CN104671304B - Comprehensive utilization method for gas-phase latent heat at top of rectifying tower - Google Patents
Comprehensive utilization method for gas-phase latent heat at top of rectifying tower Download PDFInfo
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- CN104671304B CN104671304B CN201510016043.3A CN201510016043A CN104671304B CN 104671304 B CN104671304 B CN 104671304B CN 201510016043 A CN201510016043 A CN 201510016043A CN 104671304 B CN104671304 B CN 104671304B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
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Abstract
The invention relates to a comprehensive utilization method for gas-phase latent heat at the top of a rectifying tower. The comprehensive utilization method comprises the steps of (1) delivering alkaline liquid and wastewater generated in aniline black production to the top of the rectifying tower after being mixed through a static mixer, meanwhile, directly enabling steam to enter from the bottom of the rectifying tower to carry out steam stripping on the wastewater, and treating the wastewater generated at the bottom of the tower after steam stripping in a sewage plant; (2) condensing a gas-phase mixture generated at the top of the tower in a lithium bromide unit condenser; meanwhile, enabling 12-DEG C water to enter the lithium bromide unit condenser, and enabling the lithium bromide unit condenser to form 7-DEG C water for refrigerating under the drive of gas-phase latent heat generated by the gas-phase mixture; and (3) changing the gas-phase mixture condensed by the lithium bromide unit condenser into a liquid-phase mixture, layering by using a layering device after condensing through a first condenser and a second condenser, returning a water phase at the upper layer to the static mixer to circularly carry out the step (1), and returning aniline at the lower layer to a production process to recycle. According to the comprehensive utilization method, the gas-phase latent heat at the top of the rectifying tower is sufficiently utilized, and the economic benefit is remarkable.
Description
Technical field
The present invention relates to technical field of dye, specifically, relate to the comprehensive utilization of a kind of rectifying tower top gaseous phase latent heat
Method.
Background technology
Nigrosine is a kind of chemistry dyestuff, and its strong coloring force, dispersibility are low, light absorptive good, color steadiness high, therefore
Nigrosine can be used for plastic resin coloring, ink colorant, and wood decoration technique colours, leather, cotton, fiber crops dyeing and covering with paint, metal
The field such as color articles and pigment coloration.
The waste water containing aniline can be produced in nigrosine production process, if directly discharge is very big to environmental hazard,
But also the wasting of resources can be caused.During utilizing rectifying column to extract aniline, rectifying column top can produce the benzene of uniform flow
Amine steam and steam, in terms of per hour, the most uniformly produce aniline steam and the steam of 5310kg, this part gaseous mixture
Phase component contains substantial amounts of gas-phase potential heat, and its top gaseous phase latent heat is calculated as follows:
Known: 100 DEG C of water vapour enthalpys are: 2677KJ/Kg；The enthalpy of 100 DEG C of water is: 417.5KJ/Kg；Aniline enthalpy of vaporization is:
487.335KJ/Kg。
The gas-phase potential heat that rectifying column tower top produces per hour is:
Latent+Q the water of Q always latent=Q aniline is dived
Q water is dived=0.84 × 5310 × (2677-417.5)=10078274KJ
Q aniline is dived=0.16 × 6000 × 487.335=414040KJ
Q always latent=10078274+414040=10492314KJ
I.e. overhead vapours phase transformation produces latent heat 10492314KJ per hour, equivalent 249.8 ten thousand kilocalories.
Visible, the aniline steam of rectifying column tower top generation and the gaseous mixture phase component of steam are dived containing substantial amounts of gas phase
Heat, needs to carry out cooling and processes ability aniline recovery.Conventional method is to utilize circulating water cooling or aerial condenser cooling, as
Fig. 1 discloses the schematic flow sheet of a kind of aniline distillation recovery device, and the waste water in storage tank 1 contains aniline about 4%, pre-through charging
Sending into the tower top of rectifying column 3 after the preheating of hot device 2, live steam is directly entered from the bottom of the tower of rectifying column 3, carries out containing aniline waste water
Stripping, waste water at the bottom of tower is discharged after reclaiming preheating by feed preheater 2, is sent biochemical processing process.Tower top high concentration aniline steam
The condensed device of mixture 4 condenses to about 40 DEG C and enters aniline, the decker 5 of water, and upper strata aqueous phase contains a small amount of aniline, sends back to
Storage tank 1 circulation distillation is to reclaim aniline therein, and lower floor's aniline can recycle mutually.The most not only can waste substantial amounts of circulation
Water, and this partial heat also can not get effectively utilizing, thus cause the waste of this partial heat, economic loss is bigger.
" recovery of alcohol soluble nigrosine production Aniline " [Wang Shouheng, etc. alcohol soluble nigrosine produces Aniline
Reclaim [J], 2009,30 (3): 48-50] have also been devised the device of a kind of improvement, as in figure 2 it is shown, containing about 4% give up containing aniline
Water elevator pump 11 is squeezed in pipe-line mixer, adds in Caustic soda and regulation is to certain pH value, filter through manganese sand filter 12 and remove
Entering the storage tank 1 of neutralizer after ferric chloride, the aniline water in storage tank 1 is with the boosting of aniline water pump and at the shell of feed preheater 2
After journey is preheating to 90 DEG C by overhead vapours, send into the charging of rectifying column 3 tower top.Enter with waste water from rectifying column 3 tower top steam out
Material heat exchange, after uncooled steam entrance air cooler 15 is cooled to 60 DEG C, is mixed into cold with the condensation liquid phase of feed preheater 2
Condenser 4 continues to be cooled to about 40 DEG C, and the material after process send the decker 5 of aniline, water, and equally, upper strata aqueous phase sends storage back to
Tank 1 circulation distillation is to reclaim aniline therein, and lower floor's aniline recycles in reaction process as raw material.Rectifying column 3
Waste water at the bottom of tower first delivers to flash tank 14, then utilizes ejector 13 that waste water saturated in flash tank 14 is carried out vacuum flashing, to return
Receive heat, discharge again after reclaiming preheating.But utilize air cooler condensation not make full use of tower top aniline steam
With the gas-phase potential heat of steam, thus cause and waste substantial amounts of heat.
In view of this, the special proposition present invention.
Summary of the invention
It is an object of the invention to provide the method for comprehensive utilization of a kind of rectifying tower top gaseous phase latent heat, the method is the most sharp
With aniline steam and the gas-phase potential heat of water vapour of rectifying tower top, utilize low-pressure steam to drive lithium bromide chiller condenser, produce 7
Degree cold water freezes for other workshops, makes the heat of rectifying column tower top comprehensively be effectively utilized, and economic benefit is obvious.
For realizing the purpose of the present invention, the present invention adopts the following technical scheme that
The method of comprehensive utilization of a kind of rectifying tower top gaseous phase latent heat, wherein, described method of comprehensive utilization includes as follows
Step:
1) by alkali liquor and nigrosine production process produce mix by static mixer containing aniline waste water after, send into smart
Evaporating column overhead, steam is directly entered from the bottom of rectifying tower simultaneously, strips containing aniline waste water, produces after stripping at the bottom of rectifying tower
Raw waste water is decontaminated water factory and office reason after heat exchanger heat exchange；
2) rectifying column tower top produces aniline and the gas phase mixture of water enter the condensation of lithium bromide chiller condenser；Simultaneously 12
DEG C recirculated water enters lithium bromide chiller condenser, and the gas-phase potential heat produced by the gas phase mixture of aniline and water drives lithium bromide
Train condenser forms 7 DEG C of recirculated waters and is converted into 12 DEG C of recirculated waters after using enters back into lithium bromide chiller for refrigeration, refrigeration
Condenser recycles；
3) gas phase mixture through the condensation of lithium bromide chiller condenser becomes liquid phase mixture, passes sequentially through the first condenser
Condensing with the second condenser, be layered subsequently into decker, upper strata aqueous phase contains a small amount of aniline, sends back to static mixed
Clutch circulation carry out step 1) operation；Lower floor's aniline recycles as the raw material return production technology of synthesis nigrosine.
At present, the aniline steam of rectifying column tower top generation and the gaseous mixture phase component of water vapour are dived containing substantial amounts of gas phase
Heat, needs to carry out cooling and processes ability aniline recovery.Conventional method is to utilize circulating water cooling or aerial condenser cooling, this
Sample not only can waste substantial amounts of recirculated water, and this partial heat also can not get effectively utilizing, thus causes this partial heat
Waste, economic loss is bigger.
The present invention effectively utilizes aniline steam and the gas-phase potential heat of water vapour of rectifying tower top, utilizes low-pressure steam to drive bromine
Change lithium train condenser, produce 7 degree of cold water and freeze for each workshop, through each workshop reacting kettle jacketing or heat exchanger heat exchange
After be converted into the water of 12 degree, then after low-pressure steam drives lithium bromide chiller, produce the water recycling of 7 degree, so circulate, shape
Becoming 7 DEG C of recirculated waters and 12 DEG C of recirculated waters, make the heat of rectifying column tower top comprehensively be effectively utilized, economic benefit is obvious.With
Time, the aniline of recovery can return production technology as the raw material of nigrosine and recycle.
In method of comprehensive utilization of the present invention, wherein, step 1) in the percent mass of Aniline containing aniline
It is 3～8% than content, preferably 4%；The mass percentage content of the Aniline produced at the bottom of tower is ＜ 300ppm.
Step 2) in the temperature of gas phase mixture of aniline and water be 102～104 DEG C.
Step 3) in the temperature of liquid phase mixture be 95～100 DEG C.
Step 3) described in liquid phase mixture sequentially pass through the first condenser and the second condenser and condense to 20～25 DEG C
Rear entrance decker is layered.
Step 3) in lower floor's aniline mutually in the mass percentage content of aniline be 94～98%.
It is connected with cold on described lithium bromide chiller condenser, the first described condenser and the second condenser respectively
But water feed pipe and CWR.
The downside of described rectifying column is provided with condensation-water drain.
In the present invention, the steam condensate that steam produces after heat exchange at the bottom of rectifying tower flows out from this condensation-water drain.
The method of comprehensive utilization economic benefit using rectifying tower top gaseous phase latent heat provided by the present invention is obvious, by rectification
Tower top produces 5310Kg low-pressure steam per hour, replaces 0.6MPa steam drive lithium bromide chiller to produce 7 DEG C of cool water quantities and is
500m3/ h, supply workshop refrigeration needs.Steam expense per ton presses 200 yuan of calculating, and the whole year can steam saving expense about 7,650,000.
The method of comprehensive utilization of rectifying tower top gaseous phase latent heat provided by the present invention passes through aniline provided by the present invention
In black production process, the comprehensive utilization device of gas-phase potential heat realizes.
The comprehensive utilization device of gas-phase potential heat in described nigrosine production process, including rectifying column, condenser and layering
Device, wherein, is connected with lithium bromide chiller condenser, described lithium bromide between described rectifying column and described condenser
Train condenser is provided with recirculated water entrance and circulating water outlet.
At present, the aniline steam of rectifying column tower top generation and the gaseous mixture phase component of water vapour are dived containing substantial amounts of gas phase
Heat, needs to carry out cooling and processes ability aniline recovery.Conventional method is to utilize circulating water cooling or aerial condenser cooling, this
Sample not only can waste substantial amounts of recirculated water, and this partial heat also can not get effectively utilizing, thus causes this partial heat
Waste, economic loss is bigger.
The present invention effectively utilizes aniline steam and the gas-phase potential heat of water vapour of rectifying tower top, utilizes low-pressure steam to drive bromine
Change lithium train condenser, produce 7 DEG C of water and freeze for each workshop, after each workshop reacting kettle jacketing or heat exchanger heat exchange
It is converted into 12 DEG C of water, produces 7 DEG C of water after entering back into the condensation of lithium bromide chiller condenser and recycle, make the heat of rectifying column tower top
Comprehensively being effectively utilized, economic benefit is obvious.Meanwhile, containing aniline waste water through rectifying column stripping, lithium bromide chiller condenser
The aniline reclaimed after condensation, condenser condensation and decker layering can return production technology circulation profit as the raw material of nigrosine
With.
In order to improve condensation effect further, condenser of the present invention includes the first condenser and the second condenser,
The first described condenser and the second condenser are connected in turn between described lithium bromide chiller condenser and decker.
Further, described lithium bromide chiller condenser is provided with aniline steam entry and aniline water out；Described
Aniline steam entry be connected by the tower top of pipeline with described rectifying column；Described aniline water out by pipeline with
The first described condenser is connected.
Preferably, the upside of described rectifying column is also connected with being provided with static mixer.
Further, one end of described static mixer is provided with alkali liquor inlet and the entrance Han aniline waste water, the other end with
The upside of described rectifying column is connected.
The original ph of the mother solution containing aniline waste water is acid, and aniline is presented in hydrochlorate, by rectifying column
Upside connect a static mixer be set, make mother solution containing aniline waste water mix from entering static mixer containing aniline waste water entrance
Closing, add liquid caustic soda mixing by alkali liquor inlet simultaneously and be neutralized in static mixer, after neutralization, aniline is by anilinechloride
Form be converted into aniline, consequently facilitating rectification.
In the present invention, the downside of described rectifying column is provided with steam inlet and condensation-water drain.
Live steam steam inlet on the downside of rectifying column is directly entered, and strips containing aniline waste water, strips heat exchange
The steam condensate of rear generation flows out from described condensation-water drain.
In the present invention, on described lithium bromide chiller condenser, the first described condenser and the second condenser respectively
It is connected with cooling water supply pipe and CWR.
As a preferred embodiment of the present invention, at the bottom of the tower of rectifying column of the present invention, it is connected with heat exchanger.
Containing heat from waste water out at the bottom of rectifying tower, if directly sending sewage treatment plant to process, will result in this part
The waste of heat.The present invention arranges a heat exchanger in connection at the bottom of rectifying tower, and at the bottom of such tower, waste water is collected by heat exchanger heat exchange
Enter back into sewage treatment plant after heat to process, thus avoid the waste of waste water heat at the bottom of tower.
Compared with prior art, present invention have the advantage that
(1) method of comprehensive utilization of rectifying tower top gaseous phase latent heat provided by the present invention can effectively process aniline black byestuffs
Waste water, it is achieved the resource of pollutant and the cleaning of nigrosine produce, and the removal of aniline can reduce the poison to biochemical wastewater treatment
Evil, realizes qualified discharge for sewage farm and provides premise；Meanwhile, the aniline of recovery can return as the raw material of nigrosine
Production. art of bringing back to life recycles；
(2) method of comprehensive utilization of rectifying tower top gaseous phase latent heat provided by the present invention effectively utilizes the benzene of rectifying tower top
Amine steam and the gas-phase potential heat of steam, utilize low-pressure steam to drive lithium bromide chiller condenser, produces 7 degree of cold water for each workshop
Refrigeration uses, and is converted into the water of 12 degree, then drives through low-pressure steam after each workshop reacting kettle jacketing or heat exchanger heat exchange
Produce the water recycling of 7 degree after lithium bromide chiller, make the heat of rectifying column tower top comprehensively be effectively utilized, economic benefit
Substantially.
Accompanying drawing explanation
Fig. 1 is the structural representation of the aniline distillation recovery device of prior art；
Fig. 2 is the structural representation of the aniline distillation recovery device that prior art is improved；
Fig. 3 is the comprehensive utilization schematic diagram of rectifying tower top gaseous phase latent heat provided by the present invention；
Wherein, in accompanying drawing, each component names is as follows:
1 storage tank, 2 feed preheaters, 3 rectifying columns, 4 condensers, 41 first condensers,
42 second condensers, 5 deckers, 6 lithium bromide chiller condensers, 7 static mixers, 8 change
Hot device, 9 cooling water supply pipes, 10 CWRs, 11 elevator pumps, 12 manganese sand filter,
13 ejectors, 14 flash tanks, 15 air coolers.
Detailed description of the invention
Be below the detailed description of the invention of the present invention, described embodiment be in order to further describe the present invention rather than
Limit the present invention.
Embodiment 1
1) as it is shown on figure 3, by alkali liquor and nigrosine production process produce aniline content be 4wt% containing aniline waste water
After being mixed by static mixer 7, sending into rectifying column 3 tower top, steam is directly entered from the bottom of rectifying column 3 tower simultaneously, to containing aniline
Waste water strips, and the waste water produced at the bottom of rectifying column 3 tower after stripping is decontaminated water factory and office reason after heat exchanger 8 heat exchange；Wherein, at the bottom of tower
The mass percentage content of the Aniline produced is less than 300ppm, and the consumption of alkali liquor is 1075Kg/h；
2) rectifying column 3 tower top produces the aniline that temperature is 102 DEG C and the gas phase mixture entrance lithium bromide chiller of water are cold
Condenser 6 condenses；12 DEG C of recirculated waters enter lithium bromide chiller condenser 6 simultaneously, are produced by the gas phase mixture of aniline and water
Gas-phase potential heat drives lithium bromide chiller condenser 6 to form 7 DEG C of recirculated waters and is converted into 12 DEG C of circulations for refrigeration, refrigeration after using
Water enters back into lithium bromide chiller condenser 6 and recycles；
3) gas phase mixture through lithium bromide chiller condenser 6 condensation becomes the liquid phase mixture of 95 DEG C, passes sequentially through the
One condenser 41 and the second condenser 42 condense, and condense after 20 DEG C entrance decker 5 and are layered, and upper strata aqueous phase contains
Have a small amount of aniline, send back to static mixer 7 circulation carry out step 1) operation；Lower floor's aniline is mutually as the raw material of synthesis nigrosine
Return production technology recycles；Wherein the content of lower floor's aniline middle aniline mutually is 94wt%.
Connect respectively on described lithium bromide chiller condenser 6, the first described condenser 41 and the second condenser 42
It is provided with cooling water supply pipe 9 and CWR 10.
Embodiment 2
1) as it is shown on figure 3, by alkali liquor and nigrosine production process produce aniline content be 3wt% containing aniline waste water
After being mixed by static mixer 7, sending into rectifying column 3 tower top, steam is directly entered from the bottom of rectifying column 3 tower simultaneously, to containing aniline
Waste water strips, and the waste water produced at the bottom of rectifying column 3 tower after stripping is decontaminated water factory and office reason after heat exchanger 8 heat exchange；Wherein, at the bottom of tower
The mass percentage content of the Aniline produced is less than 300ppm, and the consumption of alkali liquor is 1075Kg/h；
2) rectifying column 3 tower top produces the aniline that temperature is 104 DEG C and the gas phase mixture entrance lithium bromide chiller of water are cold
Condenser 6 condenses；12 DEG C of recirculated waters enter lithium bromide chiller condenser 6 simultaneously, are produced by the gas phase mixture of aniline and water
Gas-phase potential heat drives lithium bromide chiller condenser 6 to form 7 DEG C of recirculated waters and is converted into 12 DEG C of circulations for refrigeration, refrigeration after using
Water enters back into lithium bromide chiller condenser 6 and recycles；
3) gas phase mixture through lithium bromide chiller condenser 6 condensation becomes the liquid phase mixture of 100 DEG C, passes sequentially through the
One condenser 41 and the second condenser 42 condense, and condense after 25 DEG C entrance decker 5 and are layered, and upper strata aqueous phase contains
Have a small amount of aniline, send back to static mixer 7 circulation carry out step 1) operation；Lower floor's aniline is mutually as the raw material of synthesis nigrosine
Return production technology recycles；Wherein the content of lower floor's aniline middle aniline mutually is 98wt%.
Connect respectively on described lithium bromide chiller condenser 6, the first described condenser 41 and the second condenser 42
It is provided with cooling water supply pipe 9 and CWR 10.
Embodiment 3
1) as it is shown on figure 3, by alkali liquor and nigrosine production process produce aniline content be 8wt% containing aniline waste water
After being mixed by static mixer 7, sending into rectifying column 3 tower top, steam is directly entered from the bottom of rectifying column 3 tower simultaneously, to containing aniline
Waste water strips, and the waste water produced at the bottom of rectifying column 3 tower after stripping is decontaminated water factory and office reason after heat exchanger 8 heat exchange；Wherein, at the bottom of tower
The mass percentage content of the Aniline produced is less than 300ppm, and the consumption of alkali liquor is 1075Kg/h；
2) rectifying column 3 tower top produces the aniline that temperature is 103 DEG C and the gas phase mixture entrance lithium bromide chiller of water are cold
Condenser 6 condenses；12 DEG C of recirculated waters enter lithium bromide chiller condenser 6 simultaneously, are produced by the gas phase mixture of aniline and water
Gas-phase potential heat drives lithium bromide chiller condenser 6 to form 7 DEG C of recirculated waters and is converted into 12 DEG C of circulations for refrigeration, refrigeration after using
Water enters back into lithium bromide chiller condenser 6 and recycles；
3) gas phase mixture through lithium bromide chiller condenser 6 condensation becomes the liquid phase mixture of 98 DEG C, passes sequentially through the
One condenser 41 and the second condenser 42 condense, and condense after 23 DEG C entrance decker 5 and are layered, and upper strata aqueous phase contains
Have a small amount of aniline, send back to static mixer 7 circulation carry out step 1) operation；Lower floor's aniline is mutually as the raw material of synthesis nigrosine
Return production technology recycles；Wherein the content of lower floor's aniline middle aniline mutually is 96wt%.
Connect respectively on described lithium bromide chiller condenser 6, the first described condenser 41 and the second condenser 42
It is provided with cooling water supply pipe 9 and CWR 10.
Embodiment 4
1) as it is shown on figure 3, by alkali liquor and nigrosine production process produce aniline content be 5wt% containing aniline waste water
After being mixed by static mixer 7, sending into rectifying column 3 tower top, steam is directly entered from the bottom of rectifying column 3 tower simultaneously, to containing aniline
Waste water strips, and the waste water produced at the bottom of rectifying column 3 tower after stripping is decontaminated water factory and office reason after heat exchanger 8 heat exchange；Wherein, at the bottom of tower
The mass percentage content of the Aniline produced is less than 300ppm, and the consumption of alkali liquor is 1075Kg/h；
2) rectifying column 3 tower top produces the aniline that temperature is 102 DEG C and the gas phase mixture entrance lithium bromide chiller of water are cold
Condenser 6 condenses；12 DEG C of recirculated waters enter lithium bromide chiller condenser 6 simultaneously, are produced by the gas phase mixture of aniline and water
Gas-phase potential heat drives lithium bromide chiller condenser 6 to form 7 DEG C of recirculated waters and is converted into 12 DEG C of circulations for refrigeration, refrigeration after using
Water enters back into lithium bromide chiller condenser 6 and recycles；
3) gas phase mixture through lithium bromide chiller condenser 6 condensation becomes the liquid phase mixture of 96 DEG C, passes sequentially through the
One condenser 41 and the second condenser 42 condense, and condense after 20 DEG C entrance decker 5 and are layered, and upper strata aqueous phase contains
Have a small amount of aniline, send back to static mixer 7 circulation carry out step 1) operation；Lower floor's aniline is mutually as the raw material of synthesis nigrosine
Return production technology recycles；Wherein the content of lower floor's aniline middle aniline mutually is 97wt%.
Connect respectively on described lithium bromide chiller condenser 6, the first described condenser 41 and the second condenser 42
It is provided with cooling water supply pipe 9 and CWR 10.
Embodiment 5
This embodiment on the basis of embodiment 1, embodiment 2, embodiment 3 or embodiment 4 further in described rectification
The downside of tower arranges a condensation-water drain.It is easy to steam condensate that steam produces after heat exchange at the bottom of the tower of rectifying column 3 from this condensation
Water out flows out.
The method of comprehensive utilization of the rectifying tower top gaseous phase latent heat described in above-described embodiment passes through benzene provided by the present invention
In amido black production process, the following comprehensive utilization device of gas-phase potential heat realizes.
The comprehensive utilization device of gas-phase potential heat in described nigrosine production process, as it is shown on figure 3, include rectifying column 3, cold
Condenser 4 and decker 5, wherein, be connected with lithium bromide chiller condensation between described rectifying column 3 and described condenser 4
Device 6, described lithium bromide chiller condenser 6 is provided with recirculated water entrance and circulating water outlet.The present invention effectively utilizes rectifying column 3
The aniline steam of tower top and the gas-phase potential heat of water vapour, utilize low-pressure steam to drive lithium bromide chiller condenser 6, produce 7 DEG C of water
Freeze for each workshop, after each workshop reacting kettle jacketing or heat exchanger heat exchange, be converted into 12 DEG C of water, enter back into bromination
Produce 7 DEG C of water after lithium train condenser 6 condensation to recycle, make the heat of rectifying column 3 tower top comprehensively be effectively utilized, warp
Ji benefit is obvious.Meanwhile, strip through rectifying column 3 containing aniline waste water, lithium bromide chiller condenser 6 condenses, condenser 4 condenses and divides
The aniline reclaimed after bed device 5 layering can return production technology as the raw material of nigrosine and recycle.
In order to improve condensation effect further, condenser 4 of the present invention includes the first condenser 41 and the second condensation
Device 42, the first described condenser 41 and the second condenser 42 are connected to described lithium bromide chiller condenser 6 and layering in turn
Between device 5.
Described lithium bromide chiller condenser 6 is provided with aniline steam entry and aniline water out；Described aniline water
Steam inlet is connected by the tower top of pipeline with described rectifying column 3；Described aniline water out passes through pipeline with described
First condenser 41 is connected.
The upside of described rectifying column 3 is connected with static mixer 7.
One end of described static mixer 7 is provided with alkali liquor inlet and the entrance Han aniline waste water, the other end and described essence
The upside evaporating tower 3 is connected.
The original ph of the mother solution containing aniline waste water is acid, and aniline is presented in hydrochlorate, by rectifying column
Upside connect a static mixer be set, make mother solution containing aniline waste water mix from entering static mixer containing aniline waste water entrance
Closing, add liquid caustic soda mixing by alkali liquor inlet simultaneously and be neutralized in static mixer, after neutralization, aniline is by anilinechloride
Form be converted into aniline, consequently facilitating rectification.
The downside of described rectifying column 3 is provided with steam inlet and condensation-water drain.
Live steam steam inlet on the downside of rectifying column is directly entered, and strips containing aniline waste water, strips heat exchange
The steam condensate of rear generation flows out from described condensation-water drain.
Connect respectively on described lithium bromide chiller condenser 6, the first described condenser 41 and the second condenser 42
It is provided with cooling water supply pipe 9 and CWR 10.
Comparative example
The method of the present invention and the method for prior art being contrasted, the oldest device is the device of Fig. 1, improvement
Device is the device of Fig. 2.Result see table shown in 1:
Table 1, the new and old device of prior art contrast with the major economic indicators of the method for the present invention
On the one hand the method for comprehensive utilization of rectifying tower top gaseous phase latent heat provided by the present invention effectively utilizes rectifying tower top
Aniline steam and the gas-phase potential heat of steam, utilize low-pressure steam to drive lithium bromide chiller condenser, produce the confessions of 7 degree cold water respectively
Other workshops refrigeration uses, and is converted into the water of 12 degree after each workshop reacting kettle jacketing or heat exchanger heat exchange, then through low pressure
Produce the water recycling of 7 degree after steam drive lithium bromide chiller, make the heat of rectifying column tower top comprehensively be effectively utilized,
Economic benefit is obvious.Produce 5310Kg low-pressure steam by rectifying tower top per hour, replace 0.6MPa steam drive lithium bromide chiller
Producing 7 DEG C of cool water quantities is 500m3/ h, supply workshop refrigeration needs.Steam expense per ton presses 200 yuan of calculating, can save steaming the whole year
Vapour expense about 7,650,000.On the other hand, compared with the device of old device and improvement, use the method for comprehensive utilization of the present invention significantly
Reduce the consumption of recirculated water.
Claims (9)
1. the method for comprehensive utilization of a rectifying tower top gaseous phase latent heat, it is characterised in that described method of comprehensive utilization includes
Following steps:
1) by alkali liquor and nigrosine production process produce containing aniline waste water by static mixer (7) mix after, send into essence
Evaporating tower (3) tower top, steam is directly entered from the bottom of rectifying column (3) tower simultaneously, strips the waste water containing aniline, rectification after stripping
The waste water produced at the bottom of tower (3) tower is decontaminated water factory and office reason after heat exchanger (8) heat exchange；
2) rectifying column (3) tower top produces aniline and the gas phase mixture of water enter lithium bromide chiller condenser (6) condensation；Simultaneously
12 DEG C of recirculated waters enter lithium bromide chiller condenser (6), and the gas-phase potential heat produced by the gas phase mixture of aniline and water is driven
Lithium bromide chiller condenser (6) forms 7 DEG C of recirculated waters and is converted into 12 DEG C of recirculated waters after using enters back into bromine for refrigeration, refrigeration
Change lithium train condenser (6) to recycle；
3) gas phase mixture condensed through lithium bromide chiller condenser (6) becomes liquid phase mixture, passes sequentially through the first condenser
(41) and the second condenser (42) condenses, and is layered subsequently into decker (5), and upper strata aqueous phase contains a small amount of benzene
Amine, send back to static mixer (7) circulation carry out step 1) operation；Lower floor's aniline is mutually as the raw material return life of synthesis nigrosine
Production. art recycles.
Method of comprehensive utilization the most according to claim 1, it is characterised in that step 1) in containing the matter of aniline in aniline waste water
Amount degree is 3～8%；The mass percentage content ＜ 300ppm of the Aniline produced at the bottom of tower.
Method of comprehensive utilization the most according to claim 2, it is characterised in that step 1) in containing the matter of aniline in aniline waste water
Amount degree is 4%.
4. according to the method for comprehensive utilization described in Claims 2 or 3, it is characterised in that step 2) in the gas phase of aniline and water mix
The temperature of compound is 102～104 DEG C.
Method of comprehensive utilization the most according to claim 4, it is characterised in that step 3) in the temperature of liquid phase mixture be 95
～100 DEG C.
6. according to the method for comprehensive utilization described in claim 1 or 2 or 3 or 5, it is characterised in that step 3) described in liquid phase
Mixture sequentially passes through the first condenser (41) and the second condenser (42) condenses after 20～25 DEG C entrance decker (5) and enters
Row layering.
Method of comprehensive utilization the most according to claim 6, it is characterised in that step 3) in lower floor's aniline mutually in the matter of aniline
Amount degree is 94～98%.
Method of comprehensive utilization the most according to claim 7, it is characterised in that described lithium bromide chiller condenser (6), institute
Cooling water supply pipe (9) and cooling water backwater it is connected with respectively on the first condenser (41) stated and the second condenser (42)
Pipe (10).
Method of comprehensive utilization the most according to claim 8, it is characterised in that the downside of described rectifying column (3) is provided with cold
Solidifying water out.
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| CN110559677A (en) * | 2019-09-25 | 2019-12-13 | 南通百川新材料有限公司 | Efficient trimethylolpropane synthetic solvent rectification tail gas recovery device |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004026753A (en) * | 2002-06-27 | 2004-01-29 | Mitsui Takeda Chemicals Inc | Method for recovering organic substance from waste water containing methylene-bridged polyarylpolyamine |
| CN201476314U (en) * | 2009-07-31 | 2010-05-19 | 宜兴市前成生物有限公司 | Comprehensive utilizing device for waste heat produced during fumaric acid production |
| CN101973595A (en) * | 2010-10-11 | 2011-02-16 | 徐州瑞赛科技实业有限公司 | Method for processing organic wastewater by azeotropy-steam distillation |
| CN101987816A (en) * | 2009-07-31 | 2011-03-23 | 宜兴市前成生物有限公司 | Waste heat comprehensive utilization device during the production process of fumaric acid |
| US8697913B2 (en) * | 2009-06-17 | 2014-04-15 | Huntsman International Llc | Chemical installation |
| CN203687472U (en) * | 2014-01-10 | 2014-07-02 | 河北冀衡赛瑞化工有限公司 | Cooling device in ammonium nitrate production device |
| WO2014170250A1 (en) * | 2013-04-18 | 2014-10-23 | Bayer Materialscience Ag | Method for reprocessing wastewater from nitrobenzene production |
-
2015
- 2015-01-13 CN CN201510016043.3A patent/CN104671304B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004026753A (en) * | 2002-06-27 | 2004-01-29 | Mitsui Takeda Chemicals Inc | Method for recovering organic substance from waste water containing methylene-bridged polyarylpolyamine |
| US8697913B2 (en) * | 2009-06-17 | 2014-04-15 | Huntsman International Llc | Chemical installation |
| CN201476314U (en) * | 2009-07-31 | 2010-05-19 | 宜兴市前成生物有限公司 | Comprehensive utilizing device for waste heat produced during fumaric acid production |
| CN101987816A (en) * | 2009-07-31 | 2011-03-23 | 宜兴市前成生物有限公司 | Waste heat comprehensive utilization device during the production process of fumaric acid |
| CN101973595A (en) * | 2010-10-11 | 2011-02-16 | 徐州瑞赛科技实业有限公司 | Method for processing organic wastewater by azeotropy-steam distillation |
| WO2014170250A1 (en) * | 2013-04-18 | 2014-10-23 | Bayer Materialscience Ag | Method for reprocessing wastewater from nitrobenzene production |
| CN203687472U (en) * | 2014-01-10 | 2014-07-02 | 河北冀衡赛瑞化工有限公司 | Cooling device in ammonium nitrate production device |
Non-Patent Citations (2)
| Title |
|---|
| "废水处理中苯胺回收装置的节能研究";马连湘等;《现代化工》;20080131;第28卷(第1期);第73页 1原流程简介、2流程改造 * |
| "醇溶苯胺黑生产废水中苯胺的回收";王守恒.等;《化学工业与工程技术》;20090630;第30卷(第3期);第49页1 原回收装置简介，2中和-过滤-恒沸精馏回收工艺，图1-2 * |
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