CN110627635A - System and process for recycling residual heat of diacid tower bottoms - Google Patents
System and process for recycling residual heat of diacid tower bottoms Download PDFInfo
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- CN110627635A CN110627635A CN201910832945.2A CN201910832945A CN110627635A CN 110627635 A CN110627635 A CN 110627635A CN 201910832945 A CN201910832945 A CN 201910832945A CN 110627635 A CN110627635 A CN 110627635A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
- C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
- C07C51/445—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation by steam distillation
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- 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
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Abstract
The invention relates to a system and a process for recycling residue heat of a tower bottom liquid of a diacid tower, which comprises the following steps: the device comprises a diacid tower, a triacid tower and a reboiler B, wherein a liquid outlet of a tower kettle of the diacid tower is connected with a shell pass liquid inlet of the reboiler B of the triacid tower, and a liquid outlet of the reboiler B of the triacid tower is connected with a liquid inlet in the middle of the triacid tower. The arrangement of the triacid tower reboiler B effectively recovers the residual heat of the tower bottom liquid of the diacid tower, and reduces water consumption and power consumption, thereby reducing energy consumption; the heat required by the tower kettle temperature rise of the triacid tower utilizes the residual heat of the tower kettle liquid of the diacid tower, reduces the using amount of heating steam of the triacid tower and reduces the energy consumption.
Description
Technical Field
The invention belongs to a waste heat recycling process, and particularly relates to a system and a process for recycling waste heat of a tower kettle of a diacid tower of a formic acid device.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
Patent CN102952007A discloses a production device of 10 ten thousand tons of formic acid of single set of annual output, mainly include carbonyl reactor, methyl ester rectifying column, methyl ester storage tank, first hydrolysis reactor, second hydrolysis reactor, an acid tower, diacid tower, triacid tower, wherein the bottom export of carbonyl reactor and the middle part import of methyl ester rectifying column are connected, the top of methyl ester rectifying column is connected with the top of condensate methyl ester storage tank, the bottom export of methyl ester storage tank and the bottom of first hydrolysis reactor are connected, the upper portion export of first hydrolysis reactor and the lower part import of second hydrolysis reactor are connected, the upper portion export of second hydrolysis reactor and the middle part import of acid tower are connected, the bottom export of acid tower and the middle part import of diacids tower are connected, the lower part export of diacids tower and triacid tower middle part import are connected.
In the production process of formic acid, a diacid tower is a pressurized tower, the temperature of a tower kettle is 150-154 ℃, the temperature of the tower kettle is required to be reduced and then the tower kettle enters the middle part of a triacid tower, the tower kettle liquid of the traditional diacid tower is cooled by a kettle liquid cooler and then enters the triacid tower, the kettle liquid cooler is directly cooled by circulating water, and the shell pass circulating water side of the kettle liquid cooler is frequently scaled due to high temperature of the kettle liquid, so that the heat exchange efficiency is reduced and a heat exchanger is required to be frequently washed; the consumption of the circulating water is large, so that the electricity consumption of the circulating water pump is increased, and the energy waste is caused; the medium temperature is high, and the circulating water heat exchanger is easy to scale.
On the other hand, the triacid acid tower formic acid (85%) produced by the existing process flow also has the problems of low purity and poor product quality.
Disclosure of Invention
In order to overcome the problems, the invention provides a process for recycling the residual heat of the tower bottom liquid of the diacid tower, so as to realize the efficient utilization of the residual heat of the tower bottom liquid of the diacid tower and be beneficial to saving energy. The system not only effectively reduces the using amount of circulating water, saves energy, and realizes the process of efficiently utilizing the residual heat of the tower kettle of the diacid tower.
In order to achieve the technical purpose, the technical scheme adopted by the invention is as follows:
a diacid tower bottom waste heat recovery system comprises: the device comprises a diacid tower, a triacid tower and a reboiler B, wherein a liquid outlet of a tower kettle of the diacid tower is connected with a shell pass liquid inlet of the reboiler B of the triacid tower, and a liquid outlet of the reboiler B of the triacid tower is connected with a liquid inlet in the middle of the triacid tower.
Aiming at the problems of large consumption and easy scaling of the circulating water of the prior diacid tower. According to the invention, the tower bottom liquid of the diacid tower is connected with the lower side of the shell pass of the reboiler of the triacid tower through a pipeline, and is used as a heat source to heat the tower bottom of the triacid tower, so that the heat of the tower bottom liquid of the diacid tower is effectively transferred to the triacid tower, the use amount of circulating water of the diacid tower and the scaling of the shell pass of the cooler of the tower bottom liquid are reduced, the use amount of heating steam of the triacid tower is reduced, and the energy consumption is reduced.
More importantly, the method aims at the problem that the purity of formic acid (85%) produced by the existing 10 ten thousand ton formic acid production device is low. Through years of systematic, deep research and large-scale experimental investigation, the inventor discovers that: mainly because the long-period operation stability of the existing diacid tower bottom liquid cooler is poor, sometimes the temperature of the bottom liquid entering the triacid tower is too high (about after 3 and 4 months of operation), so that the corrosion of the three-tower feeding liquid distributor (the triacid tower is corrosion-resistant below 110 ℃, and the erosion corrosion is serious above the temperature) influences the three-tower liquid distribution effect, causes bias current to influence the rectification effect, and inevitably causes the influence of dissolved impurities on a formic acid finished product. After the temperature of the tower bottom of the triacidic tower is increased by using the tower bottom liquid of the diacid tower as a heat source, the long-period operation stability of the formic acid production device is improved, and the purity (87%) of formic acid is improved.
In some embodiments, the diacid tower is further provided with a plurality of heat exchangers, and tower bottom liquid of the diacid tower is heated (a reboiler) or cooled (a bottom liquid cooler) to meet different use requirements of the bottom liquid.
The steam partial pressure of each substance is different under different pressures, in order to obtain better rectification effect, in some embodiments, the diacid tower is a pressurized rectification tower, the operation pressure of the tower kettle is 290KPa-310KPa, the kettle temperature is 150 ℃ -154 ℃, and under the operation pressure and temperature, the separation rate and purity of formic acid are high.
In the invention, the type of the reboiler of the triacid tower is not particularly limited as long as the heat exchange requirement between the tower bottom liquid of the diacid tower and the triacid tower can be met, so that in some embodiments, the reboiler B of the triacid tower is a vertical tube side thermosyphon reboiler, thereby improving the heat exchange efficiency and the purity of formic acid.
In some embodiments, the triacid tower is a vacuum tower, the operation pressure at the top of the tower is-90 KPa-70KPa, the kettle temperature is 70-80 ℃, so that the purity of formic acid from the diacid tower is further improved, and the rectification efficiency is high.
The invention also provides a formic acid production device, which comprises: any of the above systems.
Different from the simple waste heat recovery, the method uses the waste heat of the tower bottom liquid of the diacid tower for heating the tower bottom of the triacid tower, thereby reducing the overall energy consumption of the equipment and improving the long-term operation stability; meanwhile, the problem that the purity of the formic acid (85%) in the triacid tower which is troubled by 10 ten thousand ton grade formic acid production for a long time at present is low is solved.
The invention also provides a method for recycling the residual heat of the tower bottom liquid of the diacid tower, which comprises the following steps:
and (3) heating the tower bottom liquid of the diacid tower by a tower reboiler B of the triacid tower, and then rectifying the tower bottom liquid of the diacid tower in the middle of the triacid tower to obtain the product.
In order to match the system, the residual heat of the tower bottom liquid of the diacid tower is efficiently transferred to the tower bottom of the triacid tower for heating, and the higher yield and purity of the formic acid are ensured. The invention carries out systematic optimization on the operation conditions of the tower kettle of the diacid tower and the triacid tower, and in some embodiments, the operation pressure of the tower kettle of the diacid tower is 290KPa to 310KPa, and the temperature of the tower kettle is 150 ℃ to 154 ℃. The tower top operating pressure of the triacid tower is-90 KPa-70KPa, and the kettle temperature is 70-80 ℃. The temperature of the tower bottom liquid of the diacid tower after heat exchange is reduced to 95-99 ℃, the tower bottom liquid enters the middle part of the triacid tower, a feeding liquid distributor of the three tower is not corroded, the rectification efficiency is high, and the purity (87%) of formic acid is high.
The invention also provides application of any one of the systems in waste heat utilization.
The invention has the beneficial effects that:
(1) the arrangement of the triacid tower reboiler B effectively recovers the residual heat of the tower bottom liquid of the diacid tower, and reduces water consumption and power consumption, thereby reducing energy consumption; the heat required by the tower kettle temperature rise of the triacid tower utilizes the residual heat of the tower kettle liquid of the diacid tower, reduces the using amount of heating steam of the triacid tower and reduces the energy consumption.
(2) Different from a pure waste heat recovery design, the method uses the waste heat of the tower bottom liquid of the diacid tower for heating the tower bottom of the triacid tower, thereby reducing the overall energy consumption of the equipment and improving the long-term operation stability; meanwhile, the problem that the purity of formic acid in the triacid tower is low, which is troubled for a long time at present in the production of 10-ten-thousand-ton-grade formic acid, is solved.
(3) The device has the advantages of simple structure, convenient operation, low cost, universality and easy large-scale production.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic structural view of embodiment 1 of the present invention; wherein, 1, diacid tower, 2, transmission pipeline, 3, triacid tower reboiler B, 4, triacid tower.
FIG. 2 is a diagram of a traditional production device for producing 10 ten thousand tons of formic acid per year, wherein the production device comprises a carbonyl reactor 1, a methyl ester reactor 2, a methyl ester rectifying tower, a methyl ester storage tank 4, a first hydrolyzer 5, a second hydrolyzer 6, a first acid tower 7, a second acid tower 8 and a third acid tower.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
As introduced in the background art, the method aims at the problems that the use amount of circulating water in the prior diacid tower is large, the temperature of a medium is high, and a circulating water heat exchanger is easy to scale. Therefore, the invention provides a process for recycling the residual heat of the tower bottom liquid of the diacid tower, so as to realize the efficient utilization of the residual heat of the tower bottom liquid of the diacid tower and be beneficial to saving energy.
The invention relates to a diacid tower bottom liquid waste heat recycling process, which comprises a main structure comprising a diacid tower, a triacid tower reboiler B and a conveying pipeline; the diacid tower kettle liquid is connected with the lower side of the shell pass of the reboiler of the triacid tower through a pipeline; the upper side of the shell side of the reboiler of the triacid tower is connected with the middle part of the triacid tower.
Further, the diacid tower is a pressurized rectifying tower (the operation pressure of a tower kettle is 290KPa-310KPa, the kettle temperature is 150-154 ℃); the triacid tower reboiler B is a vertical tube side thermosyphon reboiler.
Further, the triacid tower is a vacuum tower (the operation pressure at the top of the tower is-90 KPa-70KPa, and the temperature of the kettle is 70 ℃ -80 ℃).
A process for recycling the residual heat of the tower bottom liquid of a diacid tower mainly comprises a tower bottom liquid conveying system and a heat exchange system, wherein the tower bottom liquid of the diacid tower is heated through a triacid tower reboiler B, and then enters the middle part of a triacid tower for further rectification to obtain a product.
In some embodiments, the still bottoms transfer system comprises a diacid tower, a still bottoms transfer line.
In some embodiments, the heat exchange system comprises a triacid column reboiler B, a triacid column.
The invention also provides a process for recycling the residual heat of the tower bottom liquid of the diacid tower, which comprises the following specific steps:
(1) the diacid tower is heated by primary steam, the temperature and the pressure are raised to normal operation conditions, and tower bottom liquid of the diacid tower enters a triacid tower reboiler B for heat exchange through a conveying pipeline.
(2) And returning the diacid tower bottom liquid subjected to heat exchange by the triacid tower reboiler B to a conveying pipeline, and further rectifying the diacid tower bottom liquid in the middle of the triacid tower to obtain a product.
In some embodiments, the diacid tower kettle pressure is controlled at 290-310Kpa, and the kettle liquid temperature is controlled at 150-154 ℃; the pressure of the triacid tower is between 90 ℃ below zero and 70KPa below zero, and the temperature of the kettle liquid is controlled between 70 ℃ and 80 ℃. The conveying power is provided by the pressure difference between the diacid tower and the triacid tower.
The technical solution of the present invention will be described below with specific examples.
Example 1:
as shown in figure 1, the process for recycling the residual heat of the tower bottom liquid of the diacid tower comprises the steps that the tower bottom liquid (154 ℃) of a diacid tower 1 enters a triacid tower reboiler B3 through a conveying pipeline 2 to heat the tower bottom liquid of the triacid tower, and then the tower bottom liquid (98 ℃) of the diacid tower returns to the conveying pipeline 2 and enters the middle part of a triacid tower 4. And (4) utilizing the residual heat of the tower bottom liquid of the diacid tower.
The results of the one year production run show: the average purity of the formic acid in the triacid tower is 87%.
Example 2:
a diacid tower bottom waste heat recovery system comprises: the device comprises a diacid tower 1, a triacid tower 4 and a reboiler B3, wherein a liquid outlet of the tower kettle of the diacid tower 1 is connected with a shell side liquid inlet of a triacid tower reboiler B3, and a liquid outlet of a triacid tower reboiler B3 is connected with a liquid inlet in the middle of the triacid tower 4.
Aiming at the problems of large consumption and easy scaling of circulating water in the existing diacid tower 1. The tower bottom liquid of the diacid tower 1 is connected with the lower side of the shell pass of a reboiler B3 of the triacid tower through a pipeline 2, and is used as a heat source to heat the tower bottom of the triacid tower 4, so that the heat of the tower bottom liquid of the diacid tower 1 is effectively transferred to the triacid tower 4, the use amount of the circulating water of the diacid tower 1 and the scaling of the shell pass of a kettle liquid cooler are reduced, the use amount of heating steam of the triacid tower 4 is reduced, and the energy consumption is reduced.
More importantly, the method aims at the problem that the purity of formic acid (85%) produced by the existing 10 ten thousand ton formic acid production device is low. Through years of systematic, deep research and large-scale experimental investigation, the inventor discovers that: mainly because the long-period operation stability of the kettle liquid cooler of the existing diacid tower 1 is poor, sometimes the temperature of the kettle liquid entering the triacid tower 4 is too high, so that the corrosion of the feed liquid distributor of the triacid tower 4 (the triacid tower is corrosion-resistant below the temperature of 110 ℃, and the erosion corrosion is serious above the temperature) influences the distribution effect of the liquid of the three towers, causes bias current to influence the rectification effect, and inevitably causes influence on a formic acid finished product due to dissolved impurities. After the temperature of the tower bottom of the triacidic tower is increased by using the tower bottom liquid of the diacid tower as a heat source, the long-period operation stability of the formic acid production device is improved, and the purity (87%) of formic acid is improved.
Example 3:
a diacid tower bottom waste heat recovery system comprises: the device comprises a diacid tower 1, a triacid tower 4 and a reboiler B3, wherein a liquid outlet of the tower kettle of the diacid tower 1 is connected with a shell side liquid inlet of a triacid tower reboiler B3, and a liquid outlet of a triacid tower reboiler B3 is connected with a liquid inlet in the middle of the triacid tower 4.
The diacid tower 1 is also provided with a plurality of heat exchangers for heating (reboiler) or cooling (kettle cooler) the tower kettle liquid of the diacid tower, such as the heat exchangers on the left side and the right side of the diacid tower 1 in figure 1, so as to meet different use requirements of the kettle liquid.
Example 4:
a diacid tower bottom waste heat recovery system comprises: the device comprises a diacid tower 1, a triacid tower 4 and a reboiler B3, wherein a liquid outlet of the tower kettle of the diacid tower 1 is connected with a shell side liquid inlet of a triacid tower reboiler B3, and a liquid outlet of a triacid tower reboiler B3 is connected with a liquid inlet in the middle of the triacid tower 4.
The steam partial pressure of each substance is different under different pressures, and in order to obtain a better rectification effect, the diacid tower 1 is a pressurized rectification tower, the operating pressure of a tower kettle is 290KPa-310KPa, the kettle temperature is 150-154 ℃, and under the operating pressure and temperature, the separation rate and the purity of formic acid are high.
Example 5:
a diacid tower bottom waste heat recovery system comprises: the device comprises a diacid tower 1, a triacid tower 4 and a reboiler B3, wherein a liquid outlet of the tower kettle of the diacid tower 1 is connected with a shell side liquid inlet of a triacid tower reboiler B3, and a liquid outlet of a triacid tower reboiler B3 is connected with a liquid inlet in the middle of the triacid tower 4.
In the present invention, the type of the triacid tower reboiler B3 is not particularly limited as long as the heat exchange requirement between the bottom liquid of the diacid tower 1 and the triacid tower 4 can be satisfied, and therefore, in this embodiment, the triacid tower reboiler B3 is a vertical tube side thermosyphon reboiler, which improves the heat exchange efficiency and the formic acid purity.
Example 6:
a diacid tower bottom waste heat recovery system comprises: the device comprises a diacid tower 1, a triacid tower 4 and a reboiler B3, wherein a liquid outlet of the tower kettle of the diacid tower 1 is connected with a shell side liquid inlet of a triacid tower reboiler B3, and a liquid outlet of a triacid tower reboiler B3 is connected with a liquid inlet in the middle of the triacid tower 4.
The triacid tower 4 is a vacuum tower, the operation pressure at the top of the tower is-90 KPa-70KPa, the kettle temperature is 70-80 ℃, so that the purity of the formic acid from the diacid tower 1 is further improved, and the rectification efficiency is high.
Example 7:
a formic acid production apparatus comprising: diacid tower bottom waste heat recovery's system, wherein, diacid tower bottom waste heat recovery's system includes: the device comprises a diacid tower 1, a triacid tower 4 and a reboiler B3, wherein a liquid outlet of the tower kettle of the diacid tower 1 is connected with a shell side liquid inlet of a triacid tower reboiler B3, and a liquid outlet of a triacid tower reboiler B3 is connected with a liquid inlet in the middle of the triacid tower 4.
Aiming at the problems of large consumption and easy scaling of circulating water in the existing diacid tower 1. The tower bottom liquid of the diacid tower 1 is connected with the lower side of the shell pass of a reboiler B3 of the triacid tower through a pipeline 2, and is used as a heat source to heat the tower bottom of the triacid tower 4, so that the heat of the tower bottom liquid of the diacid tower 1 is effectively transferred to the triacid tower 4, the use amount of the circulating water of the diacid tower 1 and the scaling of the shell pass of a kettle liquid cooler are reduced, the use amount of heating steam of the triacid tower 4 is reduced, and the energy consumption is reduced.
More importantly, the method aims at the problem that the purity of formic acid (85%) produced by the existing 10 ten thousand ton formic acid production device is low. Through years of systematic, deep research and large-scale experimental investigation, the inventor discovers that: mainly because the long-period operation stability of the kettle liquid cooler of the existing diacid tower 1 is poor, sometimes the temperature of the kettle liquid entering the triacid tower 4 is too high, so that the corrosion of the feed liquid distributor of the triacid tower 4 (the triacid tower is corrosion-resistant below the temperature of 110 ℃, and the erosion corrosion is serious above the temperature) influences the distribution effect of the liquid of the three towers, causes bias current to influence the rectification effect, and inevitably causes influence on a formic acid finished product due to dissolved impurities. After the temperature of the tower bottom of the triacidic tower is increased by using the tower bottom liquid of the diacid tower as a heat source, the long-period operation stability of the formic acid production device is improved, and the purity (87%) of formic acid is improved.
The diacid tower 1 is also provided with a plurality of heat exchangers, and tower kettle liquid of the diacid tower is heated (a reboiler) or cooled (a kettle liquid cooler), so that different use requirements of the kettle liquid are met.
The steam partial pressure of each substance is different under different pressures, and in order to obtain a better rectification effect, the diacid tower 1 is a pressurized rectification tower, the operating pressure of a tower kettle is 290KPa-310KPa, the kettle temperature is 150-154 ℃, and under the operating pressure and temperature, the separation rate and the purity of formic acid are high.
In the present invention, the type of the triacid tower reboiler B3 is not particularly limited as long as the heat exchange requirement between the bottom liquid of the diacid tower 1 and the triacid tower 4 can be satisfied, and therefore, in this embodiment, the triacid tower reboiler B3 is a vertical tube side thermosyphon reboiler, which improves the heat exchange efficiency and the formic acid purity.
The triacid tower 4 is a vacuum tower, the operation pressure at the top of the tower is-90 KPa-70KPa, the kettle temperature is 70-80 ℃, so that the purity of the formic acid from the diacid tower 1 is further improved, and the rectification efficiency is high.
Different from the simple waste heat recovery, the method uses the waste heat of the tower bottom liquid of the diacid tower for heating the tower bottom of the triacid tower, thereby reducing the overall energy consumption of the equipment and improving the long-term operation stability; meanwhile, the problem that the purity of the formic acid (85%) in the triacid tower which is troubled by 10 ten thousand ton grade formic acid production for a long time at present is low is solved.
Example 8:
a method for recycling the residual heat of the tower bottom liquid of the diacid tower comprises the steps of heating the tower bottom liquid of the diacid tower through a reboiler B of the triacid tower, and rectifying the tower bottom liquid of the diacid tower into the middle part of the triacid tower to obtain a product.
In order to match the system, the residual heat of the tower bottom liquid of the diacid tower is efficiently transferred to the tower bottom of the triacid tower for heating, and the higher yield and purity of the formic acid are ensured. The invention carries out systematic optimization on the operation conditions of the tower kettle of the diacid tower and the triacid tower, and in some embodiments, the operation pressure of the tower kettle of the diacid tower is 290KPa to 310KPa, and the temperature of the tower kettle is 150 ℃ to 154 ℃. The operating pressure at the top of the triacid tower
The temperature is between 90KPa and 70KPa, and the kettle temperature is between 70 and 80 ℃. The temperature of the tower bottom liquid of the diacid tower after heat exchange is reduced to 95-99 ℃, the tower bottom liquid enters the middle part of the triacid tower, a feeding liquid distributor of the three tower is not corroded, the rectification efficiency is high, and the purity (87%) of formic acid is high.
Comparative example 1:
the traditional production device for producing 10 ten thousand tons of formic acid per year is adopted, the kettle liquid cooler is used for cooling the tower kettle liquid of the diacid tower, and other operation parameters are the same as those in the embodiment 1.
The results of the one year production run show: the average purity of the formic acid in the triacid tower is 85 percent.
It should be noted that the above-mentioned embodiments are only preferred embodiments of the present invention, and the present invention is not limited thereto, and although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications and equivalents can be made in the technical solutions described in the foregoing embodiments, or equivalents thereof. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention. Although the present invention has been described with reference to the specific embodiments, it should be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention.
Claims (10)
1. The utility model provides a diacid tower bottom waste heat recovery utilizes system which characterized in that includes: the device comprises a diacid tower, a triacid tower and a reboiler B, wherein a liquid outlet of a tower kettle of the diacid tower is connected with a shell pass liquid inlet of the reboiler B of the triacid tower, and a liquid outlet of the reboiler B of the triacid tower is connected with a liquid inlet in the middle of the triacid tower.
2. The diacid tower bottoms waste heat recovery system of claim 1 wherein the diacid tower is further provided with a plurality of reboilers.
3. The system for recycling the residual heat of the tower bottom liquid of the diacid tower as claimed in claim 1, wherein the diacid tower is a pressurized rectifying tower, the operating pressure of the tower bottom is 290KPa to 310KPa, and the temperature of the tower bottom is 150 ℃ to 154 ℃.
4. The system for recovering and utilizing the residual heat of the tower bottom liquid of the diacid tower as defined in claim 1, wherein the reboiler B of the triacid tower is a vertical tube side thermosiphon reboiler.
5. The system for recycling the residual heat of the tower bottom of the diacid tower as claimed in claim 1, wherein the triacid tower is a vacuum tower, the operation pressure of the tower top is-90 KPa-70KPa, and the temperature of the tower is 70-80 ℃.
6. A formic acid apparatus for producing, characterized by comprising: the system of any one of claims 1-5.
7. A method for recycling the residual heat of the tower bottom liquid of a diacid tower is characterized by comprising the following steps:
and (3) heating the tower bottom liquid of the diacid tower by a tower reboiler B of the triacid tower, and then rectifying the tower bottom liquid of the diacid tower in the middle of the triacid tower to obtain the product.
8. The method for recycling the residual heat of the tower bottom liquid of the diacid tower as claimed in claim 7, wherein the operation pressure of the tower bottom of the diacid tower is 290KPa to 310KPa, and the temperature of the tower bottom is 150 ℃ to 154 ℃.
9. The method for recycling the residual heat of the tower bottom of the diacid tower as claimed in claim 7, wherein the tower top operating pressure of the triacid tower is-90 KPa to 70KPa, and the kettle temperature is 70 ℃ to 80 ℃.
10. Use of the system according to any of claims 1-5 for waste heat utilization.
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| CN102952007A (en) * | 2012-11-19 | 2013-03-06 | 聊城煤杉新材料科技有限公司 | Production device capable of producing 100,000 tons of formic acid per unit per year |
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