CN101966398A - Energy-saving distillation method and device through differential pressure column section heat integration in rectification column sequences - Google Patents
Energy-saving distillation method and device through differential pressure column section heat integration in rectification column sequences Download PDFInfo
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Abstract
The invention relates to an energy-saving rectification device and method through differential pressure column section heat integration in rectification column sequences. The device comprises a light component boil-up column, a light component refining column rectification column section, an auxiliary condenser, a return tank, a flash tank, a light component refining column stripper section, an auxiliary reboiler and a main reboiler, wherein the light component boil-up column is used for pressurizing the light component refining column rectification column section; a top saturated vapor outlet pipe of the light component refining column rectification column section is connected to the heat media inlet of the main reboiler; the heat media outlet of the main reboiler is connected to the inlet of the auxiliary condenser; a bottom liquid outlet pipe is connected to the inlet of the return tank; a bottom liquid outlet pipe of the light component refining column stripper section is connected to the cold media inlet of the auxiliary reboiler and the cold media inlet of the main reboiler respectively; and the cold media outlets of the auxiliary reboiler and the main reboiler are respectively connected to a reboiled vapor inlet pipe of the light component refining column stripper section. The invention realizes single-column heat integration and matched heat exchange in the rectification column sequences. The invention realizes minimum heat consumption of the single column through differential pressure column section heat integration, even ensures the cold and heat load to be perfectly matched and ensures zero consumption, thus greatly reducing energy consumption of the system and achieving the aims of energy saving and synergy.
Description
Technical field
The present invention relates to distillation technology field and rectifying column system, especially, relate to a kind of rectifying column sequence differential pressure tower section 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.
Separate the conventional rectification sequence as shown in Figure 1 for existing multicomponent, when separating difficult separation mixture, required number of theoretical plate is more, causes the height of tower bigger; The operating reflux ratio of required tower is very big, causes the tower body 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.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 consumption 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 device and method.
A kind of rectifying column sequence of the present invention differential pressure tower section heat integration energy-saving rectifying device and method, this device comprise that light component steams tower, steam mixer, light component treating column rectifying column section, auxiliary condenser, return tank, flash tank, light component treating column and carries and heat up in a steamer tower section, auxiliary reboiler, main reboiler.Wherein: auxiliary condenser (19) is positioned between main reboiler (34) and the return tank (21); Flash tank (25) is positioned at the bottom of the light component treating column rectifying column section tower liquid outlet tube (23) and light component treating column and carries and heating up in a steamer between the tower section overhead liquid return duct (29); Auxiliary reboiler (32) is positioned at the light component treating column and carries and heating up in a steamer at the bottom of tower section (30) tower.
Described light component steams tower (2) the light component treating column rectifying column section (16) that is used to pressurize; Light component treating column rectifying column section cat head saturated vapor outlet (17) is connected to main reboiler (34) thermal medium import, and the thermal medium outlet is connected to return tank (21) import, and liquid outlet at the bottom of the tower (23) is connected to flash tank (25) import; Liquid outlet (31) was connected respectively to cold medium import of auxiliary reboiler (32) and the cold medium import of main reboiler (34) at the bottom of the light component treating column was carried and heated up in a steamer tower section tower, and cold media outlet is connected respectively to auxiliary reboiler steam outlet line (33) and main reboiler steam outlet line (35).
The method of operating of rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention is:
A) the light component treating column being divided into light component treating column rectifying column section and light component treating column carries and heats up in a steamer the tower section, wherein to steam the tower operating pressure identical for light component treating column rectifying column section and light component, and the light component treating column is carried the operating pressure that the operating pressure that heats up in a steamer the tower section is lower than light component treating column rectifying column section;
B) light component steams tower and is used to light component treating column rectifying column section that steam under pressure is provided;
C) liquid enters flash tank again at the bottom of the light component treating column rectifying column section tower after the pressure-reducing valve decompression;
D) the light component treating column is carried the operating pressure that the operating pressure that heats up in a steamer the tower section is lower than light component treating column rectifying column section, make the light component treating column carry to heat up in a steamer the tower section tower still material temperature of boiling again to be lower than light component treating column rectifying column section cat head material temperature, utilize the coupling heat exchange of these two strands of materials can realize hot integrated between two tower sections;
E) auxiliary condenser and auxiliary reboiler are used for the auxiliary even running that ensures whole system.
Concrete operation method is as follows:
Material liquid F enters the charging level that light component steams tower (2) through material liquid feeding line (1) under pressure reduction promotes, light component steams column overhead steam outlet pipe (6) and is connected to steam flow distributor (7) import; An outlet of steam flow distributor (7) is connected to the tower bottom steam inlet tube (15) of light component treating column rectifying column section, and another outlet is connected to flow control valve (8) inlet tube; Flow control valve (8) outlet, flash tank steam outlet pipe (26) and light component treating column are carried the overhead vapours outlet (36) that heats up in a steamer the tower section and are connected to steam mixer (9) import; Steam mixer (9) outlet is connected to interconderser (10) import; Interconderser (10) outlet is connected to liquid flux distributor (11) import; (11) outlets of liquid flux distributor are connected to the light component treating column and carry and heat up in a steamer tower section overhead liquid reflux pipeline (29), and another outlet is connected to force (forcing) pump (13) import; Force (forcing) pump (13) outlet is connected to light component and steams column overhead liquid return tube line (14); Phegma steams tower (2) along light component and enters liquid exit line (3) at the bottom of the tower after distributing, a liquid part enters light component and steams tower reboiler (4) at the bottom of the tower, the steam that boils again that forms enters light component along steam (vapor) outlet pipeline (5) and steams tower (2) bottom, and product extraction pipeline (37) was as bottom product B1 extraction at the bottom of another part liquid steamed Tata through light component.Light component treating column rectifying column section cat head saturated vapor outlet (17) is connected to main reboiler (34) thermal medium import, thermal medium outlet line (18) is connected to auxiliary condenser (19) import, auxiliary condenser (19) outlet is connected to return tank (21) import, the condensate liquid part of return tank outlet is through light component treating column rectifying column section overhead product extraction pipeline (39) extraction product D2, another part enters cat head through light component treating column rectifying column section overhead liquid reflux pipeline (22) as overhead reflux liquid, liquid liquid outlet tube (23) at the bottom of light component treating column rectifying column section tower enters pressure-reducing valve (24) at the bottom of the tower, and pressure-reducing valve (24) outlet is connected to flash tank (25) import; Flash tank steam outlet pipe (26) is connected to steam mixer (9) import; Flash tank liquid outlet tube (27) is connected to the light component treating column and carries and heat up in a steamer tower section overhead liquid reflux pipeline (29).Liquid outlet tube (31) was connected respectively to cold medium import of auxiliary reboiler (32) and the cold medium import of main reboiler (34) at the bottom of the light component treating column was carried and heated up in a steamer tower section tower, cold media outlet is connected respectively to auxiliary reboiler steam outlet line (33) and main reboiler steam outlet line (35), and liquid is carried by the light component treating column and heated up in a steamer tower section bottom product extraction pipeline (38) as product B 2 extraction at the bottom of a part of tower.
In operating process, if carrying less than the light component treating column, light component treating column rectifying column section (16) overhead condensation load heats up in a steamer required boiling hot again load at the bottom of tower section (30) tower, treating needs to move auxiliary reboiler (32) after system's operation operates steadily; Heat up in a steamer required boiling hot again load at the bottom of tower section (30) tower if light component treating column rectifying column section (16) overhead condensation load is carried greater than the light component treating column, treating needs to move auxiliary condenser (19) after system's operation operates steadily; If light component treating column rectifying column section (16) overhead condensation load equals the light component treating column just and carries and heat up in a steamer required boiling hot again load at the bottom of tower section (30) tower, treat can close auxiliary condenser (19) and auxiliary reboiler (32) after system's operation operates steadily, these two auxiliary equipment all need not operation.
The technology of the present invention unique distinction is: multicomponent is separated in the rectifying sequence light component treating column be split as light component treating column rectifying column section (16) and light component treating column and carry and heat up in a steamer tower section (30), light component treating column rectifying column section cat head saturated vapor outlet (17) is connected to main reboiler (34) thermal medium import, the thermal medium outlet is connected to return tank (21) import, and liquid outlet tube is connected to flash tank (25) import at the bottom of the tower; Flash tank steam outlet pipe (26) is connected to steam mixer (9) import, and flash tank liquid outlet tube (27) is connected to the light component treating column and carries and heat up in a steamer tower section overhead liquid reflux pipeline (29); Liquid outlet tube (31) was connected respectively to cold medium import of auxiliary reboiler (32) and the cold medium import of main reboiler (34) at the bottom of the light component treating column was carried and heated up in a steamer tower section tower, and cold media outlet is connected respectively to auxiliary reboiler steam outlet line (33) and main reboiler steam outlet line (35); Light component steams column overhead frozen-free device, is used to light component treating column rectifying column section that steam under pressure is provided; Light component steams column overhead part saturated vapor and light component treating column and carries and heat up in a steamer tower section cat head saturated vapor and also be connected to steam mixer (9) import; Steam mixer (9) outlet is connected to interconderser (10) import, interconderser (10) outlet is connected to liquid flux distributor (11) import, liquid flux distributor (11) outlet one end is connected to the light component treating column and carries and heat up in a steamer tower section overhead liquid reflux pipeline (29), and the other end is connected to light component and steams column overhead liquid return tube (14).
The technology of the present invention is multicomponent to be separated in the rectifying sequence light component treating column be split as light component treating column rectifying column section and light component treating column and carry and heat up in a steamer the tower section, wherein to steam the tower operating pressure identical for light component treating column rectifying column section and light component, the light component treating column is carried the operating pressure that the operating pressure that heats up in a steamer the tower section is lower than light component treating column rectifying column section, make the light component treating column carry to heat up in a steamer the tower section tower still material temperature of boiling again to be lower than light component treating column rectifying column section cat head material temperature, carry and heat up in a steamer the tower section tower still material that boils again thereby can utilize light component treating column rectifying column section cat head material condensation latent heat to heat the light component treating column, utilize the coupling heat exchange of these two strands of materials can realize hot integrated between two tower sections.Introduce auxiliary condenser and auxiliary reboiler in the flow process and be used for the auxiliary even running that ensures whole system, guarantee the realization of energy conservation object.
Separate the conventional rectification sequence with existing multicomponent and compare, the present invention has following advantage:
(1) the present invention steams the column overhead saturated vapor light component treating column rectifying column section that is used to pressurize with light component, carry and heat up in a steamer tower section bottoms material thereby make light component treating column rectifying column section overhead high pressure steam can be used in heating light component treating column, satisfy the demand of boiling again at the bottom of the tower.
(2) light component treating column rectifying column section cat head material condensation load can be put forward the thermic load of heating up in a steamer tower section tower bottom reboiler with the light component treating column and is complementary, and realizes that coupling heat exchange and single tower heat are integrated.
When (3) existing distillation technology separates difficult separation mixture usually power consumption rectifying column very big and that needs are very high realize that good product separates, the present invention can reduce tower height in the realization low energy consumption.
(4) heat loss is energy consumption main in the distillation operation, compares with existing distillation technology, and the present invention adopts the hot integrated approach of differential pressure tower section to realize the energy consumption of light component treating column minimum, even cooling and heating load can mate fully, and consumption is zero.And the mode that realizes this purpose is that light component is steamed the tower light component treating column rectifying column section that is used to pressurize, make the condensation latent heat of light component treating column rectifying column section overhead vapours can be used in heating light component treating column and carry and heat up in a steamer tower section tower bottom reboiler, increase a flash tank and auxiliary equipment simultaneously on stream.Adopt the inventive method, can avoid using expensive gas compressor on stream and the increase of the equipment investment expense that causes thus.
Rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method are compared with traditional multicomponent distillation and separation method, can reduce the total energy consumption of whole rectifying column system significantly, save operating cost, reach object of energy saving.Therefore, implement rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method and will produce very big economic benefit, have wide prospect in industrial application.
Description of drawings
Fig. 1 separates the schematic flow sheet of conventional rectification sequence for multicomponent
Among the schematic flow sheet figure of Fig. 2 for rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method: 1-material liquid feeding line, the 2-light component steams tower, the 3-light component steams liquid exit line at the bottom of the Tata, the 4-light component steams the tower reboiler, the 5-light component steams tower reboiler steam outlet line, the 6-light component steams column overhead steam (vapor) outlet pipeline, 7-steam flow distributor, the 8-flow control valve, the 9-steam mixer, the 10-interconderser, the 11-liquid flux distributor, 12-force (forcing) pump liquid-inlet pipeline, the 13-force (forcing) pump, the 14-light component steams column overhead liquid return tube line, 15-light component treating column rectifying column section tower bottom steam inlet line, 16-light component treating column rectifying column section, 17-light component treating column rectifying column section overhead vapours outlet, 18-master's reboiler thermal medium outlet line, the 19-auxiliary condenser, 20-return tank inlet line, the 21-return tank, 22-light component treating column rectifying column section overhead liquid reflux pipeline, liquid outlet tube at the bottom of the 23-light component treating column rectifying column section tower, the 24-pressure-reducing valve, the 25-flash tank, 26-flash tank steam (vapor) outlet pipeline, 27-flash tank liquid exit line, 28-liquid flux distributor outlet line, 29-light component treating column is carried and is heated up in a steamer tower section overhead liquid return duct, 30-light component treating column is carried and is heated up in a steamer the tower section, 31-light component treating column is carried and is heated up in a steamer liquid exit line at the bottom of the tower section tower, 32-assists reboiler, 33-assists the reboiler steam outlet line, 34-master's reboiler, 35-master's reboiler steam outlet line, 36-light component treating column are carried and are heated up in a steamer tower section overhead vapours outlet line, and the 37-light component steams product extraction pipeline at the bottom of the Tata, 38-light component treating column is carried and is heated up in a steamer tower section bottom product extraction pipeline, 39-light component treating column rectifying column section overhead product extraction pipeline.
The specific embodiment
The present invention is described in detail below in conjunction with accompanying drawing.
The present invention is achieved through the following technical solutions:
As shown in Figure 2, material liquid F enters the charging level that light component steams tower (2) through material liquid feeding line (1) under pressure reduction promotes, and light component steams column overhead steam outlet pipe (6) and is connected to steam flow distributor (7) import; An outlet of steam flow distributor (7) is connected to the tower bottom steam inlet tube (15) of light component treating column rectifying column section, and another outlet is connected to flow control valve (8) inlet tube; Flow control valve (8) outlet, flash tank steam outlet pipe (26) and light component treating column are carried the overhead vapours outlet (36) that heats up in a steamer the tower section and are connected to steam mixer (9) import; Steam mixer (9) outlet is connected to interconderser (10) import; Interconderser (10) outlet is connected to liquid flux distributor (11) import; (11) outlets of liquid flux distributor are connected to the light component treating column and carry and heat up in a steamer tower section overhead liquid reflux pipeline (29), and another outlet is connected to force (forcing) pump (13) import; Force (forcing) pump (13) outlet is connected to light component and steams column overhead liquid return tube line (14); Phegma steams tower (2) along light component and enters liquid exit line (3) at the bottom of the tower after distributing, a liquid part enters light component and steams tower reboiler (4) at the bottom of the tower, the steam that boils again that forms enters light component along steam (vapor) outlet pipeline (5) and steams tower (2) bottom, and product extraction pipeline (37) was as bottom product B1 extraction at the bottom of another part liquid steamed Tata through light component.Light component treating column rectifying column section cat head saturated vapor outlet (17) is connected to main reboiler (34) thermal medium import, thermal medium outlet line (18) is connected to auxiliary condenser (19) import, auxiliary condenser (19) outlet is connected to return tank (21) import, the condensate liquid part of return tank outlet is through light component treating column rectifying column section overhead product extraction pipeline (39) extraction product D2, another part enters cat head through light component treating column rectifying column section overhead liquid reflux pipeline (22) as overhead reflux liquid, liquid liquid outlet tube (23) at the bottom of light component treating column rectifying column section tower enters pressure-reducing valve (24) at the bottom of the tower, and pressure-reducing valve (24) outlet is connected to flash tank (25) import; Flash tank steam outlet pipe (26) is connected to steam mixer (9) import; Flash tank liquid outlet tube (27) is connected to the light component treating column and carries and heat up in a steamer tower section overhead liquid reflux pipeline (29).Liquid outlet tube (31) was connected respectively to cold medium import of auxiliary reboiler (32) and the cold medium import of main reboiler (34) at the bottom of the light component treating column was carried and heated up in a steamer tower section tower, cold media outlet is connected respectively to auxiliary reboiler steam outlet line (33) and main reboiler steam outlet line (35), and liquid is carried by the light component treating column and heated up in a steamer tower section bottom product extraction pipeline (38) as product B 2 extraction at the bottom of a part of tower.
In operating process, if carrying less than the light component treating column, light component treating column rectifying column section (16) overhead condensation load heats up in a steamer required boiling hot again load at the bottom of tower section (30) tower, treating needs to move auxiliary reboiler (32) after system operation operates steadily, and makes the light component treating column carry to heat up in a steamer the part of liquid phase at the bottom of the tower section tower and external heat-exchanging to satisfy the required whole thermic loads of rising steam at the bottom of the tower; If carrying greater than the light component treating column, light component treating column rectifying column section (16) overhead condensation load heats up in a steamer required boiling hot again load at the bottom of tower section (30) tower, treating needs to move auxiliary condenser (19) after system's operation operates steadily, make light component treating column rectifying column section overhead vapours reduce this burst material temperature with external heat-exchanging, to reduce to the temperature of the required withdrawing fluid of light component treating column rectifying column section cat head through the material stream (18) that main reboiler (34) cooling back forms; If light component treating column rectifying column section (16) overhead condensation load equals the light component treating column just and carries and heat up in a steamer required boiling hot again load at the bottom of tower section (30) tower, treat can close auxiliary condenser (19) and auxiliary reboiler (32) after system's operation operates steadily, these two auxiliary equipment all need not operation.
Auxiliary condenser (19) and auxiliary reboiler (32) are used for the auxiliary even running that ensures whole rectifying system, practical operation reach stable after, these two auxiliary equipment generally not can with the time move.
Technology of the present invention and device are widely used in all multicomponent rectifying separation processes, for the power savings advantages of the present invention in multicomponent rectifying field is described better, choose two case study on implementation below the present invention is illustrated, but therefore do not limit the scope of application of present technique and device.
Embodiment one (methyl alcohol, ethanol, propyl alcohol system separate)
Situation 1: methyl alcohol, ethanol, propyl alcohol system separate, and adopt flow process of the present invention.Inlet amount 1000kg/h, feed composition: methyl alcohol, 33.3% (wt%), ethanol, 33.3% (wt%), propyl alcohol, 33.4% (wt%), the feed heat situation is the bubble point charging.It is 60 that light component steams the tower number of theoretical plate, light component treating column rectifying column section and carry the number of theoretical plate that heats up in a steamer the tower section and respectively be 30.The operating pressure that light component steams tower and light component treating column rectifying column section is 1.50atm, and it is 0.58atm that the light component treating column is carried the operating pressure that heats up in a steamer the tower section.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column rectifying column section overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The light component treating column carries that to heat up in a steamer tower section overhead product produced quantity be 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).Light component treating column rectifying column section (16) overhead condensation load is carried less than the light component treating column and is heated up in a steamer required boiling hot again load at the bottom of tower section (30) tower in this situation, treating needs to move auxiliary reboiler (32) after system operation operates steadily, and makes the light component treating column carry to heat up in a steamer the part of liquid phase at the bottom of the tower section tower and external heat-exchanging to satisfy the required whole thermic loads of rising steam at the bottom of the tower.The main public work energy of this process consumes as shown in table 1.
Table 1 public work energy consumption
, technology of the present invention is separated the conventional rectification sequence with device with multicomponent among Fig. 1 compare in the technical advantage aspect the energy efficiency for ease of explanation the present invention.Feed rate, composition and feed heat situation are identical with the present invention in Fig. 1 flow process, and it is 60 that light component steams the tower number of theoretical plate, and light component treating column number of theoretical plate is 60.The operating pressure that light component steams tower and light component treating column is 1.50atm.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The bottom product produced quantity is 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).
Be used for the public work energy consumption of the Comparative Examples of embodiment one situation 1 contrast as shown in table 2.
Table 2 public work energy consumption
The energy consumption result of the embodiment of the invention one situation 1 and the energy consumption result of Comparative Examples are compared, and comparing result is as shown in table 3.
Table 3 public work energy consumption result contrast
By the public work energy consumption of table 3 correction data as a result, as can be seen, the light component treating column thermic load under embodiment one situation 1 condition has saved 87.8%, and light component treating column condensation load has saved 100.0%.To recently, system's total heat duties has saved 41.7% from the energy consumption of whole system, and the total condensation load of system has saved 40.6%.Therefore, adopt rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method, can reduce the public work consumption of process significantly, realize object of energy saving.
Situation 2: methyl alcohol, ethanol, propyl alcohol system separate, and adopt flow process of the present invention.Inlet amount 1000kg/h, feed composition: methyl alcohol, 33.3% (wt%), ethanol, 33.3% (wt%), propyl alcohol, 33.4% (wt%), the feed heat situation is the bubble point charging.It is 60 that light component steams the tower number of theoretical plate, light component treating column rectifying column section and carry the number of theoretical plate that heats up in a steamer the tower section and respectively be 30.The operating pressure that light component steams tower and light component treating column rectifying column section is 1.50atm, and it is 0.58atm that the light component treating column is carried the operating pressure that heats up in a steamer the tower section.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column rectifying column section overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The light component treating column carries that to heat up in a steamer tower section overhead product produced quantity be 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).Light component treating column rectifying column section (16) overhead condensation load is carried greater than the light component treating column and is heated up in a steamer required boiling hot again load at the bottom of tower section (30) tower in this situation, treating needs to move auxiliary condenser (19) after system's operation operates steadily, make light component treating column rectifying column section overhead vapours reduce this burst material temperature with external heat-exchanging, to reduce to the temperature of the required withdrawing fluid of light component treating column rectifying column section cat head through the material stream (18) that main reboiler (34) cooling back forms.The main public work energy of this process consumes as shown in table 4.
Table 4 public work energy consumption
, technology of the present invention is separated the conventional rectification sequence with device with multicomponent among Fig. 1 compare in the technical advantage aspect the energy efficiency for ease of explanation the present invention.Feed rate, composition and feed heat situation are identical with the present invention in Fig. 1 flow process, and it is 60 that light component steams the tower number of theoretical plate, and light component treating column number of theoretical plate is 60.The operating pressure that light component steams tower and light component treating column is 1.50atm.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The bottom product produced quantity is 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).
Be used for the public work energy consumption of the Comparative Examples of embodiment one situation 2 contrast as shown in table 5.
Table 5 public work energy consumption
The energy consumption result of the embodiment of the invention one situation 2 and the energy consumption result of Comparative Examples are compared, and comparing result is as shown in table 6.
Table 6 public work energy consumption result contrast
By the public work energy consumption of table 6 correction data as a result, as can be seen, the light component treating column thermic load under embodiment one situation 2 conditions has saved 100.0%, and light component treating column condensation load has saved 89.8%.To recently, system's total heat duties has saved 49.2% from the energy consumption of whole system, and the total condensation load of system has saved 48.0%.Therefore, adopt rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method, can reduce the public work consumption of process significantly, realize object of energy saving.
Situation 3: methyl alcohol, ethanol, propyl alcohol system separate, and adopt flow process of the present invention.Inlet amount 1000kg/h, feed composition: methyl alcohol, 33.3% (wt%), ethanol, 33.3% (wt%), propyl alcohol, 33.4% (wt%), the feed heat situation is the bubble point charging.It is 60 that light component steams the tower number of theoretical plate, light component treating column rectifying column section and carry the number of theoretical plate that heats up in a steamer the tower section and respectively be 30.The operating pressure that light component steams tower and light component treating column rectifying column section is 1.50atm, and it is 0.58atm that the light component treating column is carried the operating pressure that heats up in a steamer the tower section.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column rectifying column section overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The light component treating column carries that to heat up in a steamer tower section overhead product produced quantity be 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).Light component treating column rectifying column section (16) overhead condensation load equals the light component treating column just and carries and heat up in a steamer required boiling hot again load at the bottom of tower section (30) tower in this situation, treat can close auxiliary condenser (19) and auxiliary reboiler (32) after system's operation operates steadily, these two auxiliary equipment all need not operation.The main public work energy of this process consumes as shown in table 7.
Table 7 public work energy consumption
, technology of the present invention is separated the conventional rectification sequence with device with multicomponent among Fig. 1 compare in the technical advantage aspect the energy efficiency for ease of explanation the present invention.Feed rate, composition and feed heat situation are identical with the present invention in Fig. 1 flow process, and it is 60 that light component steams the tower number of theoretical plate, and light component treating column number of theoretical plate is 60.The operating pressure that light component steams tower and light component treating column is 1.50atm.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The bottom product produced quantity is 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).
Be used for the public work energy consumption of the Comparative Examples of embodiment one situation 3 contrast as shown in table 8.
Table 8 public work energy consumption
The energy consumption result of the embodiment of the invention one situation 3 and the energy consumption result of Comparative Examples are compared, and comparing result is as shown in table 9.
Table 9 public work energy consumption result contrast
By the public work energy consumption of table 9 correction data as a result, as can be seen, the light component treating column thermic load under embodiment one situation 3 conditions has saved 100.0%, and light component treating column condensation load has saved 100.0%.To recently, system's total heat duties has saved 49.2% from the energy consumption of whole system, and the total condensation load of system has saved 48.0%.Therefore, adopt rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method, can reduce the public work consumption of process significantly, realize object of energy saving.
Embodiment two (2-methylpentane, n-hexane, cyclohexane system separate)
Situation 1:2-methylpentane, n-hexane, cyclohexane system separate, and adopt flow process of the present invention.Inlet amount 1000kg/h, feed composition: the 2-methylpentane, 33.3% (wt%), n-hexane, 33.3% (wt%), cyclohexane, 33.4% (wt%), the feed heat situation is the bubble point charging.It is 80 that light component steams the tower number of theoretical plate, light component treating column rectifying column section and carry the number of theoretical plate that heats up in a steamer the tower section and respectively be 60.The operating pressure that light component steams tower and light component treating column rectifying column section is 1.50atm, and it is 0.58atm that the light component treating column is carried the operating pressure that heats up in a steamer the tower section.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column rectifying column section overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The light component treating column carries that to heat up in a steamer tower section overhead product produced quantity be 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).Light component treating column rectifying column section (16) overhead condensation load is carried less than the light component treating column and is heated up in a steamer required boiling hot again load at the bottom of tower section (30) tower in this situation, treating needs to move auxiliary reboiler (32) after system operation operates steadily, and makes the light component treating column carry to heat up in a steamer the part of liquid phase at the bottom of the tower section tower and external heat-exchanging to satisfy the required whole thermic loads of rising steam at the bottom of the tower.The main public work energy of this process consumes as shown in table 10.
Table 10 public work energy consumption
, technology of the present invention is separated the conventional rectification sequence with device with multicomponent among Fig. 1 compare in the technical advantage aspect the energy efficiency for ease of explanation the present invention.Feed rate, composition and feed heat situation are identical with the present invention in Fig. 1 flow process, and it is 80 that light component steams the tower number of theoretical plate, and light component treating column number of theoretical plate is 120.The operating pressure that light component steams tower and light component treating column is 1.50atm.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The bottom product produced quantity is 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).
Be used for the public work energy consumption of the Comparative Examples of embodiment two situations 1 contrast as shown in table 11.
Table 11 public work energy consumption
The energy consumption result of the embodiment of the invention two situations 1 and the energy consumption result of Comparative Examples are compared, and comparing result is as shown in table 12.
Table 12 public work energy consumption result contrast
By the public work energy consumption of table 12 correction data as a result, as can be seen, the light component treating column thermic load under embodiment two situations 1 condition has saved 89.2%, and light component treating column condensation load has saved 100.0%.To recently, system's total heat duties has saved 43.9% from the energy consumption of whole system, and the total condensation load of system has saved 42.6%.Therefore, adopt rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method, can reduce the public work consumption of process significantly, realize object of energy saving.
Situation 2:2-methylpentane, n-hexane, cyclohexane system separate, and adopt flow process of the present invention.Inlet amount 1000kg/h, feed composition: the 2-methylpentane, 33.3% (wt%), n-hexane, 33.3% (wt%), cyclohexane, 33.4% (wt%), the feed heat situation is the bubble point charging.It is 80 that light component steams the tower number of theoretical plate, light component treating column rectifying column section and carry the number of theoretical plate that heats up in a steamer the tower section and respectively be 60.The operating pressure that light component steams tower and light component treating column rectifying column section is 1.50atm, and it is 0.58atm that the light component treating column is carried the operating pressure that heats up in a steamer the tower section.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column rectifying column section overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The light component treating column carries that to heat up in a steamer tower section overhead product produced quantity be 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).Light component treating column rectifying column section (16) overhead condensation load is carried greater than the light component treating column and is heated up in a steamer required boiling hot again load at the bottom of tower section (30) tower in this situation, treating needs to move auxiliary condenser (19) after system's operation operates steadily, make light component treating column rectifying column section overhead vapours reduce this burst material temperature with external heat-exchanging, to reduce to the temperature of the required withdrawing fluid of light component treating column rectifying column section cat head through the material stream (18) that main reboiler (34) cooling back forms.The main public work energy of this process consumes as shown in table 13.
Table 13 public work energy consumption
, technology of the present invention is separated the conventional rectification sequence with device with multicomponent among Fig. 1 compare in the technical advantage aspect the energy efficiency for ease of explanation the present invention.Feed rate, composition and feed heat situation are identical with the present invention in Fig. 1 flow process, and it is 80 that light component steams the tower number of theoretical plate, and light component treating column number of theoretical plate is 120.The operating pressure that light component steams tower and light component treating column is 1.50atm.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The bottom product produced quantity is 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).
Be used for the public work energy consumption of the Comparative Examples of embodiment two situations 2 contrast as shown in table 14.
Table 14 public work energy consumption
The energy consumption result of the embodiment of the invention two situations 2 and the energy consumption result of Comparative Examples are compared, and comparing result is as shown in Table 15.
Table 15 public work energy consumption result contrast
By the public work energy consumption of table 15 correction data as a result, as can be seen, the light component treating column thermic load under embodiment two situations 2 conditions has saved 100.0%, and light component treating column condensation load has saved 90.1%.To recently, system's total heat duties has saved 46.5% from the energy consumption of whole system, and the total condensation load of system has saved 45.1%.Therefore, adopt rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method, can reduce the public work consumption of process significantly, realize object of energy saving.
Situation 3:2-methylpentane, n-hexane, cyclohexane system separate, and adopt flow process of the present invention.Inlet amount 1000kg/h, feed composition: the 2-methylpentane, 33.3% (wt%), n-hexane, 33.3% (wt%), cyclohexane, 33.4% (wt%), the feed heat situation is the bubble point charging.It is 80 that light component steams the tower number of theoretical plate, light component treating column rectifying column section and carry the number of theoretical plate that heats up in a steamer the tower section and respectively be 60.The operating pressure that light component steams tower and light component treating column rectifying column section is 1.50atm, and it is 0.58atm that the light component treating column is carried the operating pressure that heats up in a steamer the tower section.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column rectifying column section overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The light component treating column carries that to heat up in a steamer tower section overhead product produced quantity be 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).Light component treating column rectifying column section (16) overhead condensation load equals the light component treating column just and carries and heat up in a steamer required boiling hot again load at the bottom of tower section (30) tower in this situation, treat can close auxiliary condenser (19) and auxiliary reboiler (32) after system's operation operates steadily, these two auxiliary equipment all need not operation.The main public work energy of this process consumes shown in table 16.
Table 16 public work energy consumption
, technology of the present invention is separated the conventional rectification sequence with device with multicomponent among Fig. 1 compare in the technical advantage aspect the energy efficiency for ease of explanation the present invention.Feed rate, composition and feed heat situation are identical with the present invention in Fig. 1 flow process, and it is 80 that light component steams the tower number of theoretical plate, and light component treating column number of theoretical plate is 120.The operating pressure that light component steams tower and light component treating column is 1.50atm.Light component steams that the product produced quantity is 335kg/h at the bottom of the Tata, and the extraction product purity is controlled at more than 99.5% (wt%); Light component treating column overhead product produced quantity is 334.7kg/h, and the extraction product purity is controlled at more than 99.5% (wt%); The bottom product produced quantity is 330.3kg/h, and the extraction product purity is controlled at more than 99.5% (wt%).
Be used for the public work energy consumption of the Comparative Examples of embodiment two situations 3 contrast shown in table 17.
Table 17 public work energy consumption
The energy consumption result of the embodiment of the invention two situations 3 and the energy consumption result of Comparative Examples are compared, and comparing result is shown in table 18.
Table 18 public work energy consumption result contrast
By the public work energy consumption of table 18 correction data as a result, as can be seen, the light component treating column thermic load under embodiment two situations 3 conditions has saved 100.0%, and light component treating column condensation load has saved 100.0%.To recently, system's total heat duties has saved 50.9% from the energy consumption of whole system, and the total condensation load of system has saved 49.6%.Therefore, adopt rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device of the present invention and method, can reduce the public work consumption of process significantly, realize object of energy saving.
Rectifying column sequence differential pressure tower section 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 (6)
1. rectifying column sequence differential pressure tower section heat integration energy-saving rectificating method is characterized in that:
A) the light component treating column being divided into light component treating column rectifying column section and light component treating column carries and heats up in a steamer the tower section, wherein light component treating column rectifying column section is identical with the operating pressure that light component steams tower, and the light component treating column is carried the operating pressure that the operating pressure that heats up in a steamer the tower section is lower than light component treating column rectifying column section;
B) light component steams tower and is used to light component treating column rectifying column section that steam under pressure is provided;
C) liquid enters flash tank again at the bottom of the light component treating column rectifying column section tower after the pressure-reducing valve decompression;
D) the light component treating column is carried the operating pressure that the operating pressure that heats up in a steamer the tower section is lower than light component treating column rectifying column section, makes the light component treating column carry to heat up in a steamer the tower section tower still material temperature of boiling again to be lower than light component treating column rectifying column section cat head material temperature;
E) auxiliary condenser and auxiliary reboiler are used for the auxiliary even running that ensures whole system.
2. rectifying column sequence differential pressure tower section heat integration energy-saving rectifying device, this device comprise that light component steams tower (2), steam mixer (9), light component treating column rectifying column section (16), auxiliary condenser (19), return tank (21), flash tank (25), light component treating column and carries and heat up in a steamer tower section (30), auxiliary reboiler (32), main reboiler (34); It is characterized in that: auxiliary condenser (19) is positioned between main reboiler (34) and the return tank (21); Flash tank (25) is positioned at the bottom of the light component treating column rectifying column section tower liquid outlet tube (23) and light component treating column and carries and heating up in a steamer between the tower section overhead liquid return duct (29); Auxiliary reboiler (32) is positioned at the light component treating column and carries and heating up in a steamer at the bottom of tower section (30) tower.
3. device as claimed in claim 2 is characterized in that light component steams tower (2) the light component treating column rectifying column section (16) that is used to pressurize; Light component treating column rectifying column section cat head saturated vapor outlet (17) is connected to main reboiler (34) thermal medium import, and the thermal medium outlet is connected to return tank (21) import, and liquid outlet at the bottom of the tower (23) is connected to flash tank (25) import; Liquid outlet (31) was connected respectively to cold medium import of auxiliary reboiler (32) and the cold medium import of main reboiler (34) at the bottom of the light component treating column was carried and heated up in a steamer tower section tower, and cold media outlet is connected respectively to auxiliary reboiler steam outlet line (33) and main reboiler steam outlet line (35).
4. device as claimed in claim 3, the condition that it is characterized in that is as follows:
In operating process, when light component treating column rectifying column section (16) overhead condensation load was carried at the bottom of heating up in a steamer tower section (30) tower required boiling hot again load less than the light component treating column, the system that treats needed to move auxiliary reboiler (32) after operating and operating steadily;
5. as claim 3 or 4 described methods, the condition that it is characterized in that is as follows:
In operating process, when light component treating column rectifying column section (16) overhead condensation load was carried at the bottom of heating up in a steamer tower section (30) tower required boiling hot again load greater than the light component treating column, the system that treats needed to move auxiliary condenser (19) after operating and operating steadily;
6. as claim 3 or 4 described methods, the condition that it is characterized in that is as follows:
In operating process, when light component treating column rectifying column section (16) overhead condensation load equals the light component treating column just and carries at the bottom of heating up in a steamer tower section (30) tower required boiling hot again load, treat can close auxiliary condenser (19) and auxiliary reboiler (32) after system's operation operates steadily, these two auxiliary equipment all need not operation.
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| CN103524377A (en) * | 2013-09-12 | 2014-01-22 | 北京旭杰清能科技有限公司 | Cyclohexanone oxime refining method capable of saving energy through heat pump |
| CN104689591A (en) * | 2013-12-04 | 2015-06-10 | 陈小磊 | P-chlorobenzyl chloride distillation column |
| CN109661259A (en) * | 2016-09-08 | 2019-04-19 | 伊士曼化工公司 | For separating the method for being thermally integrated Distallation systm and use it of the ternary composition with heterogeneous azeotrope |
| CN110218143A (en) * | 2018-03-03 | 2019-09-10 | 榆林学院 | A kind of deep cooling transformation economic benefits and social benefits separation system in propylene production technology |
| 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 |
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| CN103524377A (en) * | 2013-09-12 | 2014-01-22 | 北京旭杰清能科技有限公司 | Cyclohexanone oxime refining method capable of saving energy through heat pump |
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| CN114728211A (en) * | 2019-12-12 | 2022-07-08 | 科思创德国股份有限公司 | Method for operating a distillation column |
| 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 |
| CN112169364A (en) * | 2020-09-29 | 2021-01-05 | 江苏博颂化工科技有限公司 | Fractionating tower heat pump system adopting external circulating working medium |
| CN114967600A (en) * | 2021-10-22 | 2022-08-30 | 天津理工大学 | Process dynamic control scheme based on paraffin separation dividing wall rectifying tower |
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