CN111548252A - Device and method for extracting octanol from trioctyl trimellitate residual liquid - Google Patents
Device and method for extracting octanol from trioctyl trimellitate residual liquid Download PDFInfo
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- CN111548252A CN111548252A CN202010587487.3A CN202010587487A CN111548252A CN 111548252 A CN111548252 A CN 111548252A CN 202010587487 A CN202010587487 A CN 202010587487A CN 111548252 A CN111548252 A CN 111548252A
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- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 title claims abstract description 112
- 239000007788 liquid Substances 0.000 title claims abstract description 90
- JNXDCMUUZNIWPQ-UHFFFAOYSA-N trioctyl benzene-1,2,4-tricarboxylate Chemical compound CCCCCCCCOC(=O)C1=CC=C(C(=O)OCCCCCCCC)C(C(=O)OCCCCCCCC)=C1 JNXDCMUUZNIWPQ-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 15
- 238000010992 reflux Methods 0.000 claims description 45
- 239000002699 waste material Substances 0.000 claims description 34
- 239000012071 phase Substances 0.000 claims description 15
- 238000005086 pumping Methods 0.000 claims description 15
- 238000000605 extraction Methods 0.000 claims description 13
- 238000005070 sampling Methods 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 5
- 239000012043 crude product Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 2
- ARCGXLSVLAOJQL-UHFFFAOYSA-N trimellitic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C(C(O)=O)=C1 ARCGXLSVLAOJQL-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 150000008064 anhydrides Chemical class 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229920001971 elastomer Polymers 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 239000005060 rubber Substances 0.000 description 2
- SRPWOOOHEPICQU-UHFFFAOYSA-N trimellitic anhydride Chemical compound OC(=O)C1=CC=C2C(=O)OC(=O)C2=C1 SRPWOOOHEPICQU-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005034 decoration Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005886 esterification reaction Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 230000009182 swimming Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
The invention relates to the technical field of organic chemical industry, and particularly discloses a device and a method for extracting octanol from trioctyl trimellitate residual liquid.
Description
Technical Field
The invention relates to the technical field of organic chemical industry, in particular to a device and a method for extracting octanol from trioctyl trimellitate residual liquid.
Background
The trioctyl trimellitate is liquid at normal temperature, is convenient to transport and use, and the ester has high boiling point, low volatility and moderate molecular weight, contains some branched chains in molecules, is good for improving the plasticity and flexibility of plastics and rubber, and is commonly used as a plasticizer, so that the temperature resistance grade of PVC plastics, rubber, resin and the like can be obviously improved. It is also used in automobile decoration material, waterproof layer of swimming pool, soaking oil of capacitor, etc.
At present, the industrial production method of trioctyl trimellitate is generally produced by directly esterifying trimellitic acid and octanol. The industrial production method comprises the steps of oxidizing trimellitic benzene in a liquid phase by air to prepare trimellitic acid, dehydrating the trimellitic acid at high temperature to form anhydride, rectifying the anhydride at high temperature and high vacuum to obtain trimellitic anhydride with the content of over 95 percent, carrying out esterification reaction on the trimellitic anhydride and octanol under the action of a catalyst to obtain crude trioctyl trimellitate, and rectifying and purifying the crude trioctyl trimellitate to obtain a finished product of trioctyl trimellitate.
A certain amount of residual liquid containing octanol and trioctyl trimellitate is generated in the reaction process and the rectification process, the color number of the residual liquid is high, the purification difficulty is high, the residual liquid is directly discarded, the residual liquid treatment burden is increased, and the unit consumption of products is increased.
Disclosure of Invention
The invention aims to solve the technical problems that the treatment burden is increased and the unit consumption of products is increased due to the fact that trioctyl trimellitate residual liquid containing octanol generated in the existing production process is directly discarded.
In order to solve the technical problems, the invention provides a device for extracting octanol from trioctyl trimellitate raffinate, which comprises a heavy component removal tower, a heavy component removal tower feeding preheater, a heavy component removal tower reboiler, a heavy component removal tower first-stage condenser, a heavy component removal tower second-stage condenser, a heavy component removal tower condensate tank, a light component removal tower feeding preheater, a light component removal tower reboiler, a light component removal tower first-stage condenser, a light component removal tower second-stage condenser, a light component removal tower reflux tank and a light component removal tower,
a feed inlet on the left side of the de-weighting tower is connected with a discharge outlet on the top end of a feed preheater of the de-weighting tower, and a feed inlet for trioctyl trimellitate residual liquid containing octanol is arranged at the bottom end of the feed preheater of the de-weighting tower;
a feed inlet at the lower part of the right side of the heavy component removal tower is connected with an outlet at the bottom end of a reboiler of the heavy component removal tower, and an inlet at the top end of the reboiler of the heavy component removal tower is connected with a residual liquid discharge outlet at the bottom end of the heavy component removal tower through a circulating pump at the bottom of the heavy component removal tower; a pipeline between the residual liquid discharge port at the bottom end of the de-heavy tower and the circulating pump at the bottom of the de-heavy tower is connected with a waste liquid extraction pump at the bottom of the de-heavy tower;
the outlet of the gas phase crude octanol at the top end of the de-weighting tower is connected with the inlet of the left side of the top of the first-stage condenser of the de-weighting tower, the outlet of the gas phase at the right side of the top of the first-stage condenser of the de-weighting tower is connected with the inlet of the left side of the top of the second-stage condenser of the de-weighting tower, and the outlet of the bottom end of the first-stage condenser of the de-weighting tower and the outlet of the bottom end of the second-stage condenser;
a crude product condensate outlet at the lower part of the right side of the heavy component removal tower condensate tank is connected with an inlet at the bottom of a light component removal tower feeding preheater through a light component removal tower feeding pump; an outlet at the top of the feed preheater of the lightness-removing column is connected with a feed inlet at the lower part of the left side of the lightness-removing column;
the gas-phase refined octanol discharge port at the top end of the lightness-removing tower is connected with the left inlet at the top of the first-stage condenser of the lightness-removing tower, the right outlet at the top of the first-stage condenser of the lightness-removing tower is connected with the left inlet at the top of the second-stage condenser of the lightness-removing tower, and the outlet at the bottom end of the first-stage condenser of the lightness-removing tower and the outlet at the bottom end of the second-stage condenser of the lightness-removing tower are connected in parallel to the;
a feed inlet at the lower part of the right side of the light component removal tower is connected with an outlet at the bottom end of a reboiler of the light component removal tower, and an inlet at the top end of the reboiler of the light component removal tower is connected with a residual liquid discharge outlet at the bottom end of the light component removal tower through a circulating pump at the bottom of the light component removal tower; a pipeline between a residual liquid discharge port at the bottom end of the light component removing tower and a circulating pump at the bottom of the light component removing tower is connected with a waste liquid extracting pump at the bottom of the light component removing tower;
and a refined condensate outlet at the lower part of the left side of the light component removal tower reflux tank is connected with a condensate inlet at the upper part of the right side of the light component removal tower through a light component removal tower reflux pump.
Furthermore, a circulating pump of the heavy component removal tower condensate tank is connected to a pipeline between the heavy component removal tower condensate tank and the light component removal tower feed pump, and the circulating pump of the heavy component removal tower condensate tank is connected with the heavy component removal tower condensate tank through a pipeline A.
Furthermore, an outlet of the light component removal tower feeding pump is connected with an inlet at the bottom of the light component removal tower feeding preheater through a pipeline B, and a pipeline C is arranged between the pipeline B and the pipeline A.
Furthermore, a circulating pump of the light component removal tower reflux tank is connected to a pipeline between the light component removal tower reflux tank and the light component removal tower reflux pump, and the circulating pump of the light component removal tower reflux tank is connected with the light component removal tower reflux tank through a pipeline D.
Further, an outlet of the reflux pump of the light component removal tower is connected with a condensate feeding port at the upper part of the light component removal tower through a pipeline E, and a pipeline F is arranged between the pipeline E and the pipeline D.
Further, a waste liquid pumping pump at the bottom of the heavy component removal tower discharges waste liquid through a pipeline G, an outlet at the top end of a circulating pump at the bottom of the heavy component removal tower is connected with an inlet at the top end of a reboiler of the heavy component removal tower through a pipeline H, and a pipeline I is arranged between the pipeline G and the pipeline H.
Further, the waste liquid at the bottom of the light component removing tower is discharged by a waste liquid extracting pump through a pipeline J, an outlet at the top end of a circulating pump at the bottom of the light component removing tower is connected with an inlet at the top end of a reboiler of the light component removing tower through a pipeline K, and a pipeline L is arranged between the pipeline J and the pipeline K.
Further, the right outlet at the top of the secondary condenser of the heavy component removal tower and the right outlet at the top of the secondary condenser of the light component removal tower are respectively connected with a vacuum system.
The method for extracting the octanol from the trioctyl trimellitate residual liquid adopts the device for extracting the octanol from the trioctyl trimellitate residual liquid for recovery, and comprises the following process steps:
s1, after the de-weighting tower is vacuumized, preheating trioctyl trimellitate residual liquid (sampling mark is S0) containing octanol through a feed preheater of the de-weighting tower, and then pumping the residual liquid into the de-weighting tower;
s2, after the liquid level of the de-weighting tower reaches 1m, starting a de-weighting tower bottom circulating pump, starting a de-weighting tower reboiler to heat and raise the temperature, controlling the kettle temperature at 125-135 ℃, and after the octanol content of the tower bottom liquid (sampled and marked as S1) is detected to be lower than 10%, pumping out the de-weighting tower bottom waste liquid by using a de-weighting tower bottom waste liquid pump;
s3, condensing the gas phase of the heavy component removal tower through a first-stage condenser of the heavy component removal tower and a second-stage condenser of the heavy component removal tower, feeding the condensate into a condensate tank of the heavy component removal tower, and analyzing the octanol content of the condensate (the sampling mark is S2); opening a circulating pump of a condensation liquid tank of the de-weighting tower, and continuously circulating the condensation liquid in the condensation liquid tank of the de-weighting tower;
s4, after the liquid level of a heavy component removal tower condensate tank reaches 1m, establishing vacuum on the light component removal tower, starting a light component removal tower feed pump, preheating heavy component removal tower condensate by a light component removal tower feed preheater, and then pumping into the light component removal tower;
s5, after the liquid level of the light component removal tower reaches 1m, starting a circulating pump at the bottom of the light component removal tower, starting a reboiler of the light component removal tower for heating and raising the temperature, wherein the kettle temperature is controlled to be 85-95 ℃;
s6, condensing the gas phase of the light component removal tower through a first-stage condenser of the light component removal tower and a second-stage condenser of the light component removal tower, and then feeding the liquid phase into a reflux tank of the light component removal tower; opening a circulating pump of a light component removal tower reflux tank, and continuously circulating the condensate in the light component removal tower reflux tank;
s7, after the liquid level of a light component removal tower reflux tank reaches 1m, starting a light component removal tower reflux pump, and controlling the tower top temperature to be 75-80 ℃;
s8, extracting octanol from the middle part of the light component removal tower (the sampling mark is S3), analyzing the content of the octanol, and extracting the octanol when the content reaches more than 95 percent; and pumping out the waste liquid at the bottom of the light component removal tower by using a pump for pumping the waste liquid at the bottom of the light component removal tower.
The invention has the advantages that:
the method is simple to operate, can recover high-content octanol for reuse through continuous feeding, reduces the material consumption of trioctyl trimellitate production, reduces the generation amount of waste liquid in the trioctyl trimellitate production process, and is beneficial to environmental protection.
Drawings
In order to more clearly illustrate the technical solution of the present invention, the drawings needed for the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic diagram showing the structure of the octanol extraction process in the trioctyl trimellitate residue according to the present invention;
in the figure: 1-heavy component removal tower, 2-heavy component removal tower feeding preheater, 3-heavy component removal tower reboiler, 401-heavy component removal tower bottom circulating pump, 402-heavy component removal tower bottom waste liquid extraction pump, 5-heavy component removal tower first-stage condenser, 6-heavy component removal tower second-stage condenser, 7-heavy component removal tower condensate tank, 801-heavy component removal tower condensate tank circulating pump, 802-light component removal tower feeding pump, 9-light component removal tower feeding preheater, 10-light component removal tower reboiler, 1101-light component removal tower bottom circulating pump, 1102-light component removal tower bottom waste liquid extraction pump, 12-light component removal tower first-stage condenser, 13-light component removal tower second-stage condenser, 14-light component removal tower reflux tank, 1501-light component removal tower reflux, 1502-light component removal tower reflux circulating pump and 16-light component removal tower.
Detailed Description
The following describes the specific embodiments of the present invention with reference to examples, so that the technical solutions and the advantages thereof are more clear and clear. The following described embodiments are exemplary and are intended to be illustrative of the invention, but are not to be construed as limiting the invention.
Example (b):
as shown in figure 1, the invention specifically discloses a device for extracting octanol from trioctyl trimellitate raffinate, which comprises a heavy component removal tower 1, a heavy component removal tower feeding preheater 2, a heavy component removal tower reboiler 3, a heavy component removal tower first-stage condenser 5, a heavy component removal tower second-stage condenser 6, a heavy component removal tower condensate tank 7, a light component removal tower feeding preheater 9, a light component removal tower reboiler 10, a light component removal tower first-stage condenser 12, a light component removal tower second-stage condenser 13, a light component removal tower reflux tank 14 and a light component removal tower 16,
a feed inlet on the left side of the de-weighting tower 1 is connected with a discharge outlet on the top end of a feed preheater 2 of the de-weighting tower, and a feed inlet for trioctyl trimellitate residual liquid containing octanol is arranged at the bottom end of the feed preheater 2 of the de-weighting tower;
a feed inlet at the lower part of the right side of the heavy component removal tower 1 is connected with an outlet at the bottom end of a heavy component removal tower reboiler 3, and an inlet at the top end of the heavy component removal tower reboiler 3 is connected with a residual liquid discharge outlet at the bottom end of the heavy component removal tower 1 through a heavy component removal tower bottom circulating pump 401; a pipeline between a residual liquid discharge port at the bottom end of the de-heavy tower 1 and a de-heavy tower bottom circulating pump 401 is connected with a de-heavy tower bottom waste liquid extraction pump 402, and the de-heavy tower bottom waste liquid extraction pump 402 discharges waste liquid through a pipeline G; an outlet at the top end of a circulating pump 401 at the bottom of the heavy component removal tower is connected with an inlet at the top end of a reboiler 3 of the heavy component removal tower through a pipeline H, and a pipeline I is arranged between the pipeline G and the pipeline H;
a gas-phase crude octanol discharge port at the top end of the de-weighting tower 1 is connected with a left inlet at the top of a first-stage condenser 5 of the de-weighting tower, a gas-phase outlet at the right side of the top of the first-stage condenser 5 of the de-weighting tower is connected with a left inlet at the top of a second-stage condenser 6 of the de-weighting tower, and a bottom outlet of the first-stage condenser 5 of the de-weighting tower and a bottom outlet of the second-stage condenser 6 of the de-weighting tower are connected;
a crude product condensate outlet at the lower part of the right side of the heavy component removal tower condensate tank 7 is connected with an inlet at the bottom of a light component removal tower feeding preheater 9 through a light component removal tower feeding pump 802; the outlet of the light component removal tower feed pump 802 is connected with the inlet at the bottom of the light component removal tower feed preheater 9 through a pipeline B; an outlet at the top of the feed preheater 9 of the lightness-removing column is connected with a feed inlet at the lower part of the left side of the lightness-removing column 16; a circulating pump 801 of the heavy component removal tower condensate tank is connected to a pipeline between the heavy component removal tower condensate tank 7 and the light component removal tower feed pump 802, and the circulating pump 801 of the heavy component removal tower condensate tank is connected with the heavy component removal tower condensate tank 7 through a pipeline A; a pipeline C is arranged between the pipeline B and the pipeline A;
a gas-phase refined octanol discharge port at the top end of the lightness-removing tower 16 is connected with a left inlet at the top of a first-stage condenser 12 of the lightness-removing tower, a right outlet at the top of the first-stage condenser 12 of the lightness-removing tower is connected with a left inlet at the top of a second-stage condenser 13 of the lightness-removing tower, and a bottom outlet of the first-stage condenser 12 of the lightness-removing tower and a bottom outlet of the second-stage condenser 13 of the lightness-removing tower are connected in parallel with a liquid;
a refined condensate outlet at the lower part of the left side of the light component removal tower reflux tank 14 is connected with a condensate inlet at the upper part of the right side of the light component removal tower 16 through a light component removal tower reflux pump 1501; a pipe between the light component removal tower reflux tank 14 and the light component removal tower reflux pump 1501 is connected with a light component removal tower reflux tank circulating pump 1502, and the light component removal tower reflux tank circulating pump 1502 is connected with the light component removal tower reflux tank 14 through a pipe D; an outlet of the lightness-removing column reflux pump 1501 is connected with a condensate feeding port at the upper part of the lightness-removing column 16 through a pipeline E, and a pipeline F is arranged between the pipeline E and the pipeline D;
a feed inlet at the lower part of the right side of the lightness-removing column 16 is connected with an outlet at the bottom end of a reboiler 10 of the lightness-removing column, and an inlet at the top end of the reboiler 10 of the lightness-removing column is connected with a discharge outlet of raffinate at the bottom end of the lightness-removing column 16 through a circulation pump 1101 at the bottom of the lightness-removing column; a pipe between a residual liquid discharge port at the bottom end of the light component removal tower 16 and a light component removal tower bottom circulating pump 1101 is connected with a light component removal tower bottom waste liquid extraction pump 1102, and the light component removal tower bottom waste liquid extraction pump 1102 discharges waste liquid through a pipe J; an outlet at the top end of a circulating pump 1101 at the bottom of the light component removing tower is connected with an inlet at the top end of a reboiler 10 of the light component removing tower through a pipeline K, and a pipeline L is arranged between the pipeline J and the pipeline K.
The right outlet at the top of the second-stage condenser 6 of the heavy component removal tower and the right outlet at the top of the second-stage condenser 13 of the light component removal tower are respectively connected with a vacuum system.
The method for recovering the octanol by adopting the octanol extraction device in the trioctyl trimellitate residual liquid comprises the following steps:
s1, after the de-weighting tower 1 is vacuumized, preheating trioctyl trimellitate residual liquid (sampling mark is S0) containing octanol through a de-weighting tower feeding preheater 2, and then pumping into the de-weighting tower 1;
s2, after the liquid level of the heavy component removal tower 1 reaches 1m, starting a heavy component removal tower bottom circulating pump 401, starting a heavy component removal tower reboiler 3 for heating and raising the temperature, controlling the kettle temperature at 125-135 ℃, and after the octanol content of the tower bottom liquid (the sampling mark is S1) is detected to be lower than 10%, pumping the heavy component removal tower bottom waste liquid by using a heavy component removal tower bottom waste liquid pump 402;
s3, condensing the gas phase of the heavy component removal tower 1 through a first-stage condenser 5 and a second-stage condenser 6 of the heavy component removal tower, feeding the condensate into a condensate tank 7 of the heavy component removal tower, and analyzing the octanol content of the condensate (the sampling mark is S2); opening a circulating pump 801 of the heavy component removal tower condensed liquid tank, and continuously circulating the condensed liquid in the heavy component removal tower condensed liquid tank 7;
s4, after the liquid level of the heavy component removal tower condensate tank 7 reaches 1m, establishing vacuum in the light component removal tower 16, starting a light component removal tower feed pump 802, preheating heavy component removal tower condensate by a light component removal tower feed preheater 9, and then pumping the heavy component removal tower condensate into the light component removal tower 16;
s5, after the liquid level of the light component removal tower 16 reaches 1m, starting a circulating pump 1101 at the bottom of the light component removal tower, starting a reboiler 10 of the light component removal tower for heating and raising the temperature, and controlling the kettle temperature to be 85-95 ℃;
s6, condensing the gas phase of the lightness-removing column 16 through a first-stage condenser 12 and a second-stage condenser 13 of the lightness-removing column, and then feeding the liquid phase into a reflux tank 14 of the lightness-removing column; a circulating pump 1502 of the light component removal tower reflux tank is opened, and the condensate in the light component removal tower reflux tank 14 is continuously circulated;
s7, after the liquid level of the light component removal tower reflux tank 14 reaches 1m, starting a light component removal tower reflux pump 1501, and controlling the tower top temperature to be 75-80 ℃;
s8, extracting octanol from the middle part of the light component removal tower 16 (the sampling mark is S3), analyzing the content of the octanol, and extracting the octanol when the content reaches more than 95 percent; the light component removal column bottom waste liquid is pumped out by a light component removal column bottom waste liquid pump 1102.
Four samples were taken for octanol content and the results are given in the following table:
the method is simple to operate, can recover high-content octanol for reuse through continuous feeding, reduces the material consumption of trioctyl trimellitate production, reduces the generation amount of waste liquid in the trioctyl trimellitate production process, and is beneficial to environmental protection.
The above disclosure is only one preferred embodiment of the present invention, and certainly should not be construed as limiting the scope of the invention, which is defined by the claims and their equivalents.
Claims (9)
1. The utility model provides an extraction element of octanol in trioctyl trimellitate raffinate which characterized in that: comprises a heavy component removal tower (1), a heavy component removal tower feeding preheater (2), a heavy component removal tower reboiler (3), a heavy component removal tower first-stage condenser (5), a heavy component removal tower second-stage condenser (6), a heavy component removal tower condensate tank (7), a light component removal tower feeding preheater (9), a light component removal tower reboiler (10), a light component removal tower first-stage condenser (12), a light component removal tower second-stage condenser (13), a light component removal tower reflux tank (14) and a light component removal tower (16),
a feed inlet on the left side of the de-weighting tower (1) is connected with a discharge outlet on the top end of the de-weighting tower feed preheater (2), and a trioctyl trimellitate residual liquid feed inlet containing octanol is formed in the bottom end of the de-weighting tower feed preheater (2);
a feed inlet at the lower part of the right side of the heavy component removal tower (1) is connected with an outlet at the bottom end of the heavy component removal tower reboiler (3), and an inlet at the top end of the heavy component removal tower reboiler (3) is connected with a residual liquid discharge outlet at the bottom end of the heavy component removal tower (1) through a heavy component removal tower bottom circulating pump (401); a pipeline between a raffinate discharge hole at the bottom end of the de-heavy tower (1) and a de-heavy tower bottom circulating pump (401) is connected with a de-heavy tower bottom waste liquid extraction pump (402);
the gas-phase crude octanol discharge port at the top end of the de-weighting tower (1) is connected with the inlet at the left top of the first-stage condenser (5) of the de-weighting tower, the gas-phase outlet at the right top of the first-stage condenser (5) of the de-weighting tower is connected with the inlet at the left top of the second-stage condenser (6) of the de-weighting tower, and the outlet at the bottom end of the first-stage condenser (5) of the de-weighting tower and the outlet at the bottom end of the second-stage condenser (6) of the de-weighting tower are connected in parallel to the octanol;
a crude product condensate outlet at the lower part of the right side of the heavy component removal tower condensate tank (7) is connected with an inlet at the bottom of the light component removal tower feed preheater (9) through a light component removal tower feed pump (802); an outlet at the top of the light component removal tower feeding preheater (9) is connected with a feeding hole at the lower part of the left side of the light component removal tower (16);
the gas-phase refined octanol discharge port at the top end of the lightness-removing tower (16) is connected with the inlet at the left top of the first-stage condenser (12) of the lightness-removing tower, the outlet at the right top of the first-stage condenser (12) of the lightness-removing tower is connected with the inlet at the left top of the second-stage condenser (13) of the lightness-removing tower, and the outlet at the bottom end of the first-stage condenser (12) of the lightness-removing tower and the outlet at the bottom end of the second-stage condenser (13) of the lightness-removing tower are connected in parallel to the liquid-phase;
a feed inlet at the lower part of the right side of the lightness-removing column (16) is connected with an outlet at the bottom end of the lightness-removing column reboiler (10), and an inlet at the top end of the lightness-removing column reboiler (10) is connected with a discharge outlet of raffinate at the bottom end of the lightness-removing column (16) through a circulation pump (1101) at the bottom of the lightness-removing column; a pipeline between a residual liquid discharge port at the bottom end of the lightness-removing tower (16) and a circulation pump (1101) at the bottom of the lightness-removing tower is connected with a pump (1102) for pumping the waste liquid at the bottom of the lightness-removing tower;
and a refined condensate outlet at the lower part of the left side of the light component removal tower reflux tank (14) is connected with a condensate feed inlet at the upper part of the right side of the light component removal tower (16) through a light component removal tower reflux pump (1501).
2. The device for extracting octanol from trioctyl trimellitate raffinate according to claim 1, wherein a pipeline between the heavy component removal tower condensate tank (7) and the light component removal tower feed pump (802) is connected with a heavy component removal tower condensate tank circulating pump (801), and the heavy component removal tower condensate tank circulating pump (801) is connected with the heavy component removal tower condensate tank (7) through a pipeline A.
3. The device for extracting octanol from trioctyl trimellitate raffinate according to claim 2, wherein the outlet of the lightness-removing column feed pump (802) is connected with the inlet at the bottom of the lightness-removing column feed preheater (9) through a pipeline B, and a pipeline C is arranged between the pipeline B and the pipeline A.
4. The device for extracting octanol from trioctyl trimellitate raffinate according to claim 1, wherein a lightness-removing column reflux tank circulating pump (1502) is connected to the pipeline between the lightness-removing column reflux tank (14) and the lightness-removing column reflux pump (1501), and the lightness-removing column reflux tank circulating pump (1502) is connected to the lightness-removing column reflux tank (14) through a pipeline D.
5. The device for extracting octanol from trioctyl trimellitate raffinate according to claim 4, wherein an outlet of the light component removal tower reflux pump (1501) is connected with a condensate feed inlet at the upper part of the light component removal tower (16) through a pipeline E, and a pipeline F is arranged between the pipeline E and the pipeline D.
6. The device for extracting octanol from trioctyl trimellitate raffinate according to claim 1, wherein the de-heavy column bottom waste liquid extraction pump (402) discharges waste liquid through a pipeline G, the top outlet of the de-heavy column bottom circulation pump (401) is connected with the top inlet of the de-heavy column reboiler (3) through a pipeline H, and a pipeline I is arranged between the pipeline G and the pipeline H.
7. The device for extracting the octanol from the trioctyl trimellitate raffinate according to claim 1, wherein the lightness-removing column bottom waste liquid extraction pump (1102) discharges the waste liquid through a pipeline J, a top outlet of the lightness-removing column bottom circulating pump (1101) is connected with a top inlet of the lightness-removing column reboiler (10) through a pipeline K, and a pipeline L is arranged between the pipeline J and the pipeline K.
8. The device for extracting octanol from trioctyl trimellitate raffinate according to claim 1, wherein the right outlet at the top of the second-stage condenser (6) of the heavy component removal tower and the right outlet at the top of the second-stage condenser (13) of the light component removal tower are respectively connected to a vacuum system.
9. A method for extracting octanol from trioctyl trimellitate residual liquid, which adopts the device for extracting octanol from trioctyl trimellitate residual liquid according to any one of claims 1 to 8 to recover, and is characterized in that: the recovery method comprises the following process steps:
s1, after the de-weighting tower (1) is vacuumized, preheating trioctyl trimellitate residual liquid (a sampling mark is S0) containing octanol through a de-weighting tower feeding preheater (2) and then pumping into the de-weighting tower (1);
s2, after the liquid level of the heavy component removal tower (1) reaches 1m, starting a heavy component removal tower bottom circulating pump (401), starting a heavy component removal tower reboiler (3) for heating and raising the temperature, controlling the kettle temperature at 125-135 ℃, and after the tower bottom liquid (sampling mark is S1) detects that the octanol content is lower than 10%, pumping the heavy component removal tower bottom waste liquid by using a heavy component removal tower bottom waste liquid pump (402);
s3, condensing the gas phase of the heavy component removal tower through a first-stage condenser (5) of the heavy component removal tower and a second-stage condenser (6) of the heavy component removal tower, feeding the condensate into a condensate tank (7) of the heavy component removal tower, and analyzing the octanol content of the condensate (the sampling mark is S2); opening a circulating pump (801) of the heavy component removal tower condensed liquid tank, and continuously circulating the condensed liquid in the heavy component removal tower condensed liquid tank (7);
s4, after the liquid level of the heavy component removal tower condensate tank (7) reaches 1m, establishing vacuum in the light component removal tower (16), starting a light component removal tower feed pump (802), preheating heavy component removal tower condensate by a light component removal tower feed preheater (9), and then pumping the heavy component removal tower condensate into the light component removal tower (16);
s5, after the liquid level of the light component removal tower (16) reaches 1m, starting a circulating pump (1101) at the bottom of the light component removal tower, starting a reboiler (10) of the light component removal tower for heating, and controlling the kettle temperature to be 85-95 ℃;
s6, condensing the gas phase of the lightness-removing tower through a first-stage condenser (12) of the lightness-removing tower and a second-stage condenser (13) of the lightness-removing tower, and then feeding the liquid phase into a reflux tank (14) of the lightness-removing tower; opening a circulating pump (1502) of a reflux tank of the light component removal tower, and continuously circulating the condensate in the reflux tank (14) of the light component removal tower;
s7, after the liquid level of a light component removal tower reflux tank (14) reaches 1m, starting a light component removal tower reflux pump (1501), and controlling the tower top temperature to be 75-80 ℃;
s8, extracting octanol from the middle part of the light component removal tower (16) (the sampling mark is S3) and analyzing the content of the octanol, and extracting the octanol when the content reaches more than 95 percent; and pumping out the light component removal tower bottom waste liquid by using a light component removal tower bottom waste liquid pumping pump (1102).
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