CN101874932A - Heat-integrated energy-saving rectification device and method - Google Patents
Heat-integrated energy-saving rectification device and method Download PDFInfo
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Abstract
本发明涉及一种热集成节能精馏装置及方法，该装置包括进料预热器、提馏段、精馏段、气体过热器、气体辅助过热器、压缩机、减压阀、主再沸器、辅助再沸器、蒸汽流量分配器、辅助冷凝器和回流罐等。本发明在实现精馏段和提馏段内部热集成的同时，将精馏段塔顶饱和蒸汽一部分用于预热进料，另一部分用于加热主再沸器和气体过热器，使整个精馏过程的热负荷消耗达到最小。一种理想情况是：整个精馏过程冷凝负荷和热负荷完全匹配，过程的能耗只有压缩机的压缩功消耗。本发明的一种全面热集成节能精馏方法及装置与传统的精馏分离系统相比，可大幅度降低整个精馏塔系统的总能耗，节省操作费用，达到节能增效的目的。
The invention relates to a heat-integrated energy-saving rectification device and method. The device includes a feed preheater, a stripping section, a rectification section, a gas superheater, a gas-assisted superheater, a compressor, a pressure reducing valve, and a main reboiler. device, auxiliary reboiler, steam flow distributor, auxiliary condenser and reflux tank, etc. In the present invention, while realizing heat integration in the rectification section and the stripping section, a part of the saturated steam at the top of the rectification section is used for preheating the feed, and the other part is used for heating the main reboiler and the gas superheater, so that the whole rectification section The heat load consumption of the distillation process is minimized. An ideal situation is: the condensing load and heat load of the whole rectification process are completely matched, and the energy consumption of the process is only the compression work consumption of the compressor. Compared with the traditional rectification separation system, the comprehensive heat-integrated energy-saving rectification method and device of the present invention can greatly reduce the total energy consumption of the entire rectification tower system, save operating costs, and achieve the purpose of energy saving and efficiency enhancement.
Description
Technical field
The present invention relates to distillation technology field and rectifying column system, especially, relate to a kind of heat integration energy-saving rectifying device and method.
Background technology
Rectifying is most widely used a kind of industrial process for separating in the present age, has been widely used in industrial departments such as chemical industry, oil, food, light industry.Though development of science and technology, new separation technology have begun commercial Application, in certain period, the dominant position of distillation technology can't be shaken.
Rectifying isolation technics maturation, easily industrialization, but shortcoming be consume energy very big.Traditional rectifying separates, and the input energy consumption accounts for more than 40% of industrial total energy consumption, and this is very important in energy 21 century in short supply day by day.
Scientist and engineers and technicians have proposed various Finestill energy-saving method according to the characteristics of rectifying.According to the distillation operation condition, rationally adjust operational factor; The integrated thought of utilization process energy is rationally utilized waste heat, waste gas; Develop various high efficiency rectifiying plates, filler, improve the rectifying separative efficiency; Research novel distillation technology is as multiple-effect rectifying, thermal coupling rectifying, heat pump distillation etc.These technology have improved the efficient that rectifying separation process energy utilizes, and have reached the purpose of energy efficient.
For existing distillation technology as shown in Figure 1, when separating difficult separation mixture, required number of theoretical plate is more, causes required tower height bigger; The operating reflux ratio of required tower is very big, causes required tower diameter bigger, and the required thermic load of tower bottom reboiler and the required condensation load of overhead condenser are bigger, so the energy consumption of tower is higher, and operating cost is also higher.Even for processes such as multiple-effect rectifying, thermal coupling rectifying, owing to the difference of thermic load at the bottom of overhead condensation load and the tower in the rectifying column system, also just the thermic load of system can not be mated to fall fully, the energy consumption of system can not be reduced to minimum.If can it be applied in the distillation process in conjunction with various technologies and technology, can make the overhead condensation load of process and tower at the bottom of thermic load reduce to minimum, realize saving energy and reduce the cost of distillation process, also can reduce production costs simultaneously, meaning is very great.
Summary of the invention
The present invention is directed to the high energy consumption problem of above-mentioned rectifying separation industries process, proposed a kind of low energy consumption, novel energy-saving rectifying method and device.
A kind of heat integration energy-saving rectifying device of the present invention and method, this device comprise feed preheater, stripping section, rectifying section, gas superheat device, the auxiliary superheater of gas, compressor, pressure-reducing valve, main reboiler, auxiliary reboiler, steam flow distributor, auxiliary condenser, return tank etc.
Feature of the present invention is: be provided with feed preheater (2) between material liquid pipeline and tower charging aperture; Stripping section (4) and rectifying section (18) can be plate column section, packing tower section or both combinations; Be provided with main reboiler (9), auxiliary reboiler (7) at the bottom of the stripping section tower between liquid outlet tube and tower bottom steam inlet tube; Be provided with the auxiliary superheater (15) of gas superheat device (14) and gas between stripping section overhead vapours outlet and compressor inlet tube; Compressor outlet gas enters the rectifying section bottom through rectifying section tower bottom steam inlet tube; Rectifying section top exit steam enters steam flow distributor (20) through rectifying section overhead vapor outlet; Be provided with auxiliary condenser (23) between feed preheater thermal medium outlet line, gas superheat device thermal medium outlet line and the return tank (24).
The method of operating of described heat integration energy-saving rectifying device:
A) a rectifying section cat head saturated vapor part is used to heat feed preheater (2), and another part is used to heat main reboiler (9) and gas superheater (14).
B) described auxiliary reboiler (7), the auxiliary superheater (15) of gas and auxiliary condenser (23) are used for auxiliary smooth starting and the even running that ensures rectifying column.
Following condition occurs, need the method for employing as follows:
Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, and auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can not make the stripping section tower, treat to close auxiliary condenser after system's operation operates steadily, but need auxiliary superheater of operation gas and auxiliary reboiler.
Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, but auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can make the stripping section tower, treat to close auxiliary condenser and auxiliary reboiler after system's operation operates steadily, but need the auxiliary superheater of operation gas.
Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, and auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can not make the stripping section tower, treat to close auxiliary condenser and the auxiliary superheater of gas after system's operation operates steadily, but need the auxiliary reboiler of operation.
When heat that the rectifying section overhead condensation provides just and at the bottom of the feed preheater thermic load, stripping section tower thermic load and the required thermic load of gas superheater be complementary, and auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can make the stripping section tower, treat can close auxiliary condenser, the auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, these three auxiliary equipment do not need operation.
Thermic load and the required thermic load sum of gas superheater at the bottom of heat that the rectifying section overhead condensation provides is greater than feed preheater thermic load, stripping section tower, but auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can make the stripping section tower, treat to close auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, but need the operation auxiliary condenser.
Unique distinction of the present invention is when realizing that rectifying section and stripping section internal heat are integrated, a rectifying section cat head saturated vapor part is used for preheated feed, another part is used to heat main reboiler and gas superheater, makes the thermic load consumption of whole rectifying process reach minimum.A kind of ideal situation is: whole rectifying process condensation load and thermic load are mated fully, and the energy consumption of whole process has only the work done during compression consumption of compressor.
A kind of heat integration energy-saving rectificating method of the present invention is compared with traditional distillation and separation method with device, can reduce the total energy consumption of whole rectifying column system significantly, saves operating cost, reaches object of energy saving.Therefore, implement a kind of heat integration energy-saving rectificating method of the present invention and will produce very big economic benefit, have wide prospect in industrial application with device.
Description of drawings
Fig. 1 is the schematic flow sheet of common rectifying tower;
Fig. 2 is the schematic flow sheet of heat integration energy-saving rectifying device of the present invention and method.
Among the figure: 1-material liquid feeding line, 2-feed preheater, 3-stripping section cat head feed pipe, the 4-stripping section, liquid outlet tube at the bottom of the 5-stripping section tower, the auxiliary reboiler liquid inlet of 6-pipeline, 7-assists reboiler, 8-master's reboiler liquid inlet pipeline, 9-master's reboiler, 10-stripping section bottom product extraction pipeline, 11-master's reboiler steam outlet, 12-assists the reboiler steam outlet, 13-stripping section overhead vapor outlet, 14-gas superheat device, 15-gas is assisted superheater, the 16-compressor, 17-rectifying section tower bottom steam inlet tube, 18-rectifying section, 19-rectifying section overhead vapor outlet, 20-steam flow distributor, 21-feed preheater thermal medium suction line, 22-feed preheater thermal medium outlet line, the 23-auxiliary condenser, the 24-return tank, 25-master's reboiler heating steam suction line, 26-gas superheat device thermal medium outlet line, 27-rectifying section overhead reflux liquid inlet tube, 28-rectifying section overhead product extraction pipeline, liquid exit line at the bottom of the 29-rectifying section tower, 30-pressure-reducing valve
The specific embodiment
The present invention is described in detail below in conjunction with accompanying drawing.
As shown in Figure 2, material liquid enters stripping section top along stripping section cat head feed pipe (3) by material liquid feeding line (1) after feed preheater (2) preheating.Material after liquid distribution trough is uniform enters the stripping section bottom along stripping section (4), liquid at the bottom of the tower is behind liquid outlet tube (5) at the bottom of the stripping section tower, a part enters auxiliary reboiler (7) through auxiliary reboiler liquid inlet pipeline (6), another part enters main reboiler (9) through main reboiler liquid inlet pipeline (8), and bottom product is through stripping section bottom product extraction pipeline (10) extraction.The saturated vapor part that the tower still produces is at the bottom of entering the stripping section tower behind the main reboiler steam outlet (11), and another part is at the bottom of entering the stripping section tower behind the auxiliary reboiler steam outlet (12).Rising steam enters stripping section overhead vapor outlet (13) through stripping section (4), behind gas superheat device (14) and the auxiliary superheater (15) of gas, enter gas compressor (16), gas after compressed machine (16) compression becomes superheated steam, enter the rectifying section bottom through rectifying section tower bottom steam inlet tube (17), rising steam enters steam flow distributor (20) along rectifying section (18) and rectifying section overhead vapor outlet (19).Steam part through steam flow distributor (20) enters feed preheater (2) along feed preheater thermal medium suction line (21), and the condensate liquid of formation enters auxiliary condenser (23) through feed preheater thermal medium outlet line (22) again; Master's reboiler (9) was used for heating tower's still feed liquid at the bottom of another part steam was introduced into tower along main reboiler heating steam suction line (25), entered gas superheat device (14) again and was used to heat stripping section cat head saturated vapor, made it become superheated steam; Through behind these two heat exchangers, this part rectifying section cat head saturated vapor is condensed into liquid, enters auxiliary condenser (23) through gas superheat device thermal medium outlet line (26) again.Material from feed preheater thermal medium outlet line (22) and gas superheater thermal medium outlet line (26) further enters return tank (24) after the cooling again through auxiliary condenser (23).A liquid part that goes out return tank (24) is returned the rectifying section top through rectifying section overhead reflux liquid inlet tube (27), another part through rectifying section overhead product extraction pipeline (28) as the overhead product extraction.The phegma that returns the rectifying section top enters liquid exit line (29) at the bottom of the rectifying section tower along rectifying section (18), behind pressure-reducing valve (30), returns the stripping section top along stripping section cat head feed pipe (3) again.
In operating process, thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, and the thermic load of two tower intersegmental parts exchange can not make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser after system's operation operates steadily, but need auxiliary superheater of operation gas and auxiliary reboiler; Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, but the thermic load of two tower intersegmental parts exchange can make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser and auxiliary reboiler after system's operation operates steadily, but need the auxiliary superheater of operation gas; Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, and the thermic load of two tower intersegmental parts exchange can not make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser and the auxiliary superheater of gas after system's operation operates steadily, but need the auxiliary reboiler of operation; When heat that the rectifying section overhead condensation provides is complementary with thermic load at the bottom of feed preheater thermic load, the stripping section tower and the required thermic load of gas superheater just, and the thermic load of two tower intersegmental parts exchange assists the reboiler thermic load to reduce to 0 at the bottom of can making the stripping section tower.Therefore, treat can close auxiliary condenser, the auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, these three auxiliary equipment do not need operation; Thermic load and the required thermic load sum of gas superheater at the bottom of heat that the rectifying section overhead condensation provides is greater than feed preheater thermic load, stripping section tower, but the thermic load of two tower intersegmental parts exchange can make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, but need the operation auxiliary condenser.
For the power savings advantages of further instruction the present invention, choose two case study on implementation below the present invention is illustrated in the rectifying field.
Embodiment one (separation of alcohols system)
Situation 1: ethanol-normal propyl alcohol system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 30 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The thermic load that the condensation of rectifying section cat head material provides in this situation less than feed preheater thermic load, stripping section tower at the bottom of thermic load and the required thermic load sum of gas superheater, and the thermic load of two tower intersegmental parts exchanges can not make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser after system's operation operates steadily, but need auxiliary superheater of operation gas and auxiliary reboiler.
It below is used public work price list.As shown in table 1.
Table 1 public work price
According to the public work price in the table 1, can draw the operating cost under embodiment one situation 1 condition, as shown in table 2.
Table 2 public work expense
According to the operating cost of main energy-dissipating device in the table 2, the annual total operation expense that can get under embodiment one situation 1 condition is 27673.83$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment one situation 1 contrast as shown in table 3.
Table 3 public work expense
According to the operating cost of main energy-dissipating device in the table 3, the annual total operation expense that can get common single tower distillation is 96619.34$/y.
The result of calculation of contrast table 2 and table 3, as can be seen, under embodiment one situation 1 condition annual total operation expense be 27673.83$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment one situation 1 contrast is 96619.34$/y.Therefore, the annual total operation expense under embodiment one situation 1 condition of employing the technology of the present invention and device has saved 71.36%, compares with the operating cost of existing common rectifying tower, can reduce the public work consumption of process significantly, saves operating cost.
Situation 2: ethanol-normal propyl alcohol system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 53 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The thermic load that the condensation of rectifying section cat head material provides in this situation less than feed preheater thermic load, stripping section tower at the bottom of thermic load and the required thermic load sum of gas superheater, but the thermic load of two tower intersegmental parts exchanges can make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser and auxiliary reboiler after system's operation operates steadily, but need the auxiliary superheater of operation gas.
According to the public work price in the table 1, can draw the operating cost under embodiment one situation 2 conditions, as shown in table 4.
Table 4 public work expense
According to the operating cost of main energy-dissipating device in the table 4, the annual total operation expense that can get under embodiment one situation 2 conditions is 21288.11$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment one situation 2 contrast as shown in table 5.
Table 5 public work expense
According to the operating cost of main energy-dissipating device in the table 5, the annual total operation expense that can get common single tower distillation is 90473.55$/y.
The result of calculation of contrast table 4 and table 5, as can be seen, under embodiment one situation 2 conditions annual total operation expense be 21288.11$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment one situation 2 contrast is 90473.55$/y.Therefore, the annual total operation expense under embodiment one situation 2 conditions of employing the technology of the present invention and device has saved 76.47%, compares with the operating cost of existing common rectifying tower, can reduce the public work consumption of process significantly, saves operating cost.
Situation 3: ethanol-normal propyl alcohol system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 58 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The thermic load that the condensation of rectifying section cat head material provides in this situation less than feed preheater thermic load, stripping section tower at the bottom of thermic load and the required thermic load sum of gas superheater, and the thermic load of two tower intersegmental parts exchanges can not make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser and the auxiliary superheater of gas after system's operation operates steadily, but need the auxiliary reboiler of operation.
According to the public work price in the table 1, can draw the operating cost under embodiment one situation 3 conditions, as shown in table 6.
Table 6 public work expense
According to the operating cost of main energy-dissipating device in the table 6, the annual total operation expense that can get under embodiment one situation 3 conditions is 19617.63$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment one situation 3 contrast as shown in table 7.
Table 7 public work expense
According to the operating cost of main energy-dissipating device in the table 7, the annual total operation expense that can get common single tower distillation is 89079.15$/y.
The result of calculation of contrast table 6 and table 7, as can be seen, under embodiment one situation 3 conditions annual total operation expense be 19617.63$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment one situation 3 contrast is 89079.15$/y.Therefore, the annual total operation expense under embodiment one situation 3 conditions of employing the technology of the present invention and device has saved 77.98%, compares with the operating cost of existing common rectifying tower, can reduce the public work consumption of process significantly, saves operating cost.
Situation 4: ethanol-normal propyl alcohol system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 62.5 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The heat that the rectifying section overhead condensation provides in this situation just is complementary with thermic load at the bottom of feed preheater thermic load, the stripping section tower and the required thermic load of gas superheater, and the thermic load of two tower intersegmental parts exchange assists the reboiler thermic load to reduce to 0 at the bottom of can making the stripping section tower.Therefore, treat can close auxiliary condenser, the auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, these three auxiliary equipment do not need operation.
According to the public work price in the table 1, can draw the operating cost under embodiment one situation 4 conditions, as shown in table 8.
Table 8 public work expense
According to the operating cost of main energy-dissipating device in the table 8, the annual total operation expense that can get under embodiment one situation 4 conditions is 17041.65$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment one situation 4 contrast as shown in table 9.
Table 9 public work expense
According to the operating cost of main energy-dissipating device in the table 9, the annual total operation expense that can get common single tower distillation is 87814.32$/y.
The result of calculation of contrast table 8 and table 9, as can be seen, under embodiment one situation 4 conditions annual total operation expense be 17041.65$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment one situation 4 contrast is 87814.32$/y.Therefore, the annual total operation expense under embodiment one situation 4 conditions of employing the technology of the present invention and device has saved 80.59%, compares with the operating cost of existing common rectifying tower, can reduce the public work consumption of process significantly, saves operating cost.
Situation 5: ethanol-normal propyl alcohol system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 80 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The heat that the rectifying section overhead condensation provides in this situation greater than feed preheater thermic load, stripping section tower at the bottom of thermic load and the required thermic load sum of gas superheater, but the thermic load of two tower intersegmental parts exchanges can make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, but need the operation auxiliary condenser.
According to the public work price in the table 1, can draw the operating cost under embodiment one situation 5 conditions, as shown in table 10.
Table 10 public work expense
According to the operating cost of main energy-dissipating device in the table 10, the annual total operation expense that can get under embodiment one situation 5 conditions is 17818.62$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment one situation 5 contrast as shown in table 11.
Table 11 public work expense
According to the operating cost of main energy-dissipating device in the table 11, the annual total operation expense that can get common single tower distillation is 82868.21$/y.
The result of calculation of contrast table 10 and table 11, as can be seen, under embodiment one situation 5 conditions annual total operation expense be 17818.62$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment one situation 5 contrast is 82868.21$/y.Therefore, the annual total operation expense under embodiment one situation 5 conditions of employing the technology of the present invention and device has saved 78.50%, compares with the operating cost of existing common rectifying tower, can reduce the public work consumption of process significantly, saves operating cost.
Embodiment two (separation of alkanes system)
Situation 1: cyclohexane-heptane system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 10 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The thermic load that the condensation of rectifying section cat head material provides in this situation less than feed preheater thermic load, stripping section tower at the bottom of thermic load and the required thermic load sum of gas superheater, and the thermic load of two tower intersegmental parts exchanges can not make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser after system's operation operates steadily, but need auxiliary superheater of operation gas and auxiliary reboiler.According to the public work price in the table 1, can draw the operating cost of embodiment two situations 1, as shown in table 12.
Table 12 public work expense
According to the operating cost of main energy-dissipating device in the table 12, the annual total operation expense that can get embodiment two situations 1 is 22859.74$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment two situations 1 contrast as shown in table 13.
Table 13 public work expense
According to the operating cost of main energy-dissipating device in the table 13, the annual total operation expense that can get common single tower distillation is 59824.86$/y.
The result of calculation of contrast table 12 and table 13, as can be seen, embodiment two situations 1 annual total operation expense be 22859.74$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment two situations 1 contrast is 59824.86$/y.Therefore, adopt the annual total operation expense of embodiment two situations 1 of the technology of the present invention and device to save 61.79%, compare, can reduce the public work consumption of process significantly, save operating cost with the operating cost of existing common rectifying tower.
Situation 2: cyclohexane-heptane system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 15 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The thermic load that the condensation of rectifying section cat head material provides in this situation less than feed preheater thermic load, stripping section tower at the bottom of thermic load and the required thermic load sum of gas superheater, but the thermic load of two tower intersegmental parts exchanges can make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser and auxiliary reboiler after system's operation operates steadily, but need the auxiliary superheater of operation gas.
According to the public work price in the table 1, can draw the operating cost of embodiment two situations 2, as shown in table 14.
Table 14 public work expense
According to the operating cost of main energy-dissipating device in the table 14, the annual total operation expense that can get embodiment two situations 2 is 22169.68$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment two situations 2 contrast as shown in Table 15.
Table 15 public work expense
According to the operating cost of main energy-dissipating device in the table 15, the annual total operation expense that can get common single tower distillation is 59373.24$/y.
The result of calculation of contrast table 14 and table 15, as can be seen, embodiment two situations 2 annual total operation expense be 22169.68$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment two situations 2 contrast is 59373.24$/y.Therefore, adopt the annual total operation expense of embodiment two situations 2 of the technology of the present invention and device to save 62.66%, compare, can reduce the public work consumption of process significantly, save operating cost with the operating cost of existing common rectifying tower.
Situation 3: cyclohexane-heptane system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 45 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The thermic load that the condensation of rectifying section cat head material provides in this situation less than feed preheater thermic load, stripping section tower at the bottom of thermic load and the required thermic load sum of gas superheater, and the thermic load of two tower intersegmental parts exchanges can not make the stripping section tower at the bottom of auxiliary reboiler thermic load reduce to 0.Therefore, treat to close auxiliary condenser and the auxiliary superheater of gas after system's operation operates steadily, but need the auxiliary reboiler of operation.
According to the public work price in the table 1, can draw the operating cost of embodiment two situations 3, shown in table 16.
Table 16 public work expense
According to the operating cost of main energy-dissipating device in the table 16, the annual total operation expense that can get embodiment two situations 3 is 17854.52$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment two situations 3 contrast shown in table 17.
Table 17 public work expense
According to the operating cost of main energy-dissipating device in the table 17, the annual total operation expense that can get common single tower distillation is 56614.52$/y.
The result of calculation of contrast table 16 and table 17, as can be seen, embodiment two situations 3 annual total operation expense be 17854.52$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment two situations 3 contrast is 56614.52$/y.Therefore, adopt the annual total operation expense of embodiment two situations 3 of the technology of the present invention and device to save 68.46%, compare, can reduce the public work consumption of process significantly, save operating cost with the operating cost of existing common rectifying tower.
Situation 4: cyclohexane-heptane system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 53.7 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The heat that the rectifying section overhead condensation provides in this situation just is complementary with thermic load at the bottom of feed preheater thermic load, the stripping section tower and the required thermic load of gas superheater, and the thermic load of two tower intersegmental parts exchange assists the reboiler thermic load to reduce to 0 at the bottom of can making the stripping section tower.Therefore, treat can close auxiliary condenser, the auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, these three auxiliary equipment do not need operation.The energy consumption of whole process has only the work done during compression consumption of compressor.
According to the public work price in the table 1, can draw the operating cost of embodiment two situations 4, shown in table 18.
Table 18 public work expense
According to the operating cost of main energy-dissipating device in the table 18, the annual total operation expense that can get embodiment two situations 4 is 16581.04$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment two situations 4 contrast shown in table 19.
Table 19 public work expense
According to the operating cost of main energy-dissipating device in the table 19, the annual total operation expense that can get common single tower distillation is 55798.91$/y.
The result of calculation of contrast table 18 and table 19, as can be seen, embodiment two situations 4 annual total operation expense be 16581.04$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment two situations 4 contrast is 55798.91$/y.Therefore, adopt the annual total operation expense of embodiment two situations 4 of the technology of the present invention and device to save 70.28%, compare, can reduce the public work consumption of process significantly, save operating cost with the operating cost of existing common rectifying tower.
Situation 5: cyclohexane-heptane system separates, and adopts flow process of the present invention.Feed entrance point is the stripping section cat head, and inlet amount 1000kg/h, feed composition respectively are 50% (wt%), and feeding temperature is 70 ℃.Inside and outside two tower section number of theoretical plates respectively are 20.The stripping section operating pressure is a normal pressure, and the rectifying section operating pressure is 0.253Mpa.Rectifying section overhead product produced quantity is 500kg/h, and the extraction product purity is controlled at more than 99% (wt%).The thermic load that the condensation of rectifying section cat head material provides in this situation is greater than the required thermic load sum of feed preheater, main reboiler and gas superheater.Therefore, need to open auxiliary condenser, to guarantee the even running of system.The auxiliary superheater of auxiliary reboiler and gas does not need operation in this situation.
According to the public work price in the table 1, can draw the operating cost of embodiment two situations 5, shown in table 20.
Table 20 public work expense
According to the operating cost of main energy-dissipating device in the table 20, the annual total operation expense that can get embodiment two situations 5 is 16714.57$/y.
, in the technical advantage aspect the energy efficiency technology of the present invention and device and common rectifying tower are compared for ease of explanation the present invention.Common single tower distillation, 40 of tower number of theoretical plates, feed entrance point are the 20th theoretical plate.Feed rate, composition and temperature are identical with the present invention, and the operating pressure of tower is a normal pressure.The flow of extraction product is also identical with the present invention with purity.
Be used for the public work expense of the common rectifying tower of embodiment two situations 5 contrast shown in table 21.
Table 21 public work expense
According to the operating cost of main energy-dissipating device in the table 21, the annual total operation expense that can get common single tower distillation is 54270.33$/y.
The result of calculation of contrast table 20 and table 21, as can be seen, the annual total operation expense of embodiment two situations 5 is 16714.57$/y, and the annual total operation expense that is used for the common rectifying tower of embodiment two situations 5 contrast is 54270.33$/y.Therefore, adopt the annual total operation expense of embodiment two situations 5 of the technology of the present invention and device to save 69.20%, compare, can reduce the public work consumption of process significantly, save operating cost with the operating cost of existing common rectifying tower.
Technology of the present invention and device are extensively to be suitable for for distillation process, and for the separation of the less system of relative volatility, its energy-saving effect will be better, will produce bigger economic benefit.
A kind of heat integration energy-saving rectifying device and method that the present invention proposes, be described by preferred embodiment, person skilled obviously can be in not breaking away from content of the present invention, spirit and scope to device as herein described with method of operating is changed or suitably change and combination, realize the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to one skilled in the artly, they all can be regarded as being included in spirit of the present invention, scope and the content.
Claims (8)
1. a heat integration energy-saving rectifying device is characterized in that comprising feed preheater, stripping section, rectifying section, gas superheat device, the auxiliary superheater of gas, compressor, pressure-reducing valve, main reboiler, auxiliary reboiler, steam flow distributor, auxiliary condenser and return tank; Feed preheater (2) is between material liquid pipeline and tower charging aperture; Main reboiler (9) and auxiliary reboiler (7) are positioned at the bottom of the stripping section tower between liquid outlet tube and tower bottom steam inlet tube; The auxiliary superheater (15) of gas superheat device (14) and gas is positioned between stripping section overhead vapours outlet and compressor inlet tube; Compressor outlet gas enters the rectifying section bottom through rectifying section tower bottom steam inlet tube; Rectifying section top exit steam enters steam flow distributor (20) through rectifying section overhead vapor outlet; Auxiliary condenser (23) is positioned between feed preheater thermal medium outlet line, gas superheat device thermal medium outlet line and the return tank (24).
2. device as claimed in claim 1 is characterized in that stripping section (4) and rectifying section (18) are plate column section, packing tower section or both combinations.
3. the method for operating of device as claimed in claim 1 or 2 is characterized in that:
A) a rectifying section cat head saturated vapor part is used to heat feed preheater (2), and another part is used to heat main reboiler (9) and gas superheater (14).
B) described auxiliary reboiler (7), the auxiliary superheater (15) of gas and auxiliary condenser (23) are used for auxiliary smooth starting and the even running that ensures rectifying column.
4. the method for operating of device as claimed in claim 3 is characterized in that:
Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, and auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can not make the stripping section tower, treat to close auxiliary condenser after system's operation operates steadily, but need auxiliary superheater of operation gas and auxiliary reboiler.
5. the method for operating of device as claimed in claim 3 is characterized in that:
Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, but auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can make the stripping section tower, treat to close auxiliary condenser and auxiliary reboiler after system's operation operates steadily, but need the auxiliary superheater of operation gas.
6. the method for operating of device as claimed in claim 3 is characterized in that:
Thermic load and the required thermic load sum of gas superheater at the bottom of thermic load that the condensation of rectifying section cat head material provides is less than feed preheater thermic load, stripping section tower, and auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can not make the stripping section tower, treat to close auxiliary condenser and the auxiliary superheater of gas after system's operation operates steadily, but need the auxiliary reboiler of operation.
7. the method for operating of device as claimed in claim 3 is characterized in that:
When heat that the rectifying section overhead condensation provides just and at the bottom of the feed preheater thermic load, stripping section tower thermic load and the required thermic load of gas superheater be complementary, and auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can make the stripping section tower, treat to close auxiliary condenser, the auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, these three auxiliary equipment do not need operation.
8. the method for operating of device as claimed in claim 3 is characterized in that:
Thermic load and the required thermic load sum of gas superheater at the bottom of heat that the rectifying section overhead condensation provides is greater than feed preheater thermic load, stripping section tower, but auxiliary reboiler thermic load reduced at 0 o'clock at the bottom of the thermic load of two tower intersegmental parts exchange can make the stripping section tower, treat to close auxiliary superheater of gas and auxiliary reboiler after system's operation operates steadily, but need the operation auxiliary condenser.
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| CN103524351A (en) * | 2013-10-17 | 2014-01-22 | 青岛科技大学 | Device and method for removing trimethylamine in production process of glycine betaine |
| CN108007068A (en) * | 2018-01-07 | 2018-05-08 | 中国科学院工程热物理研究所 | A kind of LNG cold energy uses are thermally integrated rectifying space division system |
| CN110180205A (en) * | 2019-04-28 | 2019-08-30 | 天津大学 | A kind of rectifying tower system corollary apparatus and method that new internal energy is integrated |
| CN111548243A (en) * | 2020-05-06 | 2020-08-18 | 天津市汇筑恒升科技有限公司 | Heat integration energy-saving process in device for synthesizing cyclohexanone by cyclohexene method |
| CN111686469A (en) * | 2020-06-12 | 2020-09-22 | 天津大学 | Middle steam compression two-section partition tower |
| CN112774236A (en) * | 2020-12-10 | 2021-05-11 | 大连理工大学 | Shell-and-tube active gas phase distributor |
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| CN103524351A (en) * | 2013-10-17 | 2014-01-22 | 青岛科技大学 | Device and method for removing trimethylamine in production process of glycine betaine |
| CN103524351B (en) * | 2013-10-17 | 2015-07-08 | 青岛科技大学 | A device and method for removing trimethylamine in betaine production process |
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| CN110180205A (en) * | 2019-04-28 | 2019-08-30 | 天津大学 | A kind of rectifying tower system corollary apparatus and method that new internal energy is integrated |
| CN110180205B (en) * | 2019-04-28 | 2021-02-12 | 天津大学 | Novel rectification tower system matching device and method with internal energy integration |
| CN111548243A (en) * | 2020-05-06 | 2020-08-18 | 天津市汇筑恒升科技有限公司 | Heat integration energy-saving process in device for synthesizing cyclohexanone by cyclohexene method |
| CN111686469A (en) * | 2020-06-12 | 2020-09-22 | 天津大学 | Middle steam compression two-section partition tower |
| CN112774236A (en) * | 2020-12-10 | 2021-05-11 | 大连理工大学 | Shell-and-tube active gas phase distributor |
| CN113521784A (en) * | 2021-07-05 | 2021-10-22 | 内蒙古工业大学 | A micro-distillation heat integrated system |
| CN113521784B (en) * | 2021-07-05 | 2023-01-06 | 内蒙古工业大学 | Micro-rectification heat integration system |
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