CN112023430B - Decoking method of chlorobenzene rectifying still liquid - Google Patents
Decoking method of chlorobenzene rectifying still liquid Download PDFInfo
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- CN112023430B CN112023430B CN201910476524.0A CN201910476524A CN112023430B CN 112023430 B CN112023430 B CN 112023430B CN 201910476524 A CN201910476524 A CN 201910476524A CN 112023430 B CN112023430 B CN 112023430B
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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
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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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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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
- B01D3/42—Regulation; Control
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- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
- C07C17/386—Separation; Purification; Stabilisation; Use of additives by distillation with auxiliary compounds
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Abstract
The invention provides a method for decoking chlorobenzene rectifying still liquid, which aims to solve the problems of equipment corrosion, organic matter loss or generation of a large amount of wastewater in the prior art. And (2) continuously distilling the black chlorobenzene rectifying still liquid under normal pressure, separating a water phase and an oil phase in a water separator after the gas phase is condensed, refluxing the water phase into the distilling still, reserving a certain volume of oil phase in the water separator, wherein the discharged oil phase is the decoked chlorobenzene rectifying still liquid, and the decoked chlorobenzene rectifying still liquid is clear in appearance. The invention has no decomposition of the polychlorobenzene during the distillation process, and can not cause corrosion to relevant equipment; the loss of chlorobenzene, p-dichlorobenzene and o-dichlorobenzene under the reduced pressure condition is avoided, the cost of vacuum tail gas reprocessing is reduced, and the pollution of VOCs to the atmosphere is reduced; no waste water is generated, and the production cost of enterprises can be reduced.
Description
Technical Field
The invention belongs to the technical field of chemical separation, and particularly relates to a decoking method of chlorobenzene rectifying still liquid.
Background
The chlorobenzene is mainly used as an intermediate and a solvent for dyes, medicines, pesticides and organic synthesis. At present, benzene chloride is produced by adopting a tower-type boiling continuous chlorination process in China, benzene and chlorine are subjected to substitution reaction under the action of a catalyst to generate benzene chloride and hydrogen chloride gas, a liquid-phase product is subjected to washing, neutralization and separation and then is rectified to obtain a finished product of benzene chloride and rectifying still liquid (a byproduct, namely, mixed dichlorobenzene), and a gas-phase product is absorbed by adding water to prepare a byproduct, namely hydrochloric acid. The chlorobenzene rectifying still liquid (byproduct mixed dichlorobenzene) accounts for 3.0-3.5% (wt.%) of the chlorobenzene yield, wherein the chlorobenzene content is less than or equal to 17% (wt.%), the paradichlorobenzene content is greater than or equal to 45% (wt.%), the ortho-dichlorobenzene content is less than or equal to 32% (wt.%), the polychlorobenzene content is less than or equal to 1% (wt.%), and in addition, tar, ferric trichloride and ferric hydroxide are contained. The appearance of the chlorobenzene rectifying still liquid (byproduct mixed dichlorobenzene) is black.
The utilization of the chlorobenzene distillation still liquid (byproduct mixed dichlorobenzene) generally separates and extracts three organic matters of chlorobenzene, p-dichlorobenzene and o-dichlorobenzene, but the subsequent separation and extraction work is very difficult due to the existence of tar, ferric hydroxide and the like, so that the mixed dichlorobenzene must be pretreated to remove impurities such as tar, ferric hydroxide and the like. The method commonly used in the industry at present is that the chlorobenzene rectifying still liquid (byproduct mixed dichlorobenzene) is distilled under reduced pressure to remove tar and heavy components, and then chlorobenzene, p-dichlorobenzene and o-dichlorobenzene are extracted; the vacuum degree during reduced pressure distillation is 0.08 MPa-0.09 MPa, the kettle temperature is 120-130 ℃, the tower top temperature is 90-110 ℃, and the decoking method of reduced pressure distillation has two problems: (1) under the vacuum condition, the chlorobenzene, the p-dichlorobenzene and the o-dichlorobenzene in the byproduct mixed dichlorobenzene can be partially taken away in vacuum, the taken away organic gas accounts for 0.60% (wt.%) -0.65% (wt.%) of the treatment capacity of the byproduct mixed dichlorobenzene, and if the vacuum gas is directly emptied, the atmospheric pollution is caused, and if the vacuum gas is further treated, the production cost is increased; (2) under the condition that the temperature of a distillation kettle exceeds 120 ℃, the polychlorobenzene is easy to decompose to generate HCl gas, and if only trace moisture exists in a system, serious corrosion to equipment can be caused, particularly serious corrosion to a condenser at the top of the tower. Chlor-alkali industry [2001 (8): 20-21 report the separation method of by-product mixed dichlorobenzene, and the pure mixed dichlorobenzene can be separated by directly heating with steam in a stripping tower, but no specific process operation condition is given, and a large amount of waste water is generated in the separation process.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method for decoking chlorobenzene rectifying still liquid, which aims to solve the problems of equipment corrosion, organic matter loss or large amount of waste water generation in the prior art.
In order to solve the problems, the technical scheme of the invention is that the decoking method of the chlorobenzene rectifying still liquid is characterized in that continuous steam distillation is carried out on the chlorobenzene rectifying still liquid under normal pressure.
The method of the invention comprises the following steps:
(1) adding chlorobenzene rectifying still liquid and water in a certain mass ratio into a distillation kettle in advance before starting continuous water vapor distillation, and heating materials in the kettle at normal pressure to boil the materials;
(2) the boiling kettle liquid generates steam, the steam flows into a water separator after being condensed, and a water phase and an oil phase are separated from the water separator;
(3) refluxing the water phase into a distillation kettle, discharging the oil phase at the bottom of the water separator, reserving a certain volume of oil phase in the water separator, and discharging the oil phase which is the decoking chlorobenzene rectifying kettle liquid;
(4) pumping chlorobenzene rectifying still liquid into the distilling still while discharging oil phase from the bottom of the water separator;
(5) the tar in the still was discharged periodically.
Further, the mass ratio of the chlorobenzene rectifying still liquid to water in the step (1) is 1.5-5: 1; further preferably, the mass ratio of the chlorobenzene rectifying still liquid to the water is 2.5: 1.
the temperature of the heat medium in the steps (1) and (2) is 135-; further preferably, the temperature of the heating medium is 140-145 ℃, the temperature of the kettle is 101-105 ℃, and the temperature of the gas phase is 88-98 ℃.
The volume ratio of the oil phase to the water phase in the water separator in the step (3) is 0.1-10: 1, further preferably, the volume ratio of the oil phase to the water phase in the water separator is 1-5: 1.
and (4) pumping the chlorobenzene rectifying still liquid in unit time in the step (4) and discharging the oil phase from the bottom of the water separator in unit time in the same volume.
And (5) discharging tar in the distillation kettle periodically, wherein the tar is deposited at the bottom of the distillation kettle due to high specific gravity and can be discharged by a kettle bottom valve.
Compared with the prior art, the invention has the beneficial effects that:
(1) the byproduct mixed dichlorobenzene after decoking is clear, no polychlorinated benzene is decomposed in the distillation process, and the corrosion to related equipment is avoided;
(2) the loss of chlorobenzene, p-dichlorobenzene and o-dichlorobenzene under the reduced pressure condition is avoided, the cost of vacuum tail gas reprocessing is reduced, and the pollution of VOCs to the atmosphere is reduced;
(3) no waste water is generated, and the production cost of enterprises can be reduced.
Drawings
FIG. 1 is a schematic diagram of an experimental apparatus for decoking of chlorinated benzene rectifying still liquid in the embodiment of the invention.
Detailed Description
The present invention will be described in detail below with reference to examples and the accompanying drawings.
The following example method employs an experimental set-up as shown in figure 1.
Example 1
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 533g of water, heating the oil at 145 ℃, heating at normal pressure, wherein the temperature of the still is 101 ℃, and the temperature of the gas phase is 90 ℃. The oil phase and the water phase are layered in the water separator after the gas phase is condensed, and the water phase flows back into the distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 1: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is transparent and clear. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 2
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 533g of water, heating the oil at 145 ℃, heating at normal pressure, wherein the temperature of the still is 102 ℃, and the temperature of the gas phase is 92 ℃. The oil phase and the water phase are layered in the water separator after the gas phase is condensed, and the water phase flows back into the distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 2: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is transparent and clear. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 3
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 533g of water, heating the oil at 145 ℃, heating at normal pressure, wherein the temperature of the still is 102 ℃, and the temperature of the gas phase is 94 ℃. The oil phase and the water phase are layered in the water separator after the gas phase is condensed, and the water phase flows back into the distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 4: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is transparent and clear. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 4
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 320g of water, heating the oil to 145 ℃, heating at normal pressure, wherein the temperature of the still is 104 ℃, and the temperature of the gas phase is 92 ℃. The oil phase and the water phase are layered in the water separator after the gas phase is condensed, and the water phase flows back into the distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 1: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is transparent and clear. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 5
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 320g of water, heating the oil at 145 ℃, heating at normal pressure, wherein the temperature of the still is 103 ℃, and the temperature of the gas phase is 92 ℃. The oil phase and the water phase are layered in the water separator after the gas phase is condensed, and the water phase flows back into the distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 2: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is transparent and clear. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 6
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 320g of water, heating the oil to 145 ℃, heating at normal pressure, wherein the temperature of the still is 101 ℃, and the temperature of the gas phase is 90 ℃. The oil phase and the water phase are layered in the water separator after the gas phase is condensed, and the water phase flows back into the distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 5:1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is transparent and clear. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 7
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 160g of water, heating the oil at 140 ℃, heating at normal pressure, wherein the temperature of the still is 108 ℃ and the temperature of the gas phase is 98 ℃. After the gas phase is condensed, the oil phase and the water phase are layered in a water separator, and the water phase flows back into a distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 0.5: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is light yellow. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 8
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 160g of water, heating the oil at 140 ℃, heating at normal pressure, wherein the temperature of the still is 105 ℃, and the temperature of the gas phase is 94 ℃. After the gas phase is condensed, the oil phase and the water phase are layered in a water separator, and the water phase flows back into a distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 1: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is light yellow. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Example 9
Pumping 800g of chlorobenzene rectifying still liquid into a 2L distillation still by a pump, adding 160g of water, heating the oil at 140 ℃, heating at normal pressure, wherein the temperature of the still is 103 ℃, and the temperature of the gas phase is 94 ℃. The oil phase and the water phase are layered in the water separator after the gas phase is condensed, and the water phase flows back into the distillation kettle. When the volume ratio of the oil phase to the water phase in the water separator is 3: 1, starting to extract an oil phase at the bottom of the water separator, and simultaneously pumping black chlorobenzene rectifying still liquid into the distillation still by using a pump, wherein the volume of the pumped chlorobenzene rectifying still liquid in unit time is the same as that of the oil phase separated from the bottom of the water separator in unit time. The oil phase separated from the bottom of the water separator is the benzene chloride rectifying still liquid after decoking, and the appearance is light yellow. When the tar in the distillation kettle influences the normal operation, the tar is discharged, and the water is continuously used in the distillation.
Claims (4)
1. A method for decoking chlorobenzene rectifying still liquid is characterized by comprising the following steps:
(1) adding chlorobenzene rectifying still liquid and water into a distillation kettle in advance before starting continuous steam distillation, and heating materials in the kettle to boil under normal pressure; wherein the mass ratio of the chlorobenzene rectification kettle liquid to water is 1.5-5: 1;
(2) the boiling kettle liquid generates steam, the steam flows into a water separator after being condensed, and a water phase and an oil phase are separated from the water separator; wherein the temperature of the heating medium is 135-150 ℃, the temperature of the kettle is 100-110 ℃, and the temperature of the gas phase is 88-100 ℃;
(3) refluxing the water phase into a distillation still, discharging the oil phase at the bottom of the water separator, reserving a certain volume of oil phase in the water separator, wherein the volume ratio of the oil phase to the water phase in the water separator is 0.1-10: 1, and the discharged oil phase is decoking or chlorobenzene rectifying still liquid;
(4) pumping chlorobenzene rectifying still liquid into the kettle while discharging the oil phase from the bottom of the water separator; the volume of the chlorobenzene rectifying still liquid pumped in unit time is the same as that of the oil phase discharged from the bottom of the water separator in unit time;
(5) the tar in the still was discharged periodically.
2. The decoking method according to claim 1, wherein the mass ratio of the chlorobenzene rectifying still liquid to water in step (1) is 2.5: 1.
3. The decoking method as claimed in claim 1, wherein the temperature of the heat medium in steps (1) and (2) is 140 ℃ and 145 ℃, the temperature of the kettle is 101-105 ℃, and the temperature of the gas phase is 88-98 ℃.
4. The decoking method according to claim 1, wherein the volume ratio of the oil phase to the water phase in the water separator in the step (3) is 1-5: 1.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101891586A (en) * | 2010-08-19 | 2010-11-24 | 江苏隆昌化工有限公司 | Process for extracting high-purity m-dichlorobenzene from solid waste chlorobenzene tar |
| CN102951995A (en) * | 2012-10-09 | 2013-03-06 | 江苏隆昌化工有限公司 | Process for producing m-dichlorobenzene by using mixed dichlorobenzene as raw material |
| CN204261362U (en) * | 2014-11-14 | 2015-04-15 | 陕西天谷生物科技集团有限公司 | A kind of gathering-device of Rotary Evaporators volatile matter distillation oil |
| CN107340346A (en) * | 2017-08-07 | 2017-11-10 | 安徽东至广信农化有限公司 | The quick determination method of micro dichloro-benzenes in a kind of chlorination benzaldehyde product |
| CN208604044U (en) * | 2018-07-10 | 2019-03-15 | 天津天大凯泰化工科技有限公司 | A kind of device of azeotropic distillation compartment/paracresol and adjacent diethylstilbestrol |
-
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- 2019-06-03 CN CN201910476524.0A patent/CN112023430B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101891586A (en) * | 2010-08-19 | 2010-11-24 | 江苏隆昌化工有限公司 | Process for extracting high-purity m-dichlorobenzene from solid waste chlorobenzene tar |
| CN102951995A (en) * | 2012-10-09 | 2013-03-06 | 江苏隆昌化工有限公司 | Process for producing m-dichlorobenzene by using mixed dichlorobenzene as raw material |
| CN204261362U (en) * | 2014-11-14 | 2015-04-15 | 陕西天谷生物科技集团有限公司 | A kind of gathering-device of Rotary Evaporators volatile matter distillation oil |
| CN107340346A (en) * | 2017-08-07 | 2017-11-10 | 安徽东至广信农化有限公司 | The quick determination method of micro dichloro-benzenes in a kind of chlorination benzaldehyde product |
| CN208604044U (en) * | 2018-07-10 | 2019-03-15 | 天津天大凯泰化工科技有限公司 | A kind of device of azeotropic distillation compartment/paracresol and adjacent diethylstilbestrol |
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