, another in heat exchanger shell The lower part of side is exported equipped with heat gas, process steam of the heat gas from hexamethylene treating column, from heat gas Import enters inside heat exchanger, and heated gas vent is passed through hexamethylene treating column gas again after exchanging heat with efficient heat-exchanging pipe In phase condenser；It offers exhaust outlet at heat exchanger shell upper position, under abnormal operating state, opens exhaust outlet and be used for Heat exchanger shell inner part inert gas is discharged, the heat-transfer effect for influencing heat exchanger is prevented；In heat exchanger shell lower position It offers and leads leaching mouth, for discharging the hydrops in heat exchanger when parking；

When the charging high efficient heat recovery device running of cyclohexanol knockout tower, the charging of cyclohexanol knockout tower is entered by material inlet Into gas-liquid separator, separated gas is after wire mesh demister removes the mist of deentrainment by gas in gas-liquid separator Outlet is passed through in cyclohexanol knockout tower, and gas-liquid separator materials inside enters heat exchange by liquid outlet and the first connecting pipe In device, after the process steam of efficient heat-exchanging pipe and the discharge of hexamethylene treating column in the heat exchanger carries out heat exchange, then by Second connecting pipe flows back in gas-liquid separator；In circulation certain time, after temperature, liquid level reach requirement, material passes through outlet, Continuously by control valve control be sent into cyclohexanol knockout tower in, meanwhile, cyclohexanol knockout tower charging also continuously through material into Mouth enters gas-liquid separator；The aperture of adjusting control valve keeps the material liquid surface in gas-liquid separator to be in liquidometer upper orifice Between liquidometer lower nozzle position.

Preferably, the first feed heater of cyclohexanol reactor, the second feed heater of cyclohexanol reactor and cyclohexanol Reactor third feed heater is connected in series.

The utility model further includes heat energy utilization method new in a kind of cyclohexanol production, comprising the following steps:

Gone out 1. the benzene that temperature is 140~155 DEG C recycles tower bottoms DMAC by benzene recycling tower reactor pumping, initially enters benzene separation Tower bottoms high-performance heat exchanger exchanges heat to 120~135 DEG C of benzene knockout tower of kettle liquid, and DMAC temperature is reduced to 125~140 DEG C, Next goes hexamethylene treating column the first kettle liquid high-performance heat exchanger to exchange heat 85~110 DEG C of hexamethylene purification tower bottoms, will DMAC temperature is reduced to 105~115 DEG C, subsequently into cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger to 75~85 DEG C of hexamethylene Alcohol separation tower bottoms exchange heat, DMAC temperature is reduced to 85~95 DEG C, subsequently into benzene knockout tower feed heater to feed into Row heating, is increased to 60~75 DEG C or so by 35~45 DEG C for feeding temperature, DMAC temperature is reduced to 70~75 DEG C, then separates through benzene Tower extractant cooler enters benzene knockout tower after DMAC temperature is cooled to 60~66 DEG C and carries out cycling extraction benzene, then separates through benzene Tower reactor pumping goes out to be sent to benzene recovery tower and carries out multi-cycle separation recycling benzene；

Go out 2. the cyclohexene recovery tower DMAC that temperature is 140~155 DEG C recycles tower reactor pumping by cyclohexene, initially enters ring Hexene separation tower bottoms high-performance heat exchanger exchanges heat to 120~135 DEG C of cyclohexene knockout tower of kettle liquid, and DMAC temperature is reduced to 125~140 DEG C, next goes hexamethylene treating column the second kettle liquid high-performance heat exchanger to refine tower bottoms to 85~110 DEG C of hexamethylene It exchanges heat, DMAC temperature is reduced to 105~115 DEG C, subsequently into cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger to 75 ~85 DEG C of cyclohexanol separation tower bottoms exchanges heat, and DMAC temperature is reduced to 85~95 DEG C, then enters back into cyclohexanol reactor Charging high-performance heat exchanger exchanges heat to charging cyclohexene, cyclohexene temperature is increased to 65~70 DEG C by 35~50 DEG C, DMAC Temperature is reduced to 75~80 DEG C, then enters ring after DMAC temperature is cooled to 70~75 DEG C by cyclohexene knockout tower extractant cooler Hexene knockout tower top carries out extraction cyclohexene, then goes out to be sent to cyclohexene recovery tower through cyclohexene separation tower reactor pumping and be recycled Separate and recover cyclohexene；

3. 150~160 DEG C of cyclohexanol gas of decylization hexene tower side take-off goes cyclohexanol knockout tower kettle liquid to steam first Device is sent out, 75~85 DEG C of the kettle liquid come to cyclohexanol separation tower reactor pumping carries out heating evaporation, and temperature is 135-145 after cooling DEG C cyclohexanol gas-liquid mixture enters cyclohexanol reactor third feed heater, adds to the cyclohexene into hydration reactor Cyclohexene temperature is increased to 115-125 DEG C by 100~110 DEG C or so by heat, and cyclohexanol gas-liquid mixture is cooled to 115~120 DEG C, the cyclohexanol condenser auxiliary in parallel with cyclohexanol reactor third feed heater is cold by the cyclohexanol gas of side take-off Solidifying, temperature is that 110~120 DEG C of cyclohexanol are pumped out by cyclohexanol after condensation, through the first feed heater pair of cyclohexanol reactor Cyclohexene heating, is increased to 75~85 DEG C by 65~70 DEG C for cyclohexene temperature, the temperature of cyclohexanol is reduced to 90~95 DEG C, so Enter cyclohexanol intermediate products tank after cooling down by cyclohexanol cooler；

The temperature that steams of cyclohexanol separation tower bottoms evaporator be 125~135 DEG C of cyclohexanol and cyclohexene mixed gas into Enter the second feed heater of cyclohexanol reactor, the cyclohexene into hydration reactor is heated, by cyclohexene temperature by 75 ~85 DEG C are increased to 100~110 DEG C, the decylization hexene tower feed cooler in parallel with the second feed heater of cyclohexanol reactor Auxiliary is by cyclohexanol and cyclohexene Mixed Gas Condensation to 90~96 DEG C；

4. the hexamethylene gas phase steam of 80~95 DEG C of hexamethylene treating column top exit is introduced into the charging of cyclohexanol knockout tower Temperature is reduced to 75~86 DEG C after high efficient heat recovery device feeds progress heating recovery heat to cyclohexanol knockout tower, then decyclization Hexane treating column gas phase condenser is condensed, and condensed liquid phase flows into hexamethylene treating column return tank, on-condensible gas reducing internal heat Torch；The temperature of cyclohexanol knockout tower charging is increased to 58~65 DEG C by 55~60 DEG C, and then air-liquid enters cyclohexanol knockout tower.

Preferably, the benzene that temperature is 150 DEG C recycles tower bottoms DMAC and is gone out by benzene recycling tower reactor pumping, initially enters benzene separation Tower bottoms high-performance heat exchanger exchanges heat to 130 DEG C of benzene knockout tower of kettle liquid, DMAC temperature is reduced to 130 DEG C, next removes hexamethylene Alkane treating column the first kettle liquid high-performance heat exchanger exchanges heat to 90 DEG C of hexamethylene purification tower bottoms, and DMAC temperature is reduced to 110 DEG C, the cyclohexanol separation tower bottoms subsequently into cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger to 78 DEG C exchanges heat, DMAC temperature is reduced to 80 DEG C, heats subsequently into benzene knockout tower feed heater to charging, and feeding temperature is risen by 40 DEG C Up to 65 DEG C or so, DMAC temperature is reduced to 72 DEG C, then after DMAC temperature is cooled to 63 DEG C by benzene knockout tower extractant cooler Cycling extraction benzene is carried out into benzene knockout tower, then goes out to be sent to benzene recovery tower through benzene separation tower reactor pumping and carries out multi-cycle separation recycling Benzene.

Preferably, the cyclohexene recovery tower DMAC that temperature is 150 DEG C recycles tower reactor pumping by cyclohexene and goes out, and initially enters ring Hexene separation tower bottoms high-performance heat exchanger exchanges heat to 130 DEG C of cyclohexene knockout tower of kettle liquid, and DMAC temperature is reduced to 130 DEG C, next goes hexamethylene treating column the second kettle liquid high-performance heat exchanger to exchange heat 100 DEG C of hexamethylene purification tower bottoms, will DMAC temperature is reduced to 110 DEG C, subsequently into cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger to 80 DEG C of cyclohexanol knockout tower Kettle liquid exchanges heat, and DMAC temperature is reduced to 90 DEG C, then enters back into cyclohexanol reactor feed high-performance heat exchanger to charging hexamethylene Alkene exchanges heat, and cyclohexene temperature is increased to 68 DEG C by 40 DEG C, DMAC temperature is reduced to 78 DEG C, then extracts through cyclohexene knockout tower Agent cooler enters cyclohexene knockout tower top and carries out extraction cyclohexene after DMAC temperature is cooled to 72 DEG C, then through cyclohexene point Go out to be sent to cyclohexene recovery tower from tower reactor pumping and carries out multi-cycle separation recycling cyclohexene.

Preferably, 155 DEG C of cyclohexanol gas of decylization hexene tower side take-off goes cyclohexanol knockout tower kettle liquid to steam first Device is sent out, 78 DEG C of the kettle liquid come to cyclohexanol separation tower reactor pumping carries out heating evaporation, and temperature is 140 DEG C of cyclohexanol after cooling Gas-liquid mixture enters cyclohexanol reactor third feed heater, heats to the cyclohexene into hydration reactor, by ring Hexene temperature is increased to 120 DEG C by 110 DEG C, and cyclohexanol gas-liquid mixture is cooled to 118 DEG C, feeds with cyclohexanol reactor third The cyclohexanol condenser auxiliary of heater parallel connection condenses the cyclohexanol gas of side take-off, and temperature is 115 DEG C of hexamethylenes after condensation Alcohol is pumped out by cyclohexanol, is heated through the first feed heater of cyclohexanol reactor to cyclohexene, by cyclohexene temperature by 68 DEG C 75 DEG C are increased to, the temperature of cyclohexanol is reduced to 92 DEG C, then enters cyclohexanol intermediate products after cyclohexanol cooler is cooling Tank；

The temperature that cyclohexanol separation tower bottoms evaporator steams is that 130 DEG C of cyclohexanol and cyclohexene mixed gas enter hexamethylene The second feed heater of alcohol reactor, heats the cyclohexene into hydration reactor, and cyclohexene temperature is increased by 75 DEG C To 105 DEG C, decylization hexene tower feed cooler auxiliary in parallel with the second feed heater of cyclohexanol reactor by cyclohexanol and Cyclohexene Mixed Gas Condensation is to 92 DEG C.

Preferably, 88 DEG C of hexamethylene treating column top exit of hexamethylene gas phase steam, be introduced into cyclohexanol knockout tower into Temperature is reduced to 78 DEG C after material high efficient heat recovery device feeds progress heating recovery heat to cyclohexanol knockout tower, then removes hexamethylene Alkane treating column gas phase condenser is condensed, and condensed liquid phase flows into hexamethylene treating column return tank, and on-condensible gas removes torch； The temperature of cyclohexanol knockout tower charging is increased to 63 DEG C by 58 DEG C, and then air-liquid enters cyclohexanol knockout tower.

The utility model has the advantage that compared with prior art

New heat energy utilization system and heat energy utilization method in the cyclohexanol production of the utility model, can be maximum Using the process heat in recovery system, Boiler Steam consumption is reduced, while reducing the usage amount of industrial circulating water, reduces circulation The consumption of water and the consumption of electric energy, specific:

Benzene recovery tower heat energy utilization unit, by the way that benzene to be recycled to 150 DEG C or so of DMAC solution of tower bottom successively to 130 DEG C or so benzene separation tower bottoms, 100 DEG C or so hexamethylene purification tower bottoms, 80 DEG C or so cyclohexanol separation tower bottoms, 40 DEG C or so of benzene knockout tower charging exchanges heat, and benzene knockout tower cycling extraction benzene is then entered after circulating water.Pass through The operation of benzene recovery tower heat energy utilization unit heated above-mentioned process stream and DMAC solution temperature be gradually reduced to 70 DEG C Left and right.On the one hand the stable operation for having ensured this cell process, reduces the dosage of Boiler Steam, reduces steam consumption, separately On the one hand the dosage for reducing cooling benzene knockout tower extractant recirculated water simultaneously again, realizes the maximum reasonable benefit of energy With with it is energy-saving；

Cyclohexene recovery tower heat energy utilization unit, by by 150 DEG C or so of DMAC solution of cyclohexene recovery tower successively Cyclohexene separation tower bottoms, 100 DEG C or so of hexamethylene purification tower bottoms, 80 DEG C or so of cyclohexanol point to 130 DEG C or so It exchanges heat from tower bottoms, 40 DEG C or so of cyclohexanol reactor feed cyclohexene, hexamethylene is then entered after circulating water Alkene knockout tower cycling extraction cyclohexene.By the operation of cyclohexene recovery tower heat energy utilization unit, that is, it heated this cell process DMAC solution temperature is gradually reduced to 75 DEG C or so again by material.Reach i.e. reduction steam consumption, and reduces recirculated water simultaneously The purpose of dosage realizes energy-saving to the greatest extent；

Decylization hexene tower heat energy utilization unit separates tower reactor to cyclohexanol with the higher cyclohexanol gas phase steam of temperature first Liquid carries out heating evaporation, on the one hand heats cyclohexene with by the cyclohexanol gas-liquid after cyclohexanol separation tower bottoms evaporator, and And cyclohexanol condenser in parallel ensures the condensation effect of cyclohexanol gas phase, it is lower that the cyclohexanol of condensation is then continued heating temperature Cyclohexene, most afterwards after circulating water enter cyclohexanol intermediate products tank；On the other hand, it is steamed with cyclohexanol separation tower bottoms The cyclohexene and cyclohexanol steam of sending again heat cyclohexanol reactor feed cyclohexene, and decylization hexene tower in parallel Feed cooler ensures that condensation effect, condensed liquid flow into decylization hexene tower feed surge tank.Pass through above-mentioned new decylization The operation of hexene tower heat energy utilization unit realizes the Multi-class propagation of decylization hexene tower side take-off high-temperature steam heat, improves The utilization efficiency of process waste；

Hexamethylene treating column heat energy utilization unit feeds high efficient heat recovery device to cyclohexanol point by cyclohexanol knockout tower Heating from tower charging takes full advantage of the heat of the hexamethylene steam flowed out at the top of hexamethylene treating column, reduce steam and The dosage of the recirculated water of condenser realizes the efficient utilization of process heat.

New heat energy utilization system in cyclohexanol production of the invention, according to the product of plant capacity each in cyclohexanol production Taste height, devise reasonable heat recovery approach and heat exchange equipment, realize to greatest extent it is energy-saving, using the present invention Technique and equipment after the steam consumption of cyclohexanol per ton can reduce by 2.0~2.5 tons, the dosage of recirculated water reduces by 200~250 Ton reduces by 320~400 yuan/ton of production cost.

Detailed description of the invention

Fig. 1 is the process flow diagram of benzene recovery tower heat energy utilization unit；

Fig. 2 is the process flow diagram of cyclohexene recovery tower heat energy utilization unit；

Fig. 3 is the process flow diagram of decylization hexene tower heat energy utilization unit；

Fig. 4 is the process flow diagram of hexamethylene treating column heat energy utilization unit

Fig. 5 is the structural schematic diagram that cyclohexanol knockout tower feeds high efficient heat recovery device；

Appended drawing reference: 1 gas-liquid separator, 2 heat exchanger, 3 first 4 second connecting pipe of connecting pipe, 5 gas vent, 6 material into 12 liquid outlet of mouth 7 liquidometer, 8 liquidometer upper orifice, 9 liquidometer lower nozzle, 10 material outlet, 11 control valve, 13 wire mesh demister 14 18 heat gas import of anti-swirl baffle 15 liquid-inlet, 16 heat exchanger shell, 17 efficient heat-exchanging pipe, 19 heat gas exports 20 rows Port 21 leads leaching 22 material liquid surface of mouth, 23 tube sheet.

Specific embodiment

The benzene of the utility model separates tower bottoms high-performance heat exchanger, the first kettle liquid of hexamethylene treating column high-performance heat exchanger, ring The first kettle liquid of hexanol knockout tower high-performance heat exchanger, benzene knockout tower feed heater, cyclohexene separate tower bottoms high-performance heat exchanger, ring The second kettle liquid of hexane treating column high-performance heat exchanger, the second kettle liquid of cyclohexanol knockout tower high-performance heat exchanger, cyclohexanol reactor feed High-performance heat exchanger is conventional in the market shell-and-tube heat exchanger or plate heat exchanger etc.；

Wherein benzene separation tower bottoms high-performance heat exchanger is high to the heat exchange of benzene separation tower bottoms, the first kettle liquid of hexamethylene treating column It imitates heat exchanger and separates tower reactor to cyclohexanol to the heat exchange of hexamethylene purification tower bottoms, cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger Liquid heat exchange, benzene knockout tower feed heater are to benzene knockout tower charging heat exchange, cyclohexene separation tower bottoms high-performance heat exchanger to hexamethylene Alkene separates tower bottoms heat exchange, hexamethylene treating column the second kettle liquid high-performance heat exchanger to the heat exchange of hexamethylene purification tower bottoms, cyclohexanol Knockout tower the second kettle liquid high-performance heat exchanger is to the heat exchange of cyclohexanol separation tower bottoms, cyclohexanol reactor feed high-performance heat exchanger to ring Hexanol reactor feed heat exchange；

Cyclohexanol reactor third feed heater, the first feed heater of cyclohexanol reactor, cyclohexanol reactor Two feed heaters are heater conventional in the market；

It is evaporator conventional in the market that cyclohexanol, which separates tower bottoms evaporator,；

Cyclohexanol condenser and hexamethylene treating column gas phase condenser are condenser conventional in the market；

Cyclohexanol cooler, decylization hexene tower feed cooler, benzene knockout tower extractant cooler and cyclohexene knockout tower Extractant cooler is cooler conventional in the market；Since benzene knockout tower extractant and cyclohexene knockout tower extractant are DMAC solution, so namely to cool down DMAC molten for benzene knockout tower extractant cooler and cyclohexene knockout tower extractant cooler The cooler of liquid.

The conventional thermal energy recoverer containing gas-liquid separator and heat exchanger can be used as the charging of cyclohexanol knockout tower in the market High efficient heat recovery device for realizing industrial exhaust heat steam to the heat exchange function of material, and has saved industrial exhaust heat.

Decylization hexene tower is the rectifying column that can remove the cyclohexene in cyclohexanol, usually plate distillation column.

For it is not described above to equipment be device existing equipment common in the market.

Below in conjunction with specific embodiment, the utility model will be further described.

Embodiment 1

New heat energy utilization system in a kind of cyclohexanol production, including benzene recovery tower heat energy utilization unit (as shown in Figure 1), Cyclohexene recovery tower heat energy utilization unit (as shown in Figure 2), decylization hexene tower heat energy utilization unit (as shown in Figure 3) and hexamethylene Treating column heat energy utilization unit (as shown in Figure 4)；

Hexamethylene treating column heat energy utilization unit cyclohexane treating column top gas phase outlet with cyclohexanol knockout tower into Expect high efficient heat recovery device shell-side inlet connection, cyclohexanol knockout tower feed high efficient heat recovery device shell-side lower end outlet with The entrance of hexamethylene treating column gas phase condenser connects, and the outlet of hexamethylene treating column gas phase condenser and hexamethylene treating column return Tank connection is flowed, the liquid-phase outlet of cyclohexanol knockout tower charging high efficient heat recovery device and top gas phase outlet are separated with cyclohexanol Tower connection；

Embodiment 2

New heat energy utilization method in a kind of cyclohexanol production, technological process apparatus connection relationship with embodiment 1, including with Lower step:

Gone out 1. the benzene that temperature is 140 DEG C recycles tower bottoms DMAC by benzene recycling tower reactor pumping, initially enters benzene separation tower reactor Liquid high-performance heat exchanger exchanges heat to 120 DEG C of benzene knockout tower of kettle liquid, and DMAC temperature is reduced to 125 DEG C, next goes hexamethylene smart Tower the first kettle liquid high-performance heat exchanger processed exchanges heat to 85 DEG C of hexamethylene purification tower bottoms, DMAC temperature is reduced to 105 DEG C, so The cyclohexanol separation tower bottoms for entering cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger afterwards to 75 DEG C exchanges heat, DMAC temperature 85 DEG C are reduced to, charging is heated subsequently into benzene knockout tower feed heater, feeding temperature is increased to 60 DEG C by 35 DEG C Left and right, DMAC temperature are reduced to 70 DEG C, then into benzene point after DMAC temperature is cooled to 60 DEG C by benzene knockout tower extractant cooler Cycling extraction benzene is carried out from tower, then goes out to be sent to benzene recovery tower through benzene separation tower reactor pumping and carries out multi-cycle separation recycling benzene；

Go out 2. the cyclohexene recovery tower DMAC that temperature is 140 DEG C recycles tower reactor pumping by cyclohexene, initially enters cyclohexene Separation tower bottoms high-performance heat exchanger exchanges heat to 120 DEG C of cyclohexene knockout tower of kettle liquid, and DMAC temperature is reduced to 125 DEG C, It is secondary that hexamethylene treating column the second kettle liquid high-performance heat exchanger is gone to exchange heat 85 DEG C of hexamethylene purification tower bottoms, by DMAC temperature 105 DEG C are reduced to, the cyclohexanol separation tower bottoms subsequently into cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger to 75 DEG C carries out Heat exchange, DMAC temperature are reduced to 85 DEG C, then enter back into cyclohexanol reactor feed high-performance heat exchanger and change charging cyclohexene Cyclohexene temperature is increased to 65 DEG C by 35 DEG C by heat, and DMAC temperature is reduced to 75 DEG C, then through cyclohexene knockout tower extractant cooler Enter cyclohexene knockout tower top after DMAC temperature is cooled to 70 DEG C and carry out extraction cyclohexene, then through cyclohexene separation tower reactor pump Extraction is sent to cyclohexene recovery tower and carries out multi-cycle separation recycling cyclohexene；

3. 150 DEG C of cyclohexanol gas of decylization hexene tower side take-off removes cyclohexanol knockout tower kettle liquid evaporator first, 75 DEG C of the kettle liquid come to cyclohexanol separation tower reactor pumping carries out heating evaporation, and temperature is 135 DEG C of cyclohexanol gas-liquids after cooling Mixture enters cyclohexanol reactor third feed heater, heats to the cyclohexene into hydration reactor, by cyclohexene Temperature is increased to 115 DEG C by 100 DEG C or so, and cyclohexanol gas-liquid mixture is cooled to 115 DEG C, feeds with cyclohexanol reactor third The cyclohexanol condenser auxiliary of heater parallel connection condenses the cyclohexanol gas of side take-off, and temperature is 110 DEG C of hexamethylenes after condensation Alcohol is pumped out by cyclohexanol, is heated through the first feed heater of cyclohexanol reactor to cyclohexene, by cyclohexene temperature by 65 DEG C 75 DEG C are increased to, the temperature of cyclohexanol is reduced to 90 DEG C, then enters cyclohexanol intermediate products after cyclohexanol cooler is cooling Tank；

The temperature that cyclohexanol separation tower bottoms evaporator steams is that 125 DEG C of cyclohexanol and cyclohexene mixed gas enter hexamethylene The second feed heater of alcohol reactor, heats the cyclohexene into hydration reactor, and cyclohexene temperature is increased by 75 DEG C To 100 DEG C, decylization hexene tower feed cooler auxiliary in parallel with the second feed heater of cyclohexanol reactor by cyclohexanol and Cyclohexene Mixed Gas Condensation is to 90 DEG C；

4. it is efficient to be introduced into the charging of cyclohexanol knockout tower for the hexamethylene gas phase steam of 80 DEG C of hexamethylene treating column top exit Temperature is reduced to 75 DEG C after thermal energy recoverer feeds progress heating recovery heat to cyclohexanol knockout tower, and hexamethylene is then gone to refine Tower gas phase condenser is condensed, and condensed liquid phase flows into hexamethylene treating column return tank, and on-condensible gas removes torch；Cyclohexanol The temperature of knockout tower charging is increased to 58 DEG C by 55 DEG C, and then air-liquid enters cyclohexanol knockout tower.

Embodiment 3

Gone out 1. the benzene that temperature is 155 DEG C recycles tower bottoms DMAC by benzene recycling tower reactor pumping, initially enters benzene separation tower reactor Liquid high-performance heat exchanger exchanges heat to 135 DEG C of benzene knockout tower of kettle liquid, and DMAC temperature is reduced to 140 DEG C, next goes hexamethylene smart Tower the first kettle liquid high-performance heat exchanger processed exchanges heat to 110 DEG C of hexamethylene purification tower bottoms, and DMAC temperature is reduced to 115 DEG C, Cyclohexanol separation tower bottoms subsequently into cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger to 85 DEG C exchanges heat, DMAC temperature Degree is reduced to 95 DEG C, heats subsequently into benzene knockout tower feed heater to charging, feeding temperature is increased to 75 by 45 DEG C DEG C or so, DMAC temperature is reduced to 75 DEG C, then enters benzene after DMAC temperature is cooled to 66 DEG C by benzene knockout tower extractant cooler Knockout tower carries out cycling extraction benzene, then goes out to be sent to benzene recovery tower through benzene separation tower reactor pumping and carry out multi-cycle separation recycling benzene；

Go out 2. the cyclohexene recovery tower DMAC that temperature is 155 DEG C recycles tower reactor pumping by cyclohexene, initially enters cyclohexene Separation tower bottoms high-performance heat exchanger exchanges heat to 135 DEG C of cyclohexene knockout tower of kettle liquid, and DMAC temperature is reduced to 140 DEG C, It is secondary that hexamethylene treating column the second kettle liquid high-performance heat exchanger is gone to exchange heat 110 DEG C of hexamethylene purification tower bottoms, by DMAC temperature Degree is reduced to 115 DEG C, subsequently into cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger to 85 DEG C of cyclohexanol separate tower bottoms into Row heat exchange, DMAC temperature are reduced to 95 DEG C, then enter back into cyclohexanol reactor feed high-performance heat exchanger and carry out to charging cyclohexene Cyclohexene temperature is increased to 70 DEG C by 50 DEG C by heat exchange, and DMAC temperature is reduced to 80 DEG C, then cooling through cyclohexene knockout tower extractant Device enters cyclohexene knockout tower top after DMAC temperature is cooled to 75 DEG C and carries out extraction cyclohexene, then separates tower reactor through cyclohexene Pumping goes out to be sent to cyclohexene recovery tower and carries out multi-cycle separation recycling cyclohexene；

3. 160 DEG C of cyclohexanol gas of decylization hexene tower side take-off removes cyclohexanol knockout tower kettle liquid evaporator first, 85 DEG C of the kettle liquid come to cyclohexanol separation tower reactor pumping carries out heating evaporation, and temperature is 145 DEG C of cyclohexanol gas-liquids after cooling Mixture enters cyclohexanol reactor third feed heater, heats to the cyclohexene into hydration reactor, by cyclohexene Temperature is increased to 125 DEG C by 110 DEG C, and cyclohexanol gas-liquid mixture is cooled to 120 DEG C, feeds and heats with cyclohexanol reactor third The cyclohexanol condenser auxiliary of device parallel connection condenses the cyclohexanol gas of side take-off, after condensation temperature be 120 DEG C of cyclohexanol by Cyclohexanol pumps out, and heats through the first feed heater of cyclohexanol reactor to cyclohexene, and cyclohexene temperature is increased by 70 DEG C To 85 DEG C, the temperature of cyclohexanol is reduced to 95 DEG C, then enters cyclohexanol intermediate products tank after cyclohexanol cooler is cooling；

The temperature that cyclohexanol separation tower bottoms evaporator steams is that 135 DEG C of cyclohexanol and cyclohexene mixed gas enter hexamethylene The second feed heater of alcohol reactor, heats the cyclohexene into hydration reactor, and cyclohexene temperature is increased by 85 DEG C To 110 DEG C, decylization hexene tower feed cooler auxiliary in parallel with the second feed heater of cyclohexanol reactor by cyclohexanol and Cyclohexene Mixed Gas Condensation is to 96 DEG C；

4. it is efficient to be introduced into the charging of cyclohexanol knockout tower for the hexamethylene gas phase steam of 95 DEG C of hexamethylene treating column top exit Temperature is reduced to 86 DEG C after thermal energy recoverer feeds progress heating recovery heat to cyclohexanol knockout tower, and hexamethylene is then gone to refine Tower gas phase condenser is condensed, and condensed liquid phase flows into hexamethylene treating column return tank, and on-condensible gas removes torch；Cyclohexanol The temperature of knockout tower charging is increased to 65 DEG C by 60 DEG C, and then air-liquid enters cyclohexanol knockout tower.

Embodiment 4

Gone out 1. the benzene that temperature is 145 DEG C recycles tower bottoms DMAC by benzene recycling tower reactor pumping, initially enters benzene separation tower reactor Liquid high-performance heat exchanger exchanges heat to 130 DEG C of benzene knockout tower of kettle liquid, and DMAC temperature is reduced to 128 DEG C, next goes hexamethylene smart Tower the first kettle liquid high-performance heat exchanger processed exchanges heat to 95 DEG C of hexamethylene purification tower bottoms, DMAC temperature is reduced to 108 DEG C, so The cyclohexanol separation tower bottoms for entering cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger afterwards to 77 DEG C exchanges heat, DMAC temperature 88 DEG C are reduced to, charging is heated subsequently into benzene knockout tower feed heater, feeding temperature is increased to 64 DEG C by 38 DEG C Left and right, DMAC temperature are reduced to 72 DEG C, then into benzene point after DMAC temperature is cooled to 62 DEG C by benzene knockout tower extractant cooler Cycling extraction benzene is carried out from tower, then goes out to be sent to benzene recovery tower through benzene separation tower reactor pumping and carries out multi-cycle separation recycling benzene；

Go out 2. the cyclohexene recovery tower DMAC that temperature is 148 DEG C recycles tower reactor pumping by cyclohexene, initially enters cyclohexene Separation tower bottoms high-performance heat exchanger exchanges heat to 125 DEG C of cyclohexene knockout tower of kettle liquid, and DMAC temperature is reduced to 130 DEG C, It is secondary that hexamethylene treating column the second kettle liquid high-performance heat exchanger is gone to exchange heat 100 DEG C of hexamethylene purification tower bottoms, by DMAC temperature Degree is reduced to 112 DEG C, subsequently into cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger to 82 DEG C of cyclohexanol separate tower bottoms into Row heat exchange, DMAC temperature are reduced to 92 DEG C, then enter back into cyclohexanol reactor feed high-performance heat exchanger and carry out to charging cyclohexene Cyclohexene temperature is increased to 68 DEG C by 38 DEG C by heat exchange, and DMAC temperature is reduced to 78 DEG C, then cooling through cyclohexene knockout tower extractant Device enters cyclohexene knockout tower top after DMAC temperature is cooled to 74 DEG C and carries out extraction cyclohexene, then separates tower reactor through cyclohexene Pumping goes out to be sent to cyclohexene recovery tower and carries out multi-cycle separation recycling cyclohexene；

3. 158 DEG C of cyclohexanol gas of decylization hexene tower side take-off removes cyclohexanol knockout tower kettle liquid evaporator first, 82 DEG C of the kettle liquid come to cyclohexanol separation tower reactor pumping carries out heating evaporation, and temperature is 138 DEG C of cyclohexanol gas-liquids after cooling Mixture enters cyclohexanol reactor third feed heater, heats to the cyclohexene into hydration reactor, by cyclohexene Temperature is increased to 118 DEG C by 112 DEG C, and cyclohexanol gas-liquid mixture is cooled to 118 DEG C, feeds and heats with cyclohexanol reactor third The cyclohexanol condenser auxiliary of device parallel connection condenses the cyclohexanol gas of side take-off, after condensation temperature be 114 DEG C of cyclohexanol by Cyclohexanol pumps out, and heats through the first feed heater of cyclohexanol reactor to cyclohexene, and cyclohexene temperature is increased by 68 DEG C To 78 DEG C, the temperature of cyclohexanol is reduced to 94 DEG C, then enters cyclohexanol intermediate products tank after cyclohexanol cooler is cooling；

The temperature that cyclohexanol separation tower bottoms evaporator steams is that 128 DEG C of cyclohexanol and cyclohexene mixed gas enter hexamethylene The second feed heater of alcohol reactor, heats the cyclohexene into hydration reactor, and cyclohexene temperature is risen by 74 DEG C DEG C Up to 106 DEG C, the decylization hexene tower feed cooler in parallel with the second feed heater of cyclohexanol reactor is assisted cyclohexanol With cyclohexene Mixed Gas Condensation to 92 DEG C；

4. it is efficient to be introduced into the charging of cyclohexanol knockout tower for the hexamethylene gas phase steam of 84 DEG C of hexamethylene treating column top exit Temperature is reduced to 85 DEG C after thermal energy recoverer feeds progress heating recovery heat to cyclohexanol knockout tower, and hexamethylene is then gone to refine Tower gas phase condenser is condensed, and condensed liquid phase flows into hexamethylene treating column return tank, and on-condensible gas removes torch；Cyclohexanol The temperature of knockout tower charging is increased to 60 DEG C by 54 DEG C, and then air-liquid enters cyclohexanol knockout tower.

Embodiment 5

Gone out 1. the benzene that temperature is 150 DEG C recycles tower bottoms DMAC by benzene recycling tower reactor pumping, initially enters benzene separation tower reactor Liquid high-performance heat exchanger exchanges heat to 130 DEG C of benzene knockout tower of kettle liquid, and DMAC temperature is reduced to 130 DEG C, next goes hexamethylene smart Tower the first kettle liquid high-performance heat exchanger processed exchanges heat to 90 DEG C of hexamethylene purification tower bottoms, DMAC temperature is reduced to 110 DEG C, so The cyclohexanol separation tower bottoms for entering cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger afterwards to 78 DEG C exchanges heat, DMAC temperature 80 DEG C are reduced to, charging is heated subsequently into benzene knockout tower feed heater, feeding temperature is increased to 65 DEG C by 40 DEG C Left and right, DMAC temperature are reduced to 72 DEG C, then into benzene point after DMAC temperature is cooled to 63 DEG C by benzene knockout tower extractant cooler Cycling extraction benzene is carried out from tower, then goes out to be sent to benzene recovery tower through benzene separation tower reactor pumping and carries out multi-cycle separation recycling benzene；

Go out 2. the cyclohexene recovery tower DMAC that temperature is 150 DEG C recycles tower reactor pumping by cyclohexene, initially enters cyclohexene Separation tower bottoms high-performance heat exchanger exchanges heat to 130 DEG C of cyclohexene knockout tower of kettle liquid, and DMAC temperature is reduced to 130 DEG C, It is secondary that hexamethylene treating column the second kettle liquid high-performance heat exchanger is gone to exchange heat 100 DEG C of hexamethylene purification tower bottoms, by DMAC temperature Degree is reduced to 110 DEG C, subsequently into cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger to 80 DEG C of cyclohexanol separate tower bottoms into Row heat exchange, DMAC temperature are reduced to 90 DEG C, then enter back into cyclohexanol reactor feed high-performance heat exchanger and carry out to charging cyclohexene Cyclohexene temperature is increased to 68 DEG C by 40 DEG C by heat exchange, and DMAC temperature is reduced to 78 DEG C, then cooling through cyclohexene knockout tower extractant Device enters cyclohexene knockout tower top after DMAC temperature is cooled to 72 DEG C and carries out extraction cyclohexene, then separates tower reactor through cyclohexene Pumping goes out to be sent to cyclohexene recovery tower and carries out multi-cycle separation recycling cyclohexene；

3. 155 DEG C of cyclohexanol gas of decylization hexene tower side take-off removes cyclohexanol knockout tower kettle liquid evaporator first, 78 DEG C of the kettle liquid come to cyclohexanol separation tower reactor pumping carries out heating evaporation, and temperature is 140 DEG C of cyclohexanol gas-liquids after cooling Mixture enters cyclohexanol reactor third feed heater, heats to the cyclohexene into hydration reactor, by cyclohexene Temperature is increased to 120 DEG C by 110 DEG C, and cyclohexanol gas-liquid mixture is cooled to 118 DEG C, feeds and heats with cyclohexanol reactor third The cyclohexanol condenser auxiliary of device parallel connection condenses the cyclohexanol gas of side take-off, after condensation temperature be 115 DEG C of cyclohexanol by Cyclohexanol pumps out, and heats through the first feed heater of cyclohexanol reactor to cyclohexene, and cyclohexene temperature is increased by 68 DEG C To 75 DEG C, the temperature of cyclohexanol is reduced to 92 DEG C, then enters cyclohexanol intermediate products tank after cyclohexanol cooler is cooling；

The temperature that cyclohexanol separation tower bottoms evaporator steams is that 130 DEG C of cyclohexanol and cyclohexene mixed gas enter hexamethylene The second feed heater of alcohol reactor, heats the cyclohexene into hydration reactor, and cyclohexene temperature is increased by 75 DEG C To 105 DEG C, decylization hexene tower feed cooler auxiliary in parallel with the second feed heater of cyclohexanol reactor by cyclohexanol and Cyclohexene Mixed Gas Condensation is to 92 DEG C；

4. it is efficient to be introduced into the charging of cyclohexanol knockout tower for the hexamethylene gas phase steam of 88 DEG C of hexamethylene treating column top exit Temperature is reduced to 78 DEG C after thermal energy recoverer feeds progress heating recovery heat to cyclohexanol knockout tower, and hexamethylene is then gone to refine Tower gas phase condenser is condensed, and condensed liquid phase flows into hexamethylene treating column return tank, and on-condensible gas removes torch；Cyclohexanol The temperature of knockout tower charging is increased to 63 DEG C by 58 DEG C, and then air-liquid enters cyclohexanol knockout tower.

What 1 2~embodiment of embodiment 5 of table produced cyclohexanol Boiler Steam per ton uses scale

	Produce Boiler Steam amount/ton of cyclohexanol per ton	Produce circulation water consumption/ton of cyclohexanol per ton
			Embodiment 2	2.51	260
Embodiment 3	2.49	245
			Embodiment 4	2.45	230
Embodiment 5	2.47	240

When the application is not used, producing cyclohexanol per ton to need the quantity of Boiler Steam is 6.5~7.5 tons or so, circulation The dosage of water is 700~800 tons or so, and the cost of steam per ton is 160 yuan or so, and the cost of recirculated water per ton is 0.1 yuan of left side The right side, by the production system equipment and production method of the application, as shown in table 1, it can be seen that produce cyclohexanol per ton and save pot Furnace steam can reach 2.0~2.5 tons or so, and the dosage of recirculated water reduces by 200~250 tons, reduce by 350~425 yuan of production cost/ Ton has huge economic benefit, realizes the recycling of heat, safety and environmental protection.

Embodiment 6

As shown in figure 5, cyclohexanol knockout tower feeds high efficient heat recovery device, including gas-liquid separator 1 and heat exchanger 2, gas Liquid/gas separator 1 is connected by the first connecting pipe 3 with the second connecting pipe 4 with heat exchanger 2；1 top of gas-liquid separator Position offers gas vent 5, for gas to be passed through cyclohexanol knockout tower after gas-liquid separation；The side of gas-liquid separator 1 Material inlet 6 is opened up, for receiving the charging of cyclohexanol knockout tower；Liquidometer 7, institute are installed in the downside of the material inlet 6 The upper end for stating liquidometer 7 is communicated by liquidometer upper orifice 8 with gas-liquid separator 1, and the lower end of liquidometer 7 passes through liquidometer down tube Mouthfuls 9 communicate with gas-liquid separator 1, the liquidometer 7 can real-time display go out the liquid level of material in gas-liquid separator 1；The gas-liquid The side of 1 bottom position of separator opens up material outlet 10, installs control valve 11 after material outlet 10, material can control to flow out gas The flow of liquid/gas separator 1, the liquid material after gas-liquid separation are passed through in cyclohexanol knockout tower via material outlet 10；The gas-liquid Liquid outlet 12 is equipped at 1 bottom centre position of separator, liquid outlet 12 is communicated with the first connecting pipe 3；The gas-liquid point Wire mesh demister 13 is installed from 1 inner upper of device, wire mesh demister 13 is used to remove the mist carried secretly in separation gas；Gas-liquid point Anti-swirl baffle 14 is installed from 1 lower inside of device, anti-swirl baffle 14 is located at 12 top of liquid outlet；

The other end of first connecting pipe 3 connects liquid-inlet 15, and liquid-inlet 15 is located at the bottom of heat exchanger 2； The heat exchanger 2 includes several efficient heat-exchanging pipes 17 of heat exchanger shell 16 with internal setting, and 2 inside of heat exchanger is pacified up and down Filling two tube sheets 23, two tube sheets 23 divide heat exchanger 2 for three chambers, and upper and lower two chambers are connected by efficient heat-exchanging pipe 17, in Between cavity be used for efficient heat-exchanging pipe 17 and heat gas heat exchange, 16 top of heat exchanger shell side be equipped with heat gas Body import 18 is equipped with heat gas outlet 19 in the lower part of 16 other side of heat exchanger shell, and the heat gas comes from hexamethylene The process steam for the treatment of column enters inside heat exchanger 2 from heat gas import 18, after exchanging heat with efficient heat-exchanging pipe 17 again Heated gas vent 19 is passed through in hexamethylene treating column gas phase condenser；The row of offering at 16 upper position of heat exchanger shell Port 20 under abnormal operating state, opens exhaust outlet 20 for discharging 16 inner part inert gas of heat exchanger shell, prevents shadow Ring the heat-transfer effect of heat exchanger 2；It is offered in 16 lower position of heat exchanger shell and leads leaching mouth 21, for discharging heat exchange when parking Hydrops in device 2；

When cyclohexanol knockout tower charging high efficient heat recovery device running when, cyclohexanol knockout tower charging by material inlet 6 into Enter into gas-liquid separator 1, separated gas is after wire mesh demister 13 removes the mist of deentrainment in gas-liquid separator 1 It is passed through in cyclohexanol knockout tower by gas vent 5,1 materials inside of gas-liquid separator passes through liquid outlet 12 and the first connecting pipe 3 enter in heat exchanger 2, the efficient heat-exchanging pipe 17 in the heat exchanger 2 and hexamethylene treating column discharge process steam into After row heat exchange, then flowed back in gas-liquid separator 1 by the second connecting pipe 4；In circulation certain time, temperature, liquid level, which reach, to be wanted After asking, material is continuously controlled by control valve 11 and is sent into cyclohexanol knockout tower by outlet 10, meanwhile, cyclohexanol knockout tower Charging also enters gas-liquid separator 1 continuously through material inlet 6；The aperture of adjusting control valve 11 is kept in gas-liquid separator 1 Material liquid surface 22 be between 9 position of liquidometer upper orifice 8 and liquidometer lower nozzle.

Claims

1. new heat energy utilization system in a kind of cyclohexanol production, it is characterised in that: including benzene recovery tower heat energy utilization unit, ring Hexene recovery tower heat energy utilization unit, decylization hexene tower heat energy utilization unit and hexamethylene treating column heat energy utilization unit；

Wherein benzene recovery tower heat energy utilization unit include benzene recovery tower, benzene recycling tower reactor pump, benzene separation tower bottoms high-performance heat exchanger, The first kettle liquid of hexamethylene treating column high-performance heat exchanger, the first kettle liquid of cyclohexanol knockout tower high-performance heat exchanger, the charging of benzene knockout tower add Hot device, benzene knockout tower extractant cooler, benzene knockout tower, benzene separation tower reactor pump；

Cyclohexene recovery tower heat energy utilization unit includes cyclohexene recovery tower, cyclohexene recycling tower reactor pump, cyclohexene separation tower reactor Liquid high-performance heat exchanger, the second kettle liquid of hexamethylene treating column high-performance heat exchanger, the second kettle liquid of cyclohexanol knockout tower high-performance heat exchanger, ring Hexanol reactor feed high-performance heat exchanger, cyclohexene knockout tower extractant cooler and cyclohexene knockout tower, cyclohexene knockout tower Kettle pump；

Decylization hexene tower heat energy utilization unit includes decylization hexene tower, cyclohexanol separation tower bottoms evaporator, cyclohexanol reactor Third feed heater, cyclohexanol condenser, cyclohexanol pump, the first feed heater of cyclohexanol reactor, cyclohexanol cooler, Cyclohexanol intermediate products tank, the second feed heater of cyclohexanol reactor, decylization hexene tower feed cooler, decylization hexene tower into Expect surge tank；

Hexamethylene treating column heat energy utilization unit include hexamethylene treating column, cyclohexanol knockout tower charging high efficient heat recovery device, Hexamethylene treating column gas phase condenser, hexamethylene treating column return tank and cyclohexanol knockout tower；

The outlet of benzene recovery tower bottoms material recycles tower reactor pump by benzene and separates tower bottoms with benzene in benzene recovery tower heat energy utilization unit The shell-side inlet of high-performance heat exchanger connects, and benzene separates the shell-side outlet and the first kettle of hexamethylene treating column of tower bottoms high-performance heat exchanger The shell-side inlet of liquid high-performance heat exchanger by pipeline connect, the shell-side outlet of hexamethylene treating column the first kettle liquid high-performance heat exchanger with The shell-side inlet of cyclohexanol knockout tower the first kettle liquid high-performance heat exchanger is connected by pipeline, and the first kettle liquid of cyclohexanol knockout tower is efficient The shell-side outlet of heat exchanger is connect with benzene knockout tower feed heater heating medium inlet by pipeline, the charging heating of benzene knockout tower Device Crude product input is connect with the shell-side inlet of benzene knockout tower extractant cooler by pipeline, and benzene knockout tower extractant is cooling The shell-side outlet of device is connect with benzene knockout tower extractant entrance by pipeline, and benzene knockout tower outlet at bottom separates tower reactor by benzene and pumps It is connect with the material inlet of benzene recovery tower；

The outlet of cyclohexene recovery tower bottoms material is recycled tower reactor pump by cyclohexene and is connected in cyclohexene recovery tower heat energy utilization unit The shell-side inlet of cyclohexene separation tower bottoms high-performance heat exchanger is connect, the shell-side outlet that cyclohexene separates tower bottoms high-performance heat exchanger is logical Piping connects the shell-side inlet of the second kettle liquid of hexamethylene treating column high-performance heat exchanger, and the second kettle liquid of hexamethylene treating column is efficiently changed The shell-side outlet of hot device connects the shell-side inlet of the second kettle liquid of cyclohexanol knockout tower high-performance heat exchanger, cyclohexanol separation by pipeline The shell-side outlet of tower the second kettle liquid high-performance heat exchanger is entered by the shell-side that pipeline connects cyclohexanol reactor feed high-performance heat exchanger Mouthful, the shell-side outlet of cyclohexanol reactor feed high-performance heat exchanger connects cyclohexene knockout tower extractant cooler by pipeline The shell-side outlet of shell-side inlet, cyclohexene knockout tower extractant cooler is entered by the extractant that pipeline connects cyclohexene knockout tower Mouthful, the outlet at bottom of cyclohexene knockout tower separates tower reactor pump connection cyclohexene recovery tower material inlet by cyclohexene；

The side take-off mouth of decylization hexene tower connects cyclohexanol knockout tower kettle by pipeline in decylization hexene tower heat energy utilization unit The Crude product input of the heating medium inlet of liquid evaporator, cyclohexanol separation tower bottoms evaporator connects cyclohexanol by pipeline The pipe side outlet of the pipe side entrance of reactor third feed heater, cyclohexanol reactor third feed heater passes through cyclohexanol The shell-side inlet of pump connection the first feed heater of cyclohexanol reactor, the shell-side of the first feed heater of cyclohexanol reactor go out Mouth is connect by pipeline with the shell-side inlet of cyclohexanol cooler, the shell-side outlet and cyclohexanol intermediate products of cyclohexanol cooler Tank is connected by pipeline；Cyclohexanol condenser is connected in parallel with cyclohexanol reactor third feed heater；Cyclohexanol knockout tower The gaseous phase outlet of kettle liquid evaporator is connect by pipeline with the pipe side entrance of the second feed heater of cyclohexanol reactor, cyclohexanol The pipe side outlet of the second feed heater of reactor is connect by pipeline with decylization hexene tower feed surge tank, decylization hexene tower into Material cooler is connected in parallel with the second feed heater of cyclohexanol reactor；

The top gas phase outlet and the charging of cyclohexanol knockout tower of hexamethylene treating column heat energy utilization unit cyclohexane treating column are high The shell-side inlet connection of thermal energy recoverer is imitated, cyclohexanol knockout tower feeds the outlet of shell-side lower end and the hexamethylene of high efficient heat recovery device The entrance of alkane treating column gas phase condenser connects, and the liquid-phase outlet and hexamethylene treating column of hexamethylene treating column gas phase condenser return Tank connection is flowed, the liquid-phase outlet of cyclohexanol knockout tower charging high efficient heat recovery device and top gas phase outlet are separated with cyclohexanol Tower connection；

Hexamethylene treating column the first kettle liquid high-performance heat exchanger and hexamethylene treating column the second kettle liquid high-performance heat exchanger are connected in parallel；Ring Hexanol knockout tower the first kettle liquid high-performance heat exchanger and cyclohexanol knockout tower the second kettle liquid high-performance heat exchanger are connected in parallel.

2. new heat energy utilization system in a kind of cyclohexanol production according to claim 1, it is characterised in that: cyclohexanol point High efficient heat recovery device, including gas-liquid separator (1) and heat exchanger (2), gas-liquid separator (1) and heat exchanger (2) are fed from tower It is connected by the first connecting pipe (3) with the second connecting pipe (4)；Gas-liquid separator (1) top position offers gas Body exports (5), for gas to be passed through cyclohexanol knockout tower after gas-liquid separation；The side of gas-liquid separator (1) opens up material Import (6), for receiving the charging of cyclohexanol knockout tower；It is equipped on the downside of the material inlet (6) liquidometer (7), it is described The upper end of liquidometer (7) is communicated by liquidometer upper orifice (8) with gas-liquid separator (1), and the lower end of liquidometer (7) passes through liquid level Meter lower nozzle (9) communicated with gas-liquid separator (1), the liquidometer (7) can real-time display go out gas-liquid separator (1) interior material Liquid level；The side of gas-liquid separator (1) bottom position opens up material outlet (10), and material outlet (10) installs control valve afterwards (11), the flow that can control material outflow gas-liquid separator (1), the liquid material after gas-liquid separation are logical via material outlet (10) Enter in cyclohexanol knockout tower；Liquid outlet (12) are equipped at gas-liquid separator (1) bottom centre position, liquid outlet (12) It is communicated with the first connecting pipe (3)；Gas-liquid separator (1) inner upper installs wire mesh demister (13), wire mesh demister (13) for removing the mist carried secretly in separation gas；Gas-liquid separator (1) lower inside installs anti-swirl baffle (14), anti-whirlpool Stream baffle (14) is located above liquid outlet (12)；

The other end of first connecting pipe (3) connects liquid-inlet (15), and liquid-inlet (15) is located at the bottom of heat exchanger (2) Portion；The heat exchanger (2) includes several efficient heat-exchanging pipes (17) of heat exchanger shell (16) and internal setting, the heat exchanger (2) internal to install two tube sheets (23) up and down, heat exchanger (2) is divided into three chambers by two tube sheets (23), and upper and lower two chambers pass through Efficient heat-exchanging pipe (17) connection, intermediate cavity is used for the heat exchange of efficient heat-exchanging pipe (17) and heat gas, in heat exchanger shell The side on body (16) top is equipped with heat gas import (18), is equipped with heat gas in the lower part of heat exchanger shell (16) other side It exports (19), process steam of the heat gas from hexamethylene treating column, enters heat exchanger from heat gas import (18) (2) internal, heated gas vent (19) is passed through hexamethylene treating column gas phase again after exchanging heat with efficient heat-exchanging pipe (17) In condenser；It is offered exhaust outlet (20) at heat exchanger shell (16) upper position, under abnormal operating state, opens exhaust Mouth (20) prevents the heat-transfer effect for influencing heat exchanger (2) for discharging heat exchanger shell (16) inner part inert gas；It is exchanging heat Device shell (16) lower position, which offers, leads leaching mouth (21), for discharging the hydrops in heat exchanger (2) when parking；

When the charging high efficient heat recovery device running of cyclohexanol knockout tower, the charging of cyclohexanol knockout tower is entered by material inlet (6) In to gas-liquid separator (1), separated gas removes the mist of deentrainment by wire mesh demister (13) in gas-liquid separator (1) It is passed through in cyclohexanol knockout tower after foam by gas vent (5), gas-liquid separator (1) materials inside passes through liquid outlet (12) and the One connecting pipe (3) enters in heat exchanger (2), and the efficient heat-exchanging pipe (17) and hexamethylene in the heat exchanger (2) refine After the process steam of tower discharge carries out heat exchange, then flowed back in gas-liquid separator (1) by the second connecting pipe (4)；In circulation one It fixes time, after temperature, liquid level reach requirement, material is continuously controlled by control valve (11) by outlet (10) and is sent into cyclohexanol In knockout tower, meanwhile, the charging of cyclohexanol knockout tower also enters gas-liquid separator (1) continuously through material inlet (6)；Adjust control The aperture of valve (11) processed keeps the material liquid surface (22) in gas-liquid separator (1) to be under liquidometer upper orifice (8) and liquidometer Between nozzle (9) position.

3. new heat energy utilization system in a kind of cyclohexanol production according to claim 1, it is characterised in that: cyclohexanol is anti- Answer the first feed heater of device, the second feed heater of cyclohexanol reactor and the series connection of cyclohexanol reactor third feed heater Connection.