CN100584421C - Differential pressure low-energy-consumption distillation method and equipment - Google Patents
Differential pressure low-energy-consumption distillation method and equipment Download PDFInfo
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- CN100584421C CN100584421C CN200710150233A CN200710150233A CN100584421C CN 100584421 C CN100584421 C CN 100584421C CN 200710150233 A CN200710150233 A CN 200710150233A CN 200710150233 A CN200710150233 A CN 200710150233A CN 100584421 C CN100584421 C CN 100584421C
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Abstract
The present invention provides a rectifying method having differential pressure and lower energy consumption, and an apparatus, including a general knockout tower section, a underpressure knockout tower section, a main reboiler, a reflux accumulator and a compressor, wherein , a compressor is set between the underpressure knockout tower section and the general knockout tower section, the gas material tube on the top of the underpressure knockout tower section is connected to the inlet of the compressor, the outlet of the compressor is connected to the gas inlet ont the bottom of the general knockout tower section; gas material outlet of the general knockout tower section is connected to the heat medium inlet of the main reboiler, heating medium outlet is connected to the reflux accumulator of the general knockout tower section; the liquid outlet on the bottom of the general knockout tower section is connected to the liquid inlet of the underpressure knockout tower section; the liquid material outlet tube on the bottom of the underpressure knockout tower section is connected to the cooling medium inlet of the main reboiler, outlet of the cooling medium is connected to the inlet of the reboiler of the underpressure knockout tower section. The invention realises thermally coupled distillation, matching heat exchange. The minimum heat consumption is realised by differential pressure temperature reduction means, even the cool-heat load are fully matched, the consumption is zero. Ways to achieve the aim only is adding a compressor in the equipment, the dynamic consumption is lower than the original consumption.
Description
Technical field
The present invention relates to the distillation technology field, particularly relate to a kind of differential pressure low-energy-consumption distillation method and equipment of suitable highly energy-consuming fine chemical process process.
Background technology
Rectifying is a kind of widely used chemical separating unit operations, but the distillation process energy consumption is huge, and the capacity usage ratio that improves distillation process is the focus of research all the time.
In recent years, thermocouple rectifying was because not only energy-conservation but also save the extensive concern that equipment investment has caused people.Thermocouple rectifying the earliest is to be proposed by Petlyuk before 50 years, discovers that thermocouple rectifying is more energy-conservation more than at least 30% than conventional rectification process, but limit by at that time technical conditions and be difficult to industrialization.In recent years, owing to energy prices rise steadily, along with raising to energy-conservation requirement, and because the raising of control technology, the research of thermocouple rectifying aspect is tending towards active again, and some major companies have incited somebody to action partition wall rectifying column industrialization wherein.For some given material, the partition wall rectifying column compare with the conventional rectification flow process need be littler reflux ratio, so increased operation capacity.Energy-conservation can reach more than 60% can be economized equipment investment 30%.The partition wall rectifying column can be widely used in petroleum refinement, petrochemical industry, chemicals and gas purification.
No matter existing thermocouple distillation technology still is equipment from flow process, the restriction of lift operations on the steam of not breaking away from still that needed overhead condensation liquid in the distillation process refluxes and the tower still boils again.No matter be to adopt to presort tower design, middle side line heat exchange, side line and distill flow process or side line and carry and heat up in a steamer flow process, for main distillation column, because tower top temperature will be higher than column bottom temperature, be that the condensed temperature of cat head material will be higher than the temperature that the bottoms material boils and will reach, thereby can not mate heat exchange simply between overhead condenser and the tower bottom reboiler, also just can not realize thermal coupling completely.
If can be implemented in complete thermal coupling in the distillation process by various means, the purpose that really reach energy-saving and cost-reducing, reduces product cost then is quite huge for the impetus of China's oil chemical industry development.
Summary of the invention
The present invention to realize that least energy consumption is a purpose, proposes a kind of novel thermocouple distillation process-differential pressure low-energy-consumption distillation method and equipment by various thermocouple distillation processes are furtherd investigate.
Differential pressure low-energy-consumption distillation equipment of the present invention, include conventional knockout tower section, step-down knockout tower section, main reboiler, backflow storage tank and compressor, wherein: between conventional knockout tower section and step-down knockout tower section, be provided with a compressor, the vapor-phase material pipe of step-down knockout tower section cat head is connected to compressor inlet, and the compressor outlet pipe is connected to the vapour phase feed pipe at the bottom of the conventional knockout tower section tower; The vapor-phase material outlet at conventional knockout tower section top is connected to the import of main reboiler thermal medium, and the thermal medium outlet is connected to the backflow storage tank of conventional knockout tower section; The outlet of conventional knockout tower section bottom liquid phases is connected to the liquid phase import at step-down knockout tower section top; The liquid phase material outlet of step-down knockout tower section bottom is connected to the cold medium import of main reboiler, and cold media outlet is connected to the steam inlet of boiling again of step-down knockout tower section.
Be provided with an auxiliary reboiler at the bottom of the described step-down knockout tower section tower.
Be provided with auxiliary condenser between described main reboiler and the backflow storage tank.
The method of operating of differential pressure low-energy-consumption distillation equipment of the present invention is:
A) common rectifying column is divided into conventional knockout tower section and step-down knockout tower section, wherein conventional knockout tower section is identical with the single tower distillation operating pressure or a little more than single tower operating pressure, step-down knockout tower section adopts reduced pressure operation;
B) step-down knockout tower section adopts reduced pressure operation, and step-down knockout tower section overhead vapours reaches through compressor compresses and enters conventional knockout tower section after requiring at the bottom of the conventional knockout tower section tower;
C) reduced pressure operation of step-down knockout tower section makes its tower still material temperature of boiling again be lower than conventional segregation section cat head material temperature, thereby utilizes the coupling heat exchange of these two strands of materials to realize two thermal couplings between the tower section.
Concrete operation method is as follows: liquid phase material 11 enters step-down knockout tower section 12 tops at the bottom of the tower after separating through conventional knockout tower section 1 under pressure reduction promotes; After pressurizeing by compressor 14, the steam 13 that comes out in step-down knockout tower section top enters conventional knockout tower section bottom as rising steam 15; Liquid phase 16 parts of coming out at the bottom of the step-down knockout tower section tower can be used as product extraction 20, another part 17 carries out heat exchange with the steam 2 that conventional knockout tower section cat head comes out in main reboiler 3, the required steam 18 that boils again at the bottom of the formation step-down knockout tower section tower, if condensation load less than main reboiler, needs to open simultaneously auxiliary reboiler 22; Conventional knockout tower section overhead vapours 2 obtains part or all of condensate liquid 4 through after the heat exchange, when condensation load during greater than main reboiler, need to open the auxiliary condenser 5 that this partial condensation liquid 4 is flowed through, the condensate liquid 6 that obtains needed backflow of conventional knockout tower section cat head and extraction enters backflow storage tank 7, condensate liquid 8 parts that flow out from the backflow storage tank are as product 9 extraction, and another part is as the overhead reflux liquid 10 of conventional knockout tower section.
Described auxiliary condenser 5 and 22 operations of auxiliary reboiler, after stable, can select one as supplementary energy equipment according to the heat coupling, steam can mate fully if boil at the bottom of conventional knockout tower section overhead condensation and the step-down knockout tower section tower in the flow scheme design again, and then two auxiliary equipment all need not to open.
Distinctive feature of the present invention is: common rectifying column is divided into conventional knockout tower section and step-down knockout tower section, the vapor-phase material pipe of step-down knockout tower section cat head is connected to compressor inlet, and the compressor outlet pipe is connected to the vapour phase feed pipe at the bottom of the conventional knockout tower section tower; The vapor-phase material outlet of conventional knockout tower section cat head is connected to the import of main reboiler thermal medium, the thermal medium outlet is connected to the auxiliary condenser import, the auxiliary condenser outlet is connected to the backflow storage tank of conventional knockout tower section, the backflow storage tank exports an end liquid phase extraction, and an end is connected to conventional knockout tower section overhead reflux material inlet; The liquid phase outlet is connected to the liquid phase import of step-down knockout tower section cat head at the bottom of the conventional knockout tower section tower; Liquid phase outlet at the bottom of the step-down knockout tower section tower is divided into two branch roads, article one, branch road links to each other with the cold medium import of main reboiler, cold media outlet end is connected to the liquid-inlet that boils again at the bottom of the step-down knockout tower section tower, and another branch road connects discharge nozzle, also can connect an auxiliary reboiler as required.
This technology is common rectifying column to be divided into conventional separation separate two tower sections with step-down, the operating pressure of wherein conventional knockout tower section is identical with the single tower distillation operating pressure or a little more than single tower operating pressure, and step-down knockout tower section adopts reduced pressure operation, reduce column bottom temperature, thereby can utilize the latent heat of conventional rectification tower section overhead condensation to realize the heating of boiling again of step-down knockout tower section bottoms material.Step-down knockout tower section overhead vapours enters conventional knockout tower section through compressor compresses, and liquid promotes to enter step-down knockout tower section by pressure reduction at the bottom of the conventional knockout tower section tower.Step-down knockout tower section reduced pressure operation can material temperature be lower than conventional knockout tower section cat head material temperature so that its tower still boils again, thereby the coupling heat exchange that utilizes these two strands of materials realizes the thermal coupling of two towers, and utilize auxiliary condenser and auxiliary reboiler to realize the coupling fully of whole rectifying process energy consumption, realize energy-conservation target.
Compared with prior art, the present invention has following advantage:
[1] load of conventional knockout tower section overhead condensation can be complementary with the load of reboiler at the bottom of the step-down knockout tower section under the step-down, realizes thermocouple rectifying, the coupling heat exchange.
[2] different with conventional rectification, conventional knockout tower section top rising steam can be used in heating step-down knockout tower section bottoms material after overcompression, satisfy the requirement of boiling again at the bottom of the tower.
[3] heat loss is the main energy consumption place in the distillation operation, and the present invention has compared with prior art realized minimum heat loss with differential pressure cooling means substantially, even cooling and heating load can mate fully, and consumption is zero.And the means that realize this purpose only are to increase by a compressor in equipment, and this power consumption is little a lot of with respect to original heat loss.
Usually need very high rectifying column to realize that good product separates when [4] existing distillation technology separates the highly energy-consuming fine chemicals, the present invention can reduce tower height when realizing low energy consumption.
Description of drawings
Fig. 1 is the schematic flow sheet of differential pressure low-energy-consumption distillation technology.
The specific embodiment
Below in conjunction with accompanying drawing technology and equipment provided by the present invention is further detailed.
The present invention is achieved through the following technical solutions:
As shown in Figure 1, under promoting, pressure reduction enters step-down knockout tower section 12 tops through liquid phase material at the bottom of the tower after conventional knockout tower section 1 separation; After pressurizeing by compressor 14, the steam 13 that comes out in step-down knockout tower section top enters conventional knockout tower section bottom as rising steam 15; Liquid phase 16 parts of coming out at the bottom of the step-down knockout tower section tower can be used as product extraction 20, another part 17 carries out heat exchange with the steam 2 that conventional knockout tower section cat head comes out in main reboiler 3, the required steam 18 that boils again at the bottom of the formation step-down knockout tower section tower, if condensation load during less than main reboiler, needs to open simultaneously auxiliary reboiler 22; Conventional knockout tower section overhead vapours 2 obtains part or all of condensate liquid 4 through after the heat exchange, when condensation load during greater than main reboiler, need to open the auxiliary condenser 5 that this partial condensation liquid 4 is flowed through, thereby the condensate liquid 6 that obtains needed backflow of conventional knockout tower section cat head and extraction enters backflow storage tank 7, condensate liquid 8 parts that flow out from the backflow storage tank are as product 9 extraction, and another part is as the overhead reflux liquid 10 of conventional knockout tower section.
During institute's calorific requirement can provide greater than conventional knockout tower section overhead condensation if step-down knockout tower section bottoms material boils again in operating process heat, then need to open simultaneously auxiliary reboiler 22, make come out at the bottom of a step-down knockout tower section tower part 21 and the external heat-exchanging of liquid phase satisfy the needed net quantity of heat of rising steam at the bottom of the step-down knockout tower section tower; And if the heat that step-down knockout tower section rising steam institute calorific requirement can provide less than conventional knockout tower section overhead condensation in operating process, then need to open simultaneously auxiliary condenser 5, make conventional knockout tower section top steam reduce this burst material temperature with external heat-exchanging, to be reduced to the temperature of the required withdrawing fluid of conventional knockout tower section cat head through the cooled material 4 of main reboiler; Thereby, after practical operation reaches stable operation, auxiliary condenser 5 and auxiliary reboiler 22 generally can not opened simultaneously, can select one as supplementary energy equipment according to the heat coupling, steam can mate fully if boil at the bottom of conventional knockout tower section overhead condensation and the step-down knockout tower section tower in the flow scheme design again, and then two auxiliary equipment all need not to open.
Technology and equipment of the present invention is widely used in all distillation processes, for the advantage of the present invention aspect energy-saving and cost-reducing is described better, only chooses wherein that two application examples are illustrated, but does not therefore limit the scope of application of present technique and equipment.
Be used for third rare-propane gas piece-rate system with the inventive method, identical with the described flow process of invention, the theoretical plate of wherein conventional knockout tower section is 145, and the theoretical cam curve of step-down knockout tower section is 55.Adopt step-down knockout tower section feeding, inlet amount is 23375kg/hr, and feeding temperature is 40 ℃, and the charging mole consists of propane 0.218, propylene 0.771, ethane 0.011.
Conventional knockout tower section tower top pressure is 1800kPa, and tower bottom pressure is 2000kPa, and tower top temperature is 43.4 ℃; Step-down knockout tower section tower top pressure is 1100kPa, and tower bottom pressure is 1200kPa, and column bottom temperature is 33.7 ℃.The heat that conventional knockout tower section top condensation provides in the present embodiment is greater than the needed heat of steam that boils again that rises at the bottom of the step-down knockout tower section, open auxiliary condenser make by main reboiler the condensate flow thigh again condensation reach the top liquid-phase reflux requirement of conventional knockout tower section.Main public work and energy consumption of compressor such as table 1 in this process.
The main energy consumption of table 1
For illustrating that the present invention in the advantage aspect saving energy and reduce the cost, compares flow process of the present invention and existing single tower separation process.Tower amounts to 200 theoretical plates, and feed entrance point is at the 146th.Feed composition is identical with the present invention, if want to realize and the identical separation requirement of product of the present invention that then tower top temperature is 43.4 ℃, pressure is 1800kPa, and column bottom temperature is 58.7 ℃, and pressure is 2100kPa.Main public work energy consumption is as shown in table 2 in this Comparative Examples.
The main energy consumption of table 2
Because the main energy consumption of distillation process concentrates in heat and the power consumption, can see that from result of calculation embodiment needs only is that the power consumption of compressor is 6.280 * 10
6KJ/hr, it is 6.693 * 10 that Comparative Examples then needs heat exhaustion
7KJ/h, the embodiment total energy consumption of comparing with Comparative Examples has reduced by 90.62%, cuts down the consumption of public work in the rectifying column operating process significantly, has really realized energy saving purposes.
The lightness-removing column (or being called primary distillation tower) that is used for the pimelinketone device FF with the inventive method, (main component is cyclohexanone and cyclohexanol for the thick alcohol ketone liquid after the drying tower dehydration in charging, all the other are raw material cyclohexane residual in the reactant mixture, a small amount of light component and heavy ends that reaction produces).
This piece-rate system is identical with the described flow process of invention, and the theoretical tray number average of wherein conventional knockout tower section and step-down knockout tower section is 26.Adopt step-down knockout tower section feeding, inlet amount is 255.2kmol/hr, and feeding temperature is 108.8 ℃.
Conventional knockout tower section tower top pressure is 53kPa, and tower bottom pressure is 57kPa, and tower top temperature is 123.7 ℃; Step-down knockout tower section tower top pressure is 23kPa, and tower bottom pressure is 27kPa, and column bottom temperature is 115 ℃.The heat that conventional knockout tower section top condensation provides in the present embodiment is greater than the needed heat of steam that boils again that rises at the bottom of the step-down knockout tower section, open auxiliary condenser make by main reboiler the condensate flow thigh again condensation reach the top liquid-phase reflux requirement of conventional knockout tower section.Main public work and energy consumption of compressor such as table 3 in this process.
The main energy consumption of table 3
For illustrating that the present invention in the advantage aspect saving energy and reduce the cost, compares flow process of the present invention and existing single tower separation process.Tower amounts to 52 theoretical plates, and feed entrance point is at the 27th.Feed composition is identical with the present invention, if want to realize and the identical separation requirement of product of the present invention that then tower top temperature is 123.8 ℃, pressure is 53kPa, and column bottom temperature is 139.7 ℃, and pressure is 61kPa.Main public work energy consumption is as shown in table 4 in this Comparative Examples.
The main energy consumption of table 4
Because the main energy consumption of distillation process concentrates in heat and the power consumption, can see that from result of calculation embodiment needs only is that the power consumption of compressor is 1.860 * 10
6KJ/hr, it is 1.622 * 10 that Comparative Examples then needs heat exhaustion
7KJ/h, the embodiment total energy consumption of comparing with Comparative Examples has reduced by 88.53%, cuts down the consumption of public work in the rectifying column operating process significantly, has really realized energy saving purposes.
The present invention also can be achieved through the following technical solutions:
As shown in Figure 1, under promoting, pressure reduction enters step-down knockout tower section 12 tops through liquid phase material at the bottom of the conventional knockout tower section 1 separation back tower; After pressurizeing by compressor 14, the steam 13 that comes out in step-down knockout tower section top enters conventional knockout tower section bottom as rising steam 15; Liquid phase 16 parts of coming out at the bottom of the step-down knockout tower section tower can be used as product extraction 20, and another part 17 carries out heat exchange with the steam 2 that conventional knockout tower section cat head comes out in main reboiler 3, the required steam 18 that boils again at the bottom of the formation step-down knockout tower section tower; Conventional knockout tower section overhead vapours 2 obtains condensate liquid 4 through after the heat exchange, enters backflow storage tank 7, and condensate liquid 8 parts that flow out from the backflow storage tank are as product 9 extraction, and another part is as the overhead reflux liquid 10 of conventional knockout tower section.
In this operating process, the steam that boils again at the bottom of conventional knockout tower section overhead condensation and the step-down knockout tower section tower can be realized coupling fully in main reboiler.
Technology and equipment of the present invention is widely used in all distillation processes, for the advantage of the present invention aspect energy-saving and cost-reducing is described better, chooses an application example again and is illustrated, but therefore do not limit the scope of application of present technique and equipment.
Be used for third rare-propane gas piece-rate system with the inventive method, identical with the described flow process of invention, the theoretical plate of wherein conventional knockout tower section is 145, and the theoretical cam curve of step-down knockout tower section is 55.Adopt step-down knockout tower section feeding, inlet amount is 23375kg/hr, and feeding temperature is 10 ℃, and the charging mole consists of propane 0.218, propylene 0.771, ethane 0.011.
Conventional knockout tower section tower top pressure is 1800kPa, and tower bottom pressure is 2000kPa, and tower top temperature is 44.1 ℃; Step-down knockout tower section tower top pressure is 1100kPa, and tower bottom pressure is 1200kPa, and column bottom temperature is 29.2 ℃.This flow process steam of can realizing boiling again at the bottom of conventional knockout tower section overhead condensation and the step-down knockout tower section tower can be realized coupling fully in main reboiler, reach the requirement of separation.
Differential pressure low-energy-consumption distillation method and equipment 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 structure as herein described with technical method 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 those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (4)
1. differential pressure low-energy-consumption distillation equipment, include conventional knockout tower section, step-down knockout tower section, main reboiler, backflow storage tank and compressor, it is characterized in that: between step-down knockout tower section and conventional knockout tower section, be provided with a compressor, the vapor-phase material pipe of step-down knockout tower section cat head is connected to compressor inlet, and the compressor outlet pipe is connected to the vapour phase feed pipe at the bottom of the conventional knockout tower section tower; The vapor-phase material outlet of conventional knockout tower section cat head is connected to the import of main reboiler thermal medium, and the thermal medium outlet is connected to the backflow storage tank of conventional knockout tower section; The liquid phase outlet is connected to the liquid phase import of step-down knockout tower section cat head at the bottom of the conventional rectification tower section tower; The liquid phase material outlet of step-down knockout tower section bottom is connected to the cold medium import of main reboiler, and cold media outlet is connected to the steam inlet of boiling again of step-down knockout tower section.
2. by the method for operating of the described differential pressure low-energy-consumption distillation equipment of claim 1, it is characterized in that:
A) common rectifying column is divided into conventional knockout tower section and step-down knockout tower section, wherein conventional knockout tower section is identical with the single tower distillation operating pressure or a little more than single tower operating pressure, step-down knockout tower section adopts reduced pressure operation;
B) step-down knockout tower section adopts reduced pressure operation, and step-down knockout tower section overhead vapours reaches through compressor compresses and enters conventional knockout tower section after requiring at the bottom of the conventional knockout tower section tower;
C) reduced pressure operation of step-down knockout tower section makes its tower still material temperature of boiling again be lower than conventional segregation section cat head material temperature, thereby utilizes the coupling heat exchange of these two strands of materials to realize two thermal couplings between the tower section.
3. the method for operating of differential pressure low-energy-consumption distillation equipment as claimed in claim 2 is characterized in that being provided with an auxiliary reboiler at the bottom of the described step-down knockout tower section tower; Be provided with auxiliary condenser between main reboiler and the backflow storage tank; Concrete operation method is as follows: liquid phase material (11) enters step-down knockout tower section (12) top at the bottom of the tower after separating through conventional knockout tower section (1) under pressure reduction promotes; After pressurizeing by compressor (14), the steam (13) that comes out in step-down knockout tower section top enters conventional knockout tower section bottom as rising steam (15); Liquid phase (a 16) part of coming out at the bottom of the step-down knockout tower section tower can be used as product extraction (20), another part (17) carries out heat exchange with the steam (2) that conventional knockout tower section cat head comes out in main reboiler (3), the required steam that boils again (18) at the bottom of the formation step-down knockout tower section tower, if condensation load during less than main reboiler, needs to open simultaneously auxiliary reboiler (22); The part or all of condensate liquid (4) of conventional knockout tower section overhead vapours (2) through obtaining after the heat exchange, when condensation load during greater than main reboiler, need to open the auxiliary condenser (5) that this partial condensation liquid (4) is flowed through, thereby the condensate liquid (6) that obtains needed backflow of conventional knockout tower section cat head and extraction enters backflow storage tank (7), the condensate liquid that flows out from the backflow storage tank (a 8) part is as product (9) extraction, and another part is as the overhead reflux liquid (10) of conventional knockout tower section.
4. the method for operating of differential pressure low-energy-consumption distillation equipment as claimed in claim 3, it is characterized in that the operation of described auxiliary condenser (5) and auxiliary reboiler (22), after stable, can select one as supplementary energy equipment according to the heat coupling, steam can mate fully if boil at the bottom of conventional knockout tower section overhead condensation and the step-down knockout tower section tower in the flow scheme design again, and then two auxiliary equipment all need not to open.
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| CN108704330B (en) * | 2018-06-15 | 2019-11-26 | 武汉理工大学 | A kind of low energy consumption variable-pressure rectification system |
| CN108905256A (en) * | 2018-08-01 | 2018-11-30 | 清水湾Chdm科技有限公司 | A kind of multitower rectifying and dewatering power-economizing method and device |
| CN109745724B (en) * | 2019-01-24 | 2021-04-23 | 山东伯仲真空科技股份有限公司 | MVR (mechanical vapor recompression) rectification and stripping composite device and process method thereof |
| CN111686469A (en) * | 2020-06-12 | 2020-09-22 | 天津大学 | Middle steam compression two-section partition tower |
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