CN215756524U - Cyclohexane oxidation waste alkali liquid evaporation plant in cyclohexanone production process - Google Patents
Cyclohexane oxidation waste alkali liquid evaporation plant in cyclohexanone production process Download PDFInfo
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Abstract
The utility model relates to a cyclohexane oxidation waste alkali liquid evaporation device in a cyclohexanone production process, which mainly comprises a distillation tower, a distillation tower condenser, a waste alkali liquid evaporator feed pump, a distillation tower reboiler, a water condensing tank, a condensed water delivery pump, an evaporation separator, a waste alkali liquid circulating pump, a waste alkali liquid evaporator and a waste alkali liquid pump; the waste alkali liquor from the waste alkali liquor separator enters a distillation tower, a vapor phase at the top of the distillation tower is condensed by a circulating water condenser to obtain an oil-water mixture, and the oil-water mixture returns to a decomposition reaction system to recover organic matters in the waste alkali liquor; and evaporating and concentrating the produced liquid in the tower kettle, wherein the evaporation adopts a countercurrent process flow, the concentration of the waste alkali liquid after evaporation and concentration reaches more than 45 percent, and then the waste alkali liquid is sent to a waste alkali liquid incineration device. The device can recover organic substances of cyclohexane, cyclohexanol and cyclohexanone in the waste alkali liquor, and secondary steam is used for steam of a reboiler of the distillation tower, so that the steam consumption is reduced, and the energy consumption and material consumption of the device are reduced; meanwhile, the device avoids the scaling phenomenon of the equipment in the operation process, and prolongs the operation period of the device.
Description
Technical Field
The utility model belongs to the technical field of petrochemical industry, and relates to a cyclohexane oxidation waste alkali liquid evaporation device in a cyclohexanone production process.
Background
In the process of producing cyclohexanone by a cyclohexane oxidation method, alkali is added in the decomposition process of cyclohexyl hydroperoxide to improve the decomposition conversion rate of the cyclohexyl hydroperoxide and neutralize organic acid and saponified organic ester which are byproducts of oxidation, waste alkali liquid is separated by a waste alkali liquid separator after decomposition reaction, part of the separated waste alkali liquid returns to a decomposition reactor, and most of the waste alkali liquid needs to be treated. The waste alkali liquor mainly contains NaOH and Na except water2CO3And sodium valerate, sodium hydroxyhexanoate, sodium adipate and other organic acid salts, and also contains a small amount (about 0.5 wt%) of cyclohexane, cyclohexanone, cyclohexanol and other organic substances. Because the waste alkali liquor has strong alkalinity and high salt content, the waste alkali liquor cannot be directly treated by a biochemical method and cannot be directly discharged. The common treatment process adopted in the oxidation method cyclohexanone production process at present is that the waste alkali liquor is evaporated and concentrated to about 45-50% of solid content, and then is sent into a waste alkali liquor incinerator for harmless incineration treatment.
The cyclohexane oxidation waste lye treatment originally adopts the technology of introducing devices abroad in the last 90 s, the oxidation waste lye which passes through an evaporator at one time is heated to more than 110 ℃ by using low-pressure steam, then the oxidation waste lye enters a gas-liquid separator to be separated from a vapor phase, an oil-water mixture after the vapor phase is condensed returns to a decomposition reaction system, and the concentrated waste lye is sent to a waste lye incinerator to be directly incinerated. In the actual production, the waste lye contains a large amount of Na2CO3When the waste alkali liquor is concentrated in the evaporator, the heat exchanger tubes are often blocked due to the saturated concentration and scaling of the salt, so that the heat transfer capacity of the evaporator is reduced, and the operation period of the equipment is seriously influenced. At present, most devices can only reach about 40 percent (wt) of solid content after the waste lye is concentrated, and cannot meet the feeding requirement of a waste lye incineratorAnd the treatment difficulty and cost of the waste alkali liquid incinerator are increased. Through continuous process optimization, the main process of the prior waste alkali liquid treatment comprises the steps of primarily evaporating and concentrating the waste alkali liquid to 25-30% of solid content, concentrating the waste alkali liquid to more than 40% of solid content through secondary concentration, and then sending the concentrated waste alkali liquid into a waste alkali liquid incinerator for treatment, so that the combustion efficiency of the waste alkali liquid incinerator is improved, a large amount of auxiliary fuel is saved, more byproduct steam is generated, and increasingly strict environmental protection requirements are met. However, although the solid content of the waste alkali liquor only needs to be concentrated to 25-30% in the primary evaporator, because the primary evaporation process of parallel flow (concurrent flow) feeding is adopted in the secondary concentration, the inorganic matter concentration of the primary reboiler is relatively high and the temperature is relatively low compared with that of the secondary reboiler, so that Na is caused2CO3The tube fouling of the saturated reboiler is achieved, and the operation period of the equipment is influenced.
The waste alkali liquor is obtained by oil-water separation of decomposition liquid containing alcoholic ketoalkane, wherein a small amount of valuable components are dissolved, such as: cyclohexanone, cyclohexanol and cyclohexane; the existing treatment process adopts a pure evaporation process, and the capacity of extracting organic matters is poor.
Aiming at the problems, the utility model firstly recovers the organic matters in the waste alkali liquor through once steam stripping; then multi-effect evaporation concentration is carried out, so that the energy consumption of the device is reduced; the evaporation adopts a countercurrent process flow, and the problem of Na caused by the increase of the concentration of inorganic matters in the solution of the temperature of the waste alkali liquor in the single-effect reboiler is solved by improving the temperature of the waste alkali liquor in the single-effect reboiler2CO3The problem of tube array scaling of the saturated reboiler is solved.
Disclosure of Invention
The utility model aims to provide a cyclohexane oxidation waste alkali liquid evaporation device in a cyclohexanone production process. The method comprises the steps of recovering organic matters in the waste alkali liquor through primary gas stripping, and then carrying out evaporation concentration, wherein the evaporation adopts a countercurrent feeding process; the utility model can recover the organic substances cyclohexane, cyclohexanol and cyclohexanone in the waste alkali liquor; the steam consumption is reduced, and the energy consumption and the material consumption of the device are reduced; meanwhile, the device avoids the scaling phenomenon of the equipment in the operation process, and greatly prolongs the operation period of the device.
Technical scheme for achieving purpose of the utility model
A cyclohexane oxidation waste alkali liquid evaporation device in a cyclohexanone production process comprises a distillation tower, a distillation tower condenser, a waste alkali liquid evaporator feed pump, a distillation tower reboiler, a condensate tank, an evaporation separator, a waste alkali liquid circulating pump, a waste alkali liquid evaporator and a waste alkali liquid pump; the pipeline from the waste alkali liquor separator is connected with a distillation tower, the tower kettle of the distillation tower is connected with a feed pump of a waste alkali liquor evaporator, and the tower top of the distillation tower is connected with a distillation tower condenser; the outlet of a feed pump of the waste alkali evaporator is respectively connected with a reboiler of the distillation tower and a circulating pump of the waste alkali, the reboiler of the distillation tower is connected with the distillation tower, the heating side inlet of the reboiler of the distillation tower is connected with a vapor phase pipeline at the top of the evaporation separator, and the heating side liquid outlet of the reboiler of the distillation tower is connected with a water condensing tank; the waste alkali liquor circulating pump is connected with a waste alkali liquor evaporator, and the waste alkali liquor evaporator is connected with the evaporation separator; the bottom of the evaporation separator is respectively connected with a waste lye circulating pump and a waste lye pump. The heating steam of the distillation tower can still be supplied by secondary evaporation steam.
And a vapor phase outlet of the heating side of the distillation tower reboiler is connected with a distillation tower condenser.
One of the implementation modes is that the cyclohexane oxidation waste alkali liquid evaporation device in the cyclohexanone production process is composed of a distillation tower, a distillation tower condenser, a waste alkali liquid double-effect evaporator feed pump, a distillation tower reboiler, a double-effect evaporation separator, a waste alkali liquid double-effect evaporator, a double-effect evaporation condenser, a water condensation tank, a waste alkali liquid single-effect evaporator feed pump, a single-effect evaporation separator, a waste alkali liquid single-effect evaporator, a waste alkali liquid circulating pump and a waste alkali liquid pump; the pipeline from the waste alkali liquor separator is connected with a distillation tower, the top vapor phase outlet of the distillation tower is connected with a distillation tower condenser, the tower kettle of the distillation tower is connected with a waste alkali liquor dual-effect evaporator feed pump, the outlet of the waste alkali liquor dual-effect evaporator feed pump is respectively connected with a distillation tower reboiler and a dual-effect evaporation separator, the liquid phase outlet of the dual-effect evaporation separator is connected with a waste alkali liquor single-effect evaporator feed pump, the outlet of the waste alkali liquor single-effect evaporator feed pump is respectively connected with a single-effect evaporation separator and a waste alkali liquor dual-effect evaporator, the waste alkali liquor dual-effect evaporator is connected with a dual-effect evaporation separator, the heating pipeline of the waste alkali liquor dual-effect evaporator is connected with the top vapor phase pipeline of the single-effect evaporation separator, the top vapor phase pipeline of the dual-effect evaporation separator is connected with a dual-effect evaporation condenser, the vapor phase outlet of the dual-effect evaporation condenser is connected with a vacuum system, and the condensate outlet of the dual-effect evaporation condenser is connected with a condensate tank; the liquid phase pipeline of the first-effect evaporation separator is connected with the inlet of a waste alkali liquor circulating pump, the outlet of the waste alkali liquor circulating pump is connected with a waste alkali liquor first-effect evaporator, the waste alkali liquor first-effect evaporator is connected with the first-effect evaporation separator, and the liquid phase outlet of the first-effect evaporation separator is also connected with a waste alkali liquor pump; the vapor phase outlet of the heating side of the waste alkali liquor dual-effect evaporator is connected with the dual-effect evaporation condenser, and the vapor phase condensate outlet of the heating side of the waste alkali liquor dual-effect evaporator is connected with the condensate tank.
The water condensing tanks can be two water condensing tanks, one water condensing tank is connected with the two-effect evaporation condenser, the other water condensing tank is connected with the heating side liquid phase outlet of the two-effect evaporator, and the two water condensing tanks are connected.
The vapor phase outlet of the double-effect evaporation condenser can be connected with a vacuum system.
In another embodiment: the cyclohexane oxidation waste alkali liquid evaporation device in the cyclohexanone production process comprises a distillation tower, a distillation tower condenser, a vacuum system, a waste alkali liquid double-effect evaporator feed pump, a distillation tower reboiler, a condensate tank, a double-effect evaporation separator, a waste alkali liquid one-effect evaporator feed pump, a waste alkali liquid double-effect evaporator, a one-effect evaporation separator, a waste alkali liquid circulating pump, a waste alkali liquid one-effect evaporator and a waste alkali liquid pump; the waste alkali liquor separator pipeline is connected with a distillation tower, a vapor phase outlet at the top of the distillation tower is connected with a distillation tower condenser, the vapor phase outlet of the distillation tower condenser is connected with a vacuum system, a tower kettle of the distillation tower is connected with a feed pump of an alkali liquor double-effect evaporator, a feed pump outlet of the alkali liquor double-effect evaporator is respectively connected with a distillation tower reboiler and a double-effect evaporation separator, the distillation tower reboiler is connected with the distillation tower, and the distillation tower reboiler is connected with the vapor phase pipeline at the top of the double-effect evaporation separator; the liquid phase outlet of the double-effect evaporation separator is connected with the inlet of a feed pump of a waste alkali liquid one-effect evaporator, the outlet of the feed pump of the waste alkali liquid one-effect evaporator is respectively connected with the single-effect evaporation separator and the waste alkali liquid two-effect evaporator, the waste alkali liquid two-effect evaporator is connected with the double-effect evaporation separator, the waste alkali liquid two-effect evaporator and the top vapor phase pipeline of the single-effect evaporation separator, and the condensate outlets of the waste alkali liquid two-effect evaporator and a distillation tower reboiler are connected with a condensate tank; the liquid phase outlet of the first-effect evaporation separator is respectively connected with a waste alkali liquor circulating pump and a waste alkali liquor pump, the waste alkali liquor circulating pump is connected with a waste alkali liquor first-effect evaporator, and the waste alkali liquor first-effect evaporator is connected with the first-effect evaporation separator. A heating side vapor phase outlet of a reboiler of the distillation tower is connected with a condenser of the distillation tower; the heating side vapor phase outlet of the waste alkali liquor double-effect evaporator is connected with the vapor phase pipeline of the double-effect evaporation separator.
In the above embodiment:
the distillation tower adopts a plate tower or a packed tower.
The reboiler of the distillation tower adopts a forced circulation reboiler or a built-in reboiler.
A heating steam pipeline of the single-effect evaporation concentration system is connected with a single-effect evaporator, steam is used for heating, and a countercurrent process flow is adopted for evaporation.
The vacuum system adopts a liquid ring pump or a dry vacuum pump.
The condensed water tank is connected with a condensed water delivery pump.
Features and effects of the utility model
The method comprises the steps of firstly, recovering organic matters in the waste alkali liquor through primary distillation, and then carrying out evaporation concentration, wherein the evaporation adopts a counter-current process flow; can recover organic substances of cyclohexane, cyclohexanol and cyclohexanone in the waste alkali liquor; the steam consumption is reduced, and the energy consumption and the material consumption of the device are reduced; as the countercurrent evaporation process flow is adopted, the temperature of the concentrated solution with high concentration in one effect is high, the scaling phenomenon of equipment in the operation process can be avoided, and the operation period and the safety of the device are improved.
Drawings
FIG. 1 shows an evaporation apparatus for cyclohexane oxidation waste lye in cyclohexanone production process
In the figure: 1-a distillation tower, 2-a distillation tower condenser, 3-a waste alkali liquid evaporator feed pump, 4-a distillation tower reboiler, 5-an evaporation separator, 6-a waste alkali liquid evaporator, 9-a condensate tank, 10-a condensate delivery pump, 15-a waste alkali liquid circulating pump, and 16-a waste alkali liquid pump.
CWS-recirculated cooling water LS-low pressure steam.
FIG. 2 shows an evaporation apparatus for cyclohexane oxidation waste lye in cyclohexanone production process
In the figure: the system comprises a distillation tower 1, a distillation tower 2, a distillation tower condenser, a waste alkali liquid double-effect evaporator feed pump 3, a distillation tower reboiler 4, a double-effect evaporation separator 5, a waste alkali liquid double-effect evaporator 6a, a double-effect evaporation condenser 7, a vacuum system 8, a double-effect evaporation water condensation tank 9a, a condensate delivery pump 10, a single-effect evaporation water condensation tank 11, a waste alkali liquid single-effect evaporator feed pump 12, a single-effect evaporation separator 13, a waste alkali liquid single-effect evaporator 14, a waste alkali liquid circulating pump 15 and a waste alkali liquid pump 16.
CWS-recirculated cooling water LS-low pressure steam.
FIG. 3 shows an evaporation apparatus for cyclohexane oxidation waste lye in cyclohexanone production process
In the figure: the method comprises the following steps of 1-a distillation tower, 2-a distillation tower condenser, 3-a waste alkali liquid double-effect evaporator feed pump, 4-a distillation tower reboiler, 5-a double-effect evaporation separator, 6 a-a waste alkali liquid double-effect evaporator, 8-a vacuum system, 9-a water condensation tank, 10-a water condensation conveying pump, 12-a waste alkali liquid single-effect evaporator feed pump, 13-a single-effect evaporation separator, 14-a waste alkali liquid single-effect evaporator, 15-a waste alkali liquid circulating pump and 16-a waste alkali liquid pump.
CWS-recirculated cooling water LS-low pressure steam.
Detailed Description
The utility model will be further described with reference to the accompanying drawings, which are not to be construed as limiting the utility model.
The cyclohexane oxidation waste lye evaporation device adopted in the production process of cyclohexanone is shown in figure 2:
the utility model provides a cyclohexane oxidation waste lye evaporation plant in cyclohexanone production process, mainly by the distillation column, distillation column feed preheater, the distillation column condenser, the distillation column reboiler, the two-effect evaporimeter charge pump of waste lye, the two-effect evaporimeter of waste lye, two-effect evaporation separator, two-effect evaporation condenser, two-effect evaporation water condensing tank, vacuum system, the condensate delivery pump, one-effect evaporimeter charge pump of waste lye, one-effect evaporimeter of waste lye, one-effect evaporation separator, one-effect evaporation water condensing tank, the waste lye circulating pump, waste lye pump constitutes, its characterized in that: a waste alkali liquor feeding pipeline is connected with a heated side of a distillation tower feeding preheater, an outlet pipeline of the distillation tower feeding preheater at the heated side is connected with a distillation tower, a vapor phase pipeline of the distillation tower is connected with a distillation tower condenser, a liquid phase pipeline of the distillation tower is connected with a waste alkali liquor dual-effect evaporator feeding pump, a feeding pump outlet pipeline of the waste alkali liquor dual-effect evaporator feeding pump is respectively connected with a distillation tower reboiler and the bottom of a dual-effect evaporation separator, an outlet of the distillation tower reboiler is connected with the distillation tower, a bottom pipeline of the dual-effect evaporation separator is connected with a waste alkali liquor single-effect evaporator feeding pump, a feeding pump outlet pipeline of the waste alkali liquor single-effect evaporator is respectively connected with a single-effect evaporation separator and a heated side of the waste alkali liquor dual-effect evaporator, a heated side outlet of the waste alkali liquor dual-effect evaporator is connected with a dual-effect evaporation separator, a vapor phase pipeline at the top of the dual-effect evaporation separator is connected with a dual-effect evaporation condenser heating side, and a vapor phase outlet at the heating side of the dual-effect evaporation condenser is connected with a vacuum system, the heating side liquid phase outlet of the double-effect evaporation condenser is connected with a double-effect evaporation condensation water tank, the liquid phase outlet of the double-effect evaporation condensation water tank is connected with a condensation water delivery pump, the discharge pipeline decibel at the bottom of the single-effect evaporation separator is connected with an alkali liquor circulating pump and an alkali liquor pump, the outlet of the alkali liquor pump burns waste liquor, the outlet of the alkali liquor circulating pump is connected with a waste alkali liquor one-effect evaporator which is heated, the outlet of the waste alkali liquor one-effect evaporator is connected with a single-effect evaporation separator, the top vapor phase of the single-effect evaporation separator is connected with the heating side inlet of the waste alkali liquor two-effect evaporator, the heating side vapor phase outlet of the double-effect evaporator is connected with an inlet pipeline of the double-effect evaporation condenser, the heating side liquid phase outlet of the double-effect evaporator is connected with a single-effect evaporation condensation water tank, and the outlet of the single-effect evaporation condensation water tank is connected with a double-effect evaporation condensation water tank.
Example 1:
a device for producing 10 ten thousand tons of cyclohexanone by a cyclohexane oxidation method every year and a flow of a waste alkali liquor evaporation device, as shown in figure 2.
The waste alkali liquor from the waste alkali liquor separator enters a distillation tower, the operating pressure of the distillation tower is 101-150KPa.A, the operating temperature is 101-112 ℃, the vapor phase at the top of the distillation tower is condensed to about 45 ℃ by a gas tower condenser, the condensed oil-water mixture returns to a decomposition system to recover cyclohexane, cyclohexanone, cyclohexanol and other organic matters in the waste alkali liquor, the tower bottom liquid of the distillation tower is pressurized by a feed pump of a waste alkali liquor two-effect evaporator, part of the tower bottom liquid is forcibly circulated to a reboiler of the distillation tower and then enters the distillation tower, and the reboiler of the distillation tower is heated by low-pressure steam; and the other part of the residue is sent to a double-effect evaporation separator. The waste alkali liquor secondary-effect evaporator is operated in vacuum, the operating pressure is 30-100KPa.A, the operating temperature is 72-101 ℃, the liquid phase of the secondary-effect evaporation separator is pressurized by a feed pump of the waste alkali liquor primary-effect evaporator, part of the liquid phase is sent to a part of the kettle liquid and sent to the primary-effect evaporation separator, the other part of the liquid phase is forced to circulate to the waste alkali liquor secondary-effect evaporator and then the secondary-effect evaporation separator, the waste alkali liquor secondary-effect evaporator adopts the top vapor phase of the primary-effect evaporation separator for heating, the top vapor phase of the secondary-effect evaporation separator is condensed to about 45 ℃ by a secondary-effect evaporation condenser, the vapor phase is vacuumized by a vacuum system, the condensate is sent to a secondary-effect evaporation condensate tank, and the condensate in the secondary-evaporation condensate tank is sent to other systems for utilization by a condensate conveying pump; the waste alkali liquid one-effect evaporator adopts positive pressure operation, the operation pressure is 101-400KPa.A, the operation temperature is 112-147 ℃, the liquid phase of the one-effect evaporation separator is pressurized by a waste alkali liquid circulating pump and then forcibly circulated to the waste alkali liquid one-effect evaporator and then enters the one-effect evaporation separator, and the waste alkali liquid one-effect evaporator adopts low-pressure steam for heating; the liquid phase of the primary evaporation separator is pressurized by a waste alkali liquor pump and then sent to a waste alkali liquor incineration device; the vapor phase at the top of the first-effect evaporation separator is used as a heating source of the waste alkali liquid double-effect evaporator, the vapor phase condensate enters the first-effect evaporation condensate tank, and the condensate of the first-effect evaporation condensate tank passes through the second-effect evaporation condensate tank by pressure difference.
Compared with the existing device, the waste alkali liquid treatment device can reduce low-pressure steam by about 30 percent, can recover organic substances of cyclohexane, cyclohexanol and cyclohexanone in the waste alkali liquid, and reduces the energy consumption and material consumption of a cyclohexane oxidation device; meanwhile, the device can avoid the scaling phenomenon of the equipment in the operation process, and improve the operation period and the safety of the device.
Example 2:
an annual 10-ten-thousand-ton cyclohexanone device by a cyclohexane oxidation method and a waste alkali liquor evaporation device flow are shown in figure 1.
The waste alkali liquor from the waste alkali liquor separator enters a distillation tower, the distillation tower adopts positive pressure operation, the operation pressure is 105-150KPa.A, the operation temperature is 101-112 ℃, a vapor phase at the top of the distillation tower is condensed to about 45 ℃ by a gas tower condenser, a condensed oil-water mixture returns to a decomposition system to recover organic matters such as cyclohexane, cyclohexanone and cyclohexanol in the waste alkali liquor, a tower bottom liquid of the distillation tower is pressurized by a waste alkali liquor evaporator feed pump, part of the tower bottom liquid is forcibly circulated to a distillation tower reboiler and then enters the distillation tower, the distillation tower reboiler adopts a vapor phase at the top of an evaporation separator to heat, and the other part of the tower bottom liquid is sent to the evaporation separator. The waste alkali evaporator adopts a pressurizing operation, the operating pressure is 200-400KPa.A, the operating temperature is 134-147 ℃, the liquid phase of the evaporation separator is pressurized by a waste alkali circulating pump and then forcibly circulated to the waste alkali evaporator and then enters the evaporation separator, and the waste alkali evaporator adopts low-pressure steam for heating; the liquid phase of the evaporation separator is pressurized by a waste alkali liquor pump and then sent to a waste alkali liquor incineration device; the vapor phase at the top of the evaporation separator is used as a heating source of a reboiler of the distillation tower, and the vapor phase condensate enters a condensate tank.
Compared with the existing waste alkali liquid treatment device, the utility model can reduce low-pressure steam by about 30 percent, can recover organic substances cyclohexane, cyclohexanol and cyclohexanone in the waste alkali liquid, and reduce the energy consumption and material consumption of a cyclohexane oxidation device; meanwhile, the device can avoid the scaling phenomenon of the equipment in the operation process, and improve the operation period and the safety of the device.
Example 3:
a device for producing 10 ten thousand tons of cyclohexanone by the cyclohexane oxidation method every year and a flow of a waste alkali liquor evaporation device, as shown in figure 3.
Waste alkali liquor from a waste alkali liquor separator enters a distillation tower, the distillation tower is operated in vacuum, the pressure is 30-100KPa.A, the operating temperature is 72-101 ℃, a vapor phase at the top of the distillation tower is condensed to about 45 ℃ by a gas tower condenser, the vapor phase is vacuumized by a vacuum system, a condensed oil-water mixture returns to a decomposition system to recover organic matters such as cyclohexane, cyclohexanone and cyclohexanol in the waste alkali liquor, a tower bottom liquid of the distillation tower is pressurized by a feed pump of a waste alkali liquor double-effect evaporator, part of the tower bottom liquid is forcibly circulated to a reboiler of the distillation tower and then enters the distillation tower, and the reboiler of the distillation tower is heated by the vapor phase at the top of the double-effect evaporation separator; and the other part of the residue is sent to a double-effect evaporation separator. The waste alkali liquor secondary-effect evaporator adopts a pressurization operation, the operation pressure is 110-134 KPa.A, the operation temperature is 108-134 ℃, the liquid phase of the secondary-effect evaporation separator is pressurized by a feed pump of the waste alkali liquor primary-effect evaporator, part of the liquid phase is sent to a part of the kettle liquid and sent to the primary-effect evaporation separator, the other part of the liquid phase is forcedly circulated to the secondary-effect evaporation separator behind the waste alkali liquor secondary-effect evaporator, the waste alkali liquor secondary-effect evaporator adopts the top vapor phase of the primary-effect evaporation separator for heating, the top vapor phase of the secondary-effect evaporation separator is used as a heat source of a reboiler of a distillation tower, condensate is sent to a condensate tank, and the condensate of the condensate tank is sent to other systems for utilization by a condensate conveying pump; the waste alkali liquid one-effect evaporator adopts the pressurization operation, the operation pressure is 300-400KPa.A, the operation temperature is 141-147 ℃, the liquid phase of the one-effect evaporation separator is pressurized by a waste alkali liquid circulating pump and then forcibly circulated to the waste alkali liquid one-effect evaporator and then enters the one-effect evaporation separator, and the waste alkali liquid one-effect evaporator adopts the low-pressure steam for heating; the liquid phase of the primary evaporation separator is pressurized by a waste alkali liquor pump and then sent to a waste alkali liquor incineration device; the vapor phase at the top of the first-effect evaporation separator is used as a heating source of the waste alkali liquid double-effect evaporator, and the vapor phase condensate enters the condensate tank.
Compared with the existing waste alkali liquid treatment device, the utility model can reduce low-pressure steam by 50%, can recover organic substances cyclohexane, cyclohexanol and cyclohexanone in the waste alkali liquid, and reduce the energy consumption and material consumption of a cyclohexane oxidation device; meanwhile, the device can avoid the scaling phenomenon of the equipment in the operation process and prolong the operation period of the device.
Claims (10)
1. A cyclohexane oxidation waste alkali liquid evaporation device in a cyclohexanone production process comprises a distillation tower, a distillation tower condenser, a waste alkali liquid evaporator feed pump, a distillation tower reboiler, a condensate tank, an evaporation separator, a waste alkali liquid circulating pump, a waste alkali liquid evaporator and a waste alkali liquid pump; the method is characterized in that: the pipeline from the waste alkali liquor separator is connected with a distillation tower, the tower kettle of the distillation tower is connected with a feed pump of a waste alkali liquor evaporator, and the tower top of the distillation tower is connected with a distillation tower condenser; an outlet of a feed pump of the waste alkali evaporator is respectively connected with an inlet of a reboiler of the distillation tower and an inlet of a circulating pump of the waste alkali, the reboiler of the distillation tower is connected with the distillation tower, an inlet of a heating side of the reboiler of the distillation tower is connected with a vapor phase pipeline at the top of the evaporation separator, and an outlet of the heating side of the reboiler of the distillation tower is connected with a water condensing tank; the waste alkali liquor circulating pump is connected with a waste alkali liquor evaporator, and the waste alkali liquor evaporator is connected with the evaporation separator; the bottom of the evaporation separator is respectively connected with a waste lye circulating pump and a waste lye pump.
2. The device for evaporating cyclohexane oxidation waste lye in the production process of cyclohexanone as claimed in claim 1, characterized in that the heating side vapor phase outlet of the distillation tower reboiler is connected with the distillation tower condenser.
3. A cyclohexane oxidation waste alkali liquid evaporation device in the cyclohexanone production process is composed of a distillation tower, a distillation tower condenser, a waste alkali liquid double-effect evaporator feed pump, a distillation tower reboiler, a double-effect evaporation separator, a waste alkali liquid double-effect evaporator, a double-effect evaporation condenser, a water condensing tank, a waste alkali liquid single-effect evaporator feed pump, a single-effect evaporation separator, a waste alkali liquid single-effect evaporator, a waste alkali liquid circulating pump and a waste alkali liquid pump; the method is characterized in that: the pipeline from the waste alkali liquor separator is connected with a distillation tower, the top vapor phase outlet of the distillation tower is connected with a distillation tower condenser, the tower kettle of the distillation tower is connected with a waste alkali liquor dual-effect evaporator feed pump, the outlet of the waste alkali liquor dual-effect evaporator feed pump is respectively connected with a distillation tower reboiler and a dual-effect evaporation separator, the liquid phase outlet of the dual-effect evaporation separator is connected with a waste alkali liquor single-effect evaporator feed pump, the outlet of the waste alkali liquor single-effect evaporator feed pump is respectively connected with a single-effect evaporation separator and a waste alkali liquor dual-effect evaporator, the waste alkali liquor dual-effect evaporator is connected with a dual-effect evaporation separator, the heating pipeline of the waste alkali liquor dual-effect evaporator is connected with the top vapor phase pipeline of the single-effect evaporation separator, the top vapor phase pipeline of the dual-effect evaporation separator is connected with the dual-effect evaporation condenser, and the condensate outlet of the dual-effect evaporation condenser is connected with a condensate tank; the liquid phase pipeline of the first-effect evaporation separator is connected with the inlet of a waste alkali liquor circulating pump, the outlet of the waste alkali liquor circulating pump is connected with a waste alkali liquor first-effect evaporator, the waste alkali liquor first-effect evaporator is connected with the first-effect evaporation separator, and the liquid phase outlet of the first-effect evaporation separator is also connected with a waste alkali liquor pump; the vapor phase outlet of the heating side of the waste alkali liquor dual-effect evaporator is connected with the dual-effect evaporation condenser, and the vapor phase condensate outlet of the heating side of the waste alkali liquor dual-effect evaporator is connected with the condensate tank.
4. The device for evaporating cyclohexane oxidation waste lye in the process of producing cyclohexanone as claimed in claim 3, characterized in that the vapor phase outlet of said two-effect evaporation condenser is connected with a vacuum system.
5. The device for evaporating cyclohexane oxidation waste lye in the process of producing cyclohexanone as claimed in claim 4 wherein said vacuum system employs a liquid ring pump or a dry vacuum pump.
6. A cyclohexane oxidation waste lye evaporation device in cyclohexanone production process comprises a distillation tower, a distillation tower condenser, a vacuum system, a waste lye double-effect evaporator feed pump, a distillation tower reboiler, a water condensing tank, a double-effect evaporation separator, a waste lye single-effect evaporator feed pump, a waste lye double-effect evaporator, a single-effect evaporation separator, a waste lye circulating pump, a waste lye single-effect evaporator and a waste lye pump; the method is characterized in that: the waste alkali liquor separator pipeline is connected with a distillation tower, a vapor phase outlet at the top of the distillation tower is connected with a distillation tower condenser, the vapor phase outlet of the distillation tower condenser is connected with a vacuum system, a tower kettle of the distillation tower is connected with a feed pump of an alkali liquor double-effect evaporator, a feed pump outlet of the alkali liquor double-effect evaporator is respectively connected with a distillation tower reboiler and a double-effect evaporation separator, the distillation tower reboiler is connected with the distillation tower, and the distillation tower reboiler is connected with the vapor phase pipeline at the top of the double-effect evaporation separator; the liquid phase outlet of the double-effect evaporation separator is connected with the inlet of a feed pump of a waste alkali liquid one-effect evaporator, the outlet of the feed pump of the waste alkali liquid one-effect evaporator is respectively connected with the single-effect evaporation separator and the waste alkali liquid two-effect evaporator, the waste alkali liquid two-effect evaporator is connected with the double-effect evaporation separator, the waste alkali liquid two-effect evaporator and the top vapor phase pipeline of the single-effect evaporation separator, and the condensate outlets of the waste alkali liquid two-effect evaporator and a distillation tower reboiler are connected with a condensate tank; the liquid phase outlet of the first-effect evaporation separator is respectively connected with a waste alkali liquor circulating pump and a waste alkali liquor pump, the waste alkali liquor circulating pump is connected with a waste alkali liquor first-effect evaporator, and the waste alkali liquor first-effect evaporator is connected with the first-effect evaporation separator.
7. The cyclohexane oxidation waste lye evaporating device in the cyclohexanone manufacturing process as claimed in any one of the claims 1, 3 or 6, characterized in that said distillation column is a plate column or a packed column.
8. The device for evaporating cyclohexane oxidation waste lye in the production process of cyclohexanone as claimed in any one of claims 1, 3 or 6 wherein said distillation tower reboiler is a forced circulation type reboiler or a built-in reboiler.
9. The cyclohexane oxidation waste lye evaporating device in the cyclohexanone production process as claimed in any one of the claims 1, 3 or 6, characterized in that said condensate tank is connected with a condensate feed pump.
10. The device for evaporating cyclohexane oxidation waste lye in the production process of cyclohexanone as claimed in claim 6, characterized in that the heating side vapor phase outlet of the distillation tower reboiler is connected with the distillation tower condenser; the heating side vapor phase outlet of the waste alkali liquor double-effect evaporator is connected with the vapor phase pipeline of the double-effect evaporation separator.
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