CN115212600A - Energy-conserving high-efficient type cyclohexanone refined system - Google Patents
Energy-conserving high-efficient type cyclohexanone refined system Download PDFInfo
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- CN115212600A CN115212600A CN202211008352.2A CN202211008352A CN115212600A CN 115212600 A CN115212600 A CN 115212600A CN 202211008352 A CN202211008352 A CN 202211008352A CN 115212600 A CN115212600 A CN 115212600A
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- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 title claims abstract description 82
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 104
- 150000002576 ketones Chemical class 0.000 claims abstract description 77
- 238000007670 refining Methods 0.000 claims abstract description 18
- 238000010992 reflux Methods 0.000 claims description 76
- 239000007789 gas Substances 0.000 claims description 52
- 239000012071 phase Substances 0.000 claims description 49
- 230000018044 dehydration Effects 0.000 claims description 39
- 238000006297 dehydration reaction Methods 0.000 claims description 39
- 239000007791 liquid phase Substances 0.000 claims description 29
- 238000009833 condensation Methods 0.000 claims description 16
- 230000005494 condensation Effects 0.000 claims description 16
- 239000007792 gaseous phase Substances 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 3
- 238000005065 mining Methods 0.000 claims 1
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 abstract description 36
- 239000000463 material Substances 0.000 abstract description 36
- 239000002699 waste material Substances 0.000 abstract description 10
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 36
- 239000003921 oil Substances 0.000 description 15
- 238000000034 method Methods 0.000 description 14
- 238000001816 cooling Methods 0.000 description 13
- 230000008569 process Effects 0.000 description 12
- -1 alcohol ketone Chemical class 0.000 description 10
- 239000007788 liquid Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 238000009835 boiling Methods 0.000 description 4
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 description 4
- 238000006356 dehydrogenation reaction Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses an energy-saving efficient cyclohexanone refining system, which belongs to the technical field of cyclohexanone refining and processing, and aims to solve the problems of poor conversion rate and serious energy consumption loss in the production process of cyclohexanone, and comprises an alcohol tower, a light component removing tower, a ketone tower and an alcohol tower, wherein a light component tower II is arranged between the light component removing tower and the ketone tower, the input end of the alcohol tower is connected with an alcohol tower reboiler, and the gas phase output end of the alcohol tower is connected with an alcohol tower condensing unit; according to the invention, the added light second tower C-52807 recovers cyclohexanol and cyclohexanone materials in the top of the light component removal tower C-52802, and in the tower bottom materials of the alcohol tower C-52804, cyclohexanol is extracted from the side line of the alcohol tower C-52804, so that cyclohexanol can be easily extracted from the middle part of the tower, a large amount of cyclohexanol can be easily separated from tower bottom heavy components, the purity of cyclohexanol is increased, the waste of the tower bottom cyclohexanol materials is also saved, and finally, the cyclohexanol and cyclohexanone materials are well recovered, and the waste of a large amount of materials is reduced.
Description
Technical Field
The invention belongs to the technical field of cyclohexanone refining processing, and particularly relates to an energy-saving and efficient cyclohexanone refining system.
Background
The process adopts benzene to add hydrogen to generate cyclohexene, the conversion rate is 40% -50%, the cyclohexene is added with water to generate cyclohexanol, the conversion rate is 8% -10%, the cyclohexanol is dehydrogenated to generate cyclohexanone and hydrogen, the conversion rate is 40% -50%, because the conversion rate of a series of production units of the process is not 100% and is accompanied with the generation of a large amount of byproducts, each reaction system is provided with a corresponding refining unit to obtain a high-purity product, and finally the high-purity cyclohexanone product is obtained; but the existing materials and heat are both wasted and can not be recycled, and the equipment runs for a long time to cause serious loss.
Referring to fig. 1, the process of the present cyclohexanone refining production system is as follows: firstly, feeding an alcohol ketone mixed material into a dehydration tower (C-52801), removing water in reaction liquid, feeding the alcohol ketone mixture with water removed from the bottom of the C-52801 tower into a lightness-removing tower (C-52802) by pressurizing through a pump when the temperature of the tower bottom reaches the boiling point of water, removing light component impurities generated by reaction, preventing the content of the light component impurities in a final product from exceeding the standard and influencing the product quality, feeding medium-pressure steam into a reboiler (E-52801) of the tower bottom to heat the material in the tower, so that the material with lower boiling point (light component) is removed from the top of the lightness-removing tower C-52802, feeding the material into overhead condensers to cool (E-52802 and E-52803) by utilizing the relative volatility difference of each material component in the alcohol ketone mixed liquid, wherein the condensers use circulating water and chilled water as cooling media, the cooled light component flows into a condensate recovery tank (V-52802), and the light component discharged from a reflux tank V-52802 serves as waste oil, and is discharged to a lightness-removing tank area, and the temperature of the lightness-125 ℃ of the lightness-52801 area of the lightness-125 ℃ of the light component-52801-removing tower top; after the water and light components are removed, an alcohol-ketone mixture is pressurized by a mechanical pump (P-52801) from the tower bottom of the light component removal tower and then is sent into a ketone tower C-52803, at the moment, a material entering the ketone tower C-52803 reaches the refining and separating effect by medium-pressure steam in the tower bottom and liquid phase reflux at the tower top, a high-quality cyclohexanone final product is separated from the top of the ketone tower C-52803, a residual material at the tower bottom of the ketone tower C-52803 is sent into an alcohol tower C-52804 to separate cyclohexanol, and because the cyclohexanol and the residual component have higher boiling points, the high-pressure steam is used as a heating heat source in the alcohol tower C-52804, the cyclohexanol is removed from the tower top, is sent to a cyclohexanol reaction system for recycling after condensation and cooling, and a heavy component with a higher boiling point in the tower bottom of the alcohol tower C-52804 is pressurized by the mechanical pump (P-52807) and then is used as waste oil to be discharged.
Adopt above-mentioned cyclohexanone refining production system, it has following defect:
(1) the process ketone tower C-52803 uses medium pressure steam as a heating source, wherein the medium pressure steam pressure is as follows: 1.1MPaG, temperature: medium-pressure steam is introduced from a reboiler (E-52808) at the bottom of the ketone tower C-52803 at 200 ℃, and the medium-pressure steam consumed by the ketone tower C-52803 at full load is about 18t/h; there are cases where the steam loss is large;
(2) the medium-pressure steam has high pressure, so that the equipment of a reboiler (E-52808) of the ketone tower is seriously washed, and the equipment of the reboiler is easily damaged and leaked;
(3) the heat brought by the light components at the top of the lightness-removing column C-52802 is directly cooled for the first time by a circulating water heat exchanger (E-52805 and E-52806), and the chilled water is cooled for the second time, so that the heat loss and the consumption of the circulating water and the chilled water are large;
(4) the cyclohexanol and cyclohexanone content at the top of the light component removal tower (C-52802) are high, and the loss is large;
(5) the cyclohexanol content in the tower bottom of the alcohol tower (C-52804) is high, and much waste is discharged as waste oil.
Therefore, an energy-saving and efficient cyclohexanone refining system is needed, and the problems of poor conversion rate and serious energy consumption loss in the cyclohexanone production process in the prior art are solved.
Disclosure of Invention
The invention aims to provide an energy-saving and efficient cyclohexanone refining system to solve the problems in the background technology.
In order to achieve the purpose, the invention provides the following technical scheme: the utility model provides an energy-conserving high-efficient type cyclohexanone refining system, includes alcohol tower, lightness-removing tower, ketone tower and alcohol tower, lightness-removing tower with be provided with light second tower between the ketone tower, the input of alcohol tower is connected with alcohol tower reboiler, the gaseous phase output of alcohol tower is connected with alcohol tower condensing unit, the liquid phase output of alcohol tower with lightness-removing tower's input is connected, lightness-removing tower's input is connected with lightness-removing tower reboiler, lightness-removing tower's gaseous phase output with be provided with lightness-removing tower condensation reflux unit between the light second tower, lightness-removing tower's liquid phase output with be connected with lightness-removing tower discharge pump between the input of ketone tower, the input of one side of ketone tower is connected with ketone tower reboiler A, the gaseous phase output of ketone tower with be connected with light second tower condensation recovery unit between the gaseous phase output of lightness-removing tower, the liquid phase output of light second tower with the input of lightness-removing tower is connected with light second tower discharge pump, one side input of ketone tower is connected with the gaseous phase condensation output, alcohol tower's lateral line input is connected with alcohol tower reboiler, the alcohol tower output is connected with alcohol tower reflux unit.
What need explain in the scheme is, dehydration tower condensing unit include with the dehydration tower condenser that the gaseous phase output of dehydration tower is connected, the gaseous phase output of dehydration tower condenser is connected with dehydration tower tail-cooling ware, dehydration tower condenser with the liquid phase output of dehydration tower tail-cooling ware is connected with dehydration tower reflux drum jointly, the bottom of dehydration tower reflux drum is connected with dehydration tower reflux drum drain pump.
It should be further noted that the condensation reflux unit of the light component removal tower is connected with a light component removal tower condenser connected with the gas phase output end of the light component removal tower, the gas phase output end of the light component removal tower condenser is connected with a light component removal tower tail cooler, the light component removal tower condenser and the liquid phase output end of the light component removal tower tail cooler are jointly connected with a light component removal tower reflux tank, and the output end of the light component removal tower reflux tank and the top reflux end of the light component removal tower are connected with a light component removal tower reflux pump.
It should be further noted that the light second tower condensation and recovery unit includes a light second tower condenser connected to a gas phase output end of the light second tower, a light second tower tail cooler is connected to a gas phase output end of the light second tower condenser, a light second tower reflux tank is connected to liquid phase output ends of the light second tower condenser and the light second tower tail cooler, and a light second tower reflux pump is connected to an output end of the light second tower reflux tank and a top reflux end of the light second tower.
In a preferred embodiment, the side draw unit comprises a ketone column reboiler B connected to an input of a bottom side of the ketone column, the output of the gas phase of the light component removal column is connected to an input of the ketone column reboiler, the output of the liquid phase of the ketone column is connected to an input of a bottom of the ketone column reboiler B, and the output of a side of the ketone column reboiler B is connected to an input of the reflux drum of the light component removal column.
As a preferred embodiment, the alcohol tower condensation reflux unit comprises an alcohol tower condenser connected with the gas phase output end of the alcohol tower, the gas phase output end of the alcohol tower condenser is connected with an alcohol tower tail cooler, the alcohol tower condenser and the liquid phase output end of the alcohol tower tail cooler are connected with an alcohol tower reflux tank, and the alcohol tower reflux tank is connected with the top reflux end of the alcohol tower.
In a preferred embodiment, the output end of the middle part of the alcohol tower is connected with an alcohol tower side-collecting pump, and the liquid phase output end of the alcohol tower is connected with an alcohol tower discharging pump.
Compared with the prior art, the energy-saving and high-efficiency cyclohexanone refining system provided by the invention at least has the following beneficial effects:
(1) Under the action of two reboilers of a ketone tower reboiler (E-52808A/B), a gas phase heat source at the top of the light component removal tower is recovered, and low-pressure steam with the pressure of 0.5MPaG is used as a heating heat source instead of the ketone tower C-52803, so that about 18t/h of medium-pressure steam can be saved.
(2) The low-pressure steam has lower pressure than the medium-pressure steam, and the washing damage to the equipment in long-term production is greatly improved after the low-pressure steam is used in the reboiler (E-52808A/B) of the ketone tower instead of the original medium-pressure steam.
(3) The reboiler (E-52808A/B) of the ketone tower uses the gas phase at the top of the lightness-removing tower as a heat source, exchanges heat with the cold material at the bottom of the ketone tower (C-52803), the cold material passes through the tube layer of the reboiler, the gas phase at the top of the lightness-removing tower serves as a hot material, and passes through the shell layer of the reboiler, after the gas phase at the top of the lightness-removing tower C-52802 is cooled by using the material at the bottom of the ketone tower C-52803 as a cooling medium, compared with the prior art, the gas phase at the top of the lightness-removing tower directly enters the heat exchanger at the top of the tower for gas phase cooling, the heat exchanger at the top of the tower uses circulating water and chilled water as cooling media, the temperature difference between the cold material and the hot material is large, so that the cooling media are evaporated and lost, the return temperature of the circulating water and the chilled water is increased, the cooling effect is reduced, and the consumption of the circulating water and the chilled water is greatly saved.
(4) The added light second tower C-52807 is used for recovering cyclohexanol and cyclohexanone materials in the top of the light component removal tower C-52802, and in the materials in the tower bottom of the alcohol tower C-52804, cyclohexanol is extracted from the side line of the alcohol tower C-52804, so that cyclohexanol can be easily extracted from the middle of the tower, a large amount of cyclohexanol can be easily separated from heavy components in the tower bottom, the purity of cyclohexanol is increased, waste of cyclohexanol materials in the tower bottom is saved, and finally, the cyclohexanol and cyclohexanone materials are well recovered, and waste of a large amount of materials is reduced.
Drawings
FIG. 1 is a schematic diagram of a conventional cyclohexanone refining process;
FIG. 2 is a schematic view of the cyclohexanone refining process of the present invention.
Detailed Description
The present invention will be further described with reference to the following examples.
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be described clearly and completely with reference to the drawings of the embodiments of the present invention, and it is obvious that the described embodiments are some embodiments of the present invention, but not all embodiments, and all other embodiments obtained by a person of ordinary skill in the art without creative work based on the described embodiments of the present invention belong to the protection scope of the present invention.
The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention. The conditions in the embodiments may be further adjusted according to specific conditions, and simple modifications of the method of the present invention based on the concept of the present invention are all within the scope of the present invention as claimed.
Referring to fig. 2, the present invention provides an energy-saving efficient cyclohexanone refining system, including an alcohol tower, a light component removal tower, a ketone tower and an alcohol tower, wherein a light component removal tower is arranged between the light component removal tower and the ketone tower, an input end of the alcohol tower is connected with an alcohol tower reboiler, a gas phase output end of the alcohol tower is connected with an alcohol tower condensing unit, a liquid phase output end of the alcohol tower is connected with an input end of the light component removal tower, an input end of the light component removal tower is connected with the light component removal tower reboiler, a light component removal tower condensing reflux unit is arranged between a gas phase output end of the light component removal tower and the light component removal tower, a light component removal tower discharge pump is connected between a liquid phase output end of the light component removal tower and an input end of the ketone tower, a side line input end of the ketone tower is connected with a light component removal reboiler, a liquid phase output end of the ketone tower is connected with an input end of the alcohol tower, a side line input end of the ketone tower is connected with a side line output end of the light component removal tower reboiler, a liquid phase output end of the ketone tower is connected with an input end of the alcohol tower, and a side line output end of the light component removal tower is connected with a light component removal tower reboiler.
It is worth specifically saying that the condensing unit of the dehydration tower includes a condenser of the dehydration tower connected to the gas phase output end of the dehydration tower, the gas phase output end of the condenser of the dehydration tower is connected to the tail cooler of the dehydration tower, the condenser of the dehydration tower and the liquid phase output end of the tail cooler of the dehydration tower are jointly connected to a reflux tank of the dehydration tower, and the bottom end of the reflux tank of the dehydration tower is connected to a drain pump of the reflux tank of the dehydration tower.
It is worth specifically saying that the condensation reflux unit of the lightness-removing column is connected with a lightness-removing column condenser at the gas phase output end of the lightness-removing column, the gas phase output end of the lightness-removing column condenser is connected with a lightness-removing column tail cooler, the lightness-removing column condenser and the liquid phase output end of the lightness-removing column tail cooler are jointly connected with a lightness-removing column reflux tank, and the output end of the lightness-removing column reflux tank and the top reflux end of the lightness-removing column are connected with a lightness-removing column reflux pump.
The light second tower condensation and recovery unit comprises a light second tower condenser connected with the gas phase output end of the light second tower, the gas phase output end of the light second tower condenser is connected with a light second tower tail cooler, the light second tower condenser and the liquid phase output end of the light second tower tail cooler are jointly connected with a light second tower reflux tank, and the output end of the light second tower reflux tank and the top reflux end of the light second tower are connected with a light second tower reflux pump.
It is worth specifically saying that the side draw unit comprises a ketone tower reboiler B connected with an input end on one side of the bottom of the ketone tower, a gas phase output end of the lightness-removing tower is connected with an input end of the ketone tower reboiler, a liquid phase output end of the ketone tower is connected with an input end on the bottom of the ketone tower reboiler B, and an output end on one side of the ketone tower reboiler B is connected with an input end of a reflux tank of the lightness-removing tower.
It is worth specifically saying that the alcohol tower condensation reflux unit comprises an alcohol tower condenser which is connected with the alcohol tower condensation unit and comprises a gas phase output end of the alcohol tower, the gas phase output end of the alcohol tower condenser is connected with an alcohol tower tail cooling device, the alcohol tower condenser and a liquid phase output end of the alcohol tower tail cooling device are jointly connected with an alcohol tower reflux tank, and the alcohol tower reflux tank is connected with a top reflux end of the alcohol tower.
It is worth specifying that the output end of the middle part of the alcohol tower is connected with an alcohol tower side-extracting pump, and the liquid phase output end of the alcohol tower is connected with an alcohol tower discharging pump.
The specific process flow in the scheme is as follows: crude alcohol ketone from a dehydrogenation product pump P-52701A/B enters the top of a dehydrating tower C-52801, medium-pressure steam with the pressure of 1.1MPa is used as a heat source for a dehydrating tower reboiler E-52801, and condensate is collected to a condensate tank V-52811 of the dehydrating tower reboiler and then is sent to a condensate header pipe for recycling by pressure difference; the micro-positive pressure operation of a dehydration tower C-52801 is carried out, the gas phase at the top of the tower is cooled and condensed by circulating water and chilled water through a dehydration tower condenser E-52802 and a dehydration tower tail cooler E-52803 respectively, noncondensable gas is discharged to a torch by pressure, the condensate flows into a dehydration tower reflux tank V-52801 by the difference of the pressure, the water phase and the oil phase in the dehydration tower reflux tank V-52801 are subjected to oil-water separation by sedimentation for a period of time, the bottom water phase is sent to V-52904 by a dehydration tower reflux tank drainage pump P-52809A/B for water phase recovery, the upper oil phase is sent to a dehydrogenation pump tank V-52705 by a pump P-52802A/B for oil phase recovery, the residue liquid of the dehydration tower C-52801 is sent to a light-weight removal tower C-52802 by a dehydration tower discharge pump P-52801A/B, the light-weight removal tower C-52802 is operated under negative pressure, and the vacuum pump set X-52301 is used for pumping under negative pressure to maintain the negative pressure operation; the reboiler E-52804 uses 1.1MPa medium pressure steam as a heat source, and the condensate is collected to a condensate tank V-52812 of a reboiler of the light component removal tower and then is sent to a condensate header pipe for recycling by pressure difference; gas phase light oil and alcohol ketone evaporated from the tower top firstly exchange heat with tower bottom liquid of a ketone tower C-52803 through a ketone tower reboiler E-52808B, then sequentially enter a lightness-removing tower condenser E-52805 and a lightness-removing tower tail cooler E-52806 and are respectively cooled and condensed by circulating water and chilled water, condensate flows into a lightness-removing tower reflux tank V-52802, and noncondensable gas is pumped and discharged to a process gas main pipe by a vacuum device X-52301; the oil in the dehydrogenation tower reflux tank V-52802 is pressurized by a light component removal tower reflux pump P-52804A/B, one part returns to the top of the light component removal tower to be refluxed, a small amount of light oil and alcohol ketone are sent to a light second tower C-52802, the alcohol ketone mixed solution from the light component removal tower reflux tank V-52802 enters the light second tower C-52807, the light second tower C-52807 is operated under negative pressure and shares a set of vacuum device with the light component removal tower C-52802; the reboiling E-52823 of the light second tower uses 1.1MPa medium-pressure steam as a heat source, and condensate is sent to a condensate header pipe through a steam trap for recycling; the light components evaporated from the tower top sequentially enter a light second tower condenser E-52824 and a light second tower tail cooler E-52825 to be cooled and condensed by circulating water and chilled water respectively, condensate flows into a light second tower reflux tank V-52808, and non-condensable gas is pumped and discharged to a process gas main pipe by a vacuum device X-52301; the light component in the light second tower reflux tank V-52808 returns to the light second tower as reflux through a light second tower reflux pump P-52821A/B, and part of the light component is sent to a heat-conducting oil furnace system or a light oil tank in a middle tank area as fuel oil; the bottom liquid of the light second tower C-52807 is sent to a light component removal tower C-52802 from the bottom of the tower through a light second tower discharge pump P-52803A/B; the bottom liquid of the light component removal tower C-52802 is sent to the middle part of a ketone tower C-52803 from the bottom of the tower by a discharge pump P-52803A/B of the light component removal tower; the ketone tower C-52803 is operated under negative pressure, the vacuum device X-52302A/B is used for vacuumizing and maintaining the negative pressure operation, medium and low pressure steam is used as a heat source for a ketone tower reboiler E-52808A, condensate is collected to a condensate tank V-52813 of the ketone tower reboiler and is sent to a condensate header pipe by pressure difference for recycling, and the gas phase at the top of the light component removal tower C-52802 is used as the heat source for the ketone tower reboiler E-52808B; cyclohexanone steam distilled from the top of the ketone tower C-52803 sequentially enters a ketone tower condenser E-52809A/B and a ketone tower tail gas cooler E-52810 and is cooled and condensed by circulating water and chilled water respectively, condensate flows into a ketone tower reflux tank V-52803, and noncondensable gas is vacuumized and X-52302A/B and is pumped and discharged to a process gas main pipe; feeding cyclohexanone in the reflux V-52803 of the ketone tower out by a ketone tower reflux pump P-52806A/B, returning part of the cyclohexanone to the top of the ketone tower C-52803 as reflux, cooling part of the cyclohexanone by circulating water of a cyclohexanone cooler E-52811, and feeding the cooled cyclohexanone to a boundary area external cyclohexanone finished product tank or a crude alcohol ketone returning cooler and then feeding the cyclohexanone to a middle tank area crude alcohol ketone tank; the bottom product of the ketone tower C-52803 is sent to the middle lower part of an alcohol tower C-52804 through a ketone tower discharge pump P-52805A/B, the alcohol tower C-52804 is operated under negative pressure, and shares a set of vacuum device X-52302A/B with the ketone tower C-52803; the alcohol tower reboiling E-52812 uses 2.5MPa high-pressure steam as heat source steam condensate to be collected in a condensate tank V-52814 of an alcohol tower reboiler and is sent to a condensate header pipe by pressure difference for recycling; alcohol ketone and a small amount of light components evaporated from the tower top sequentially enter an alcohol tower condenser E-52815 and an alcohol tower tail cooler E-52816 to be cooled and condensed by circulating water, condensate flows into an alcohol tower reflux tank V-52804, and noncondensable gas is pumped and discharged to a process gas main pipe by a vacuum device X-52302A/B; a liquid loading device is arranged in the middle of the alcohol tower C-52804 to collect high-purity cyclohexanol, and the high-purity cyclohexanol is sent to a dehydrogenation reaction unit through an alcohol tower side sampling pump P-52823A/B; cyclohexanol in the alcohol tower reflux tank V-52804 is sent out by an alcohol tower reflux pump P-52808A/B, most of cyclohexanol is returned to the top of the alcohol tower C-52804 as reflux, and a small part of cyclohexanol is sent to a light component removal tower C-52802 or a purification tower C-52205 to remove accumulated light components; the bottom liquid of the alcohol tower C-52804 is pumped out from the tower bottom by an alcohol tower discharge pump P-5287A/B and is sent to an X oil tank D-91005 in a middle tank area.
According to the above, it can be seen that: (1) under the action of two reboilers of a ketone tower reboiler (E-52808A/B), a gas-phase heat source at the top of the light component removal tower is recovered, and low-pressure steam with the pressure of 0.5MPaG is used as a heating heat source instead of the ketone tower C-52803, so that about 18t/h of medium-pressure steam can be saved;
(2) the low-pressure steam has lower pressure than the medium-pressure steam, and the washing damage to equipment in long-term production is greatly improved after the original medium-pressure steam is changed into the low-pressure steam in a ketone tower reboiler (E-52808A/B);
(3) the method comprises the following steps that a reboiler (E-52808A/B) of a ketone tower uses a gas phase at the top of a lightness-removing tower as a heat source at present, heat is exchanged with a cold material at the bottom of the ketone tower (C-52803), the cold material flows through a tube layer of the reboiler, the gas phase at the top of the lightness-removing tower serves as a hot material and a shell layer of the reboiler, the gas phase at the top of the lightness-removing tower C-52802 is cooled by using the material at the bottom of the ketone tower C-52803 as a cooling medium, and then the gas phase directly enters a tower top heat exchanger for gas phase cooling compared with the gas phase at the top of the lightness-removing tower in the original process, the temperature difference between the cold and hot materials is large, so that the cooling medium is evaporated and lost, the return water temperature of circulating water and chilled water is increased, the cooling effect is reduced, and the loss of the circulating water and the chilled water is greatly saved;
(4) the added light second tower C-52807 recovers cyclohexanol and cyclohexanone materials in the top of the light component removal tower C-52802, because the light oil at the top of the light component removal tower C-52802 has a large content of cyclohexanol and cyclohexanone materials, if the light oil is directly discharged as light oil, a large amount of cyclohexanol and cyclohexanone materials are lost; in the materials in the C-52804 tower bottom of the alcohol tower, the cyclohexanol is extracted from the C-52804 side line of the alcohol tower, so that the cyclohexanol can be easily extracted from the middle of the tower, a large amount of cyclohexanol can be easily separated from heavy components in the tower bottom, the purity of the cyclohexanol is increased, the waste of the cyclohexanol materials in the tower bottom is saved, the cyclohexanol and cyclohexanone materials are well recovered finally, and the waste of a large amount of materials is reduced.
Unless defined otherwise, technical or scientific terms used herein should be construed as commonly understood by one of ordinary skill in the art, and the use of the term "comprising" or "including" and the like in the present invention means that the element or item preceding the term covers the element or item listed after the term and its equivalents, but does not exclude other elements or items, and the term "connected" or "connected" and the like are not limited to physical or mechanical connections, but may also include electrical connections, whether direct or indirect, "upper", "lower", "left", "right", and the like, are used merely to indicate relative positional relationships, and when the absolute position of the object being described is changed, the relative positional relationships may be changed accordingly.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. The utility model provides an energy-conserving high-efficient type cyclohexanone refined system, includes alcohol tower, lightness-removing tower, ketone tower and alcohol tower, its characterized in that, lightness-removing tower with be provided with light second tower between the ketone tower, the input of alcohol tower is connected with alcohol tower reboiler, the gaseous phase output of alcohol tower is connected with alcohol tower condensing unit, the liquid phase output of alcohol tower with lightness-removing tower's input is connected, lightness-removing tower's input is connected with lightness-removing tower reboiler, lightness-removing tower's gaseous phase output with be provided with lightness-removing tower condensation reflux unit between the light second tower, lightness-removing tower's liquid phase output with be connected with lightness-removing tower discharge pump between the input of ketone tower, lightness-removing tower's liquid phase output with lightness-removing tower's input is connected with light second tower discharge pump, one side input of ketone tower is connected with ketone tower reboiler A, the opposite side input of ketone tower with be connected with light second tower condensation recovery unit between the gaseous phase output of lightness-removing tower, light second tower's liquid phase output with lightness-removing tower's input is connected with light second tower discharge pump, one side input is connected with alcohol tower output, alcohol tower output is connected with alcohol tower reboiler unit, the input is connected with alcohol tower reflux.
2. The energy-saving and efficient cyclohexanone refining system according to claim 1, wherein: the condensing unit of the dehydration tower comprises a dehydration tower condenser connected with the gas phase output end of the dehydration tower, the gas phase output end of the dehydration tower condenser is connected with a dehydration tower tail cooler, the dehydration tower condenser and the liquid phase output end of the dehydration tower tail cooler are jointly connected with a dehydration tower reflux tank, and the bottom end of the dehydration tower reflux tank is connected with a dehydration tower reflux tank drainage pump.
3. The energy-saving and efficient cyclohexanone refining system according to claim 2, wherein: the condensation reflux unit of the light component removal tower is connected with a light component removal tower condenser at the gas phase output end of the light component removal tower, the gas phase output end of the light component removal tower condenser is connected with a light component removal tower tail cooler, and the output end of the light component removal tower reflux tank and the top reflux end of the light component removal tower are connected with a light component removal tower reflux pump.
4. The system of claim 3, wherein the system is further characterized in that: the light second tower condensation and recovery unit comprises a light second tower condenser connected with the gas phase output end of the light second tower, the gas phase output end of the light second tower condenser is connected with a light second tower tail cooler, the light second tower condenser and the liquid phase output end of the light second tower tail cooler are jointly connected with a light second tower reflux tank, and the output end of the light second tower reflux tank and the top reflux end of the light second tower are connected with a light second tower reflux pump.
5. The system of claim 4, wherein the system comprises: the side draw unit comprises a ketone tower reboiler B connected with the input end of one side of the bottom of the ketone tower, the gas phase output end of the lightness-removing tower is connected with the input end of the ketone tower reboiler, the liquid phase output end of the ketone tower is connected with the input end of the bottom of the ketone tower reboiler B, and the output end of one side of the ketone tower reboiler B is connected with the input end of the reflux tank of the lightness-removing tower.
6. The energy-saving and efficient cyclohexanone refining system according to claim 5, wherein: the alcohol tower condensation reflux unit comprises an alcohol tower condenser connected with the gas phase output end of the alcohol tower, the gas phase output end of the alcohol tower condenser is connected with an alcohol tower tail cooler, the alcohol tower condenser is connected with the liquid phase output end of the alcohol tower tail cooler together with an alcohol tower reflux tank, and the alcohol tower reflux tank is connected with the top reflux end of the alcohol tower.
7. The system of claim 6, wherein the system is further characterized by: the middle output end of the alcohol tower is connected with an alcohol tower side-mining pump, and the liquid phase output end of the alcohol tower is connected with an alcohol tower discharging pump.
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| CN202211008352.2A CN115212600A (en) | 2022-08-22 | 2022-08-22 | Energy-conserving high-efficient type cyclohexanone refined system |
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| CN202211008352.2A CN115212600A (en) | 2022-08-22 | 2022-08-22 | Energy-conserving high-efficient type cyclohexanone refined system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115382233A (en) * | 2021-05-25 | 2022-11-25 | 山东洪达化工有限公司 | Cyclohexanone rectification device and method |
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