CN100486662C - Energy saving method and equipment for rectification separation - Google Patents
Energy saving method and equipment for rectification separation Download PDFInfo
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- CN100486662C CN100486662C CNB2006100900034A CN200610090003A CN100486662C CN 100486662 C CN100486662 C CN 100486662C CN B2006100900034 A CNB2006100900034 A CN B2006100900034A CN 200610090003 A CN200610090003 A CN 200610090003A CN 100486662 C CN100486662 C CN 100486662C
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Abstract
The invention relates to an equipment and method for saving energy conservation in selective evaporation. The equipment involves A and B rectification tower in series. The bottom of Tower A connects the reboiler. The export of Tower A connects the import of Tower B. The export of Tower A on the top connects middle reboiler, reflux accumulator, reflux pump. The bottom of Tower B connects middle reboiler. The top of Tower B connects condenser, reflux accumulator, reflux pump. The heat of condensation of Tower A is as the load of middle reboiler when connected Tower B. Part of the heat of condensation reflows to the tower and other is as the product. In Tower B, the light product boils over from the top. Some reflows to tower and other is as the product. The heat is from condenser and middle reboiler and attaches the light-load adjustment reboiler to achieve connecting in series, the mightiness coupling between condenser and middle reboiler. The design is reasonable; the effect on saving energy is obvious.
Description
Technical field:
The present invention relates to a kind of energy-saving rectifying separation method and equipment that rectifying separates that is used for.
Background technology:
At present typical single tower distillation schematic flow diagram is seen accompanying drawing 1.Raw material separates through rectifying column, obtains overhead product from cat head, obtains tower still product from the tower still.
Two tower rectifying schematic flow diagrams of typical series connection are seen accompanying drawing 2 at present.Raw material enters rectifying column I, obtains overhead product I by this cat head, and its tower bottoms enters rectifying column II, and another kind of overhead product II is obtained by rectifying column II cat head, and this tower still obtains tower still product.
Two tower distillation technologies of present typical single tower distillation, series connection all use condenser, the reboiler of standard, do not carry out " Thermal-mechanical Coupling ", need to consume corresponding condenser heat load, reboiler thermic load, therefore also have improved needs and possibility.
Use " intermediate reboiler " technology is arranged in the single tower distillation at present, but its thermal source is all from other parts, rather than comes this rectifying column system itself, and the operation that goes into operation is also inconvenient, so need improvement.
At present in single tower distillation, use " the two parallel condensing device/reboiler Thermal-mechanical Coupling technology of pressing of double tower " is arranged, but the practice can be brought inconvenient operation like this, because the almost completely the same tower that has been in parallel makes complicated operationization; Because " Thermal-mechanical Coupling " gives wherein " condenser/reboiler Thermal-mechanical Coupling " tower of lower pressure, can bring operation not too convenient again.
At present in the double tower methanol rectification, use " the two series connection condenser/reboiler Thermal-mechanical Coupling of pressing of double tower " technology is arranged, but not " condenser/intermediate reboiler Thermal-mechanical Coupling " technology, nor use " additive regulating reboiler ", giving wherein, " condenser/reboiler Thermal-mechanical Coupling " tower of lower pressure brings inconvenient operation.
At present in two tower rectifying of typical series connection, use " the two series connection condenser/reboiler Thermal-mechanical Coupling of pressing of double tower " technology is arranged, but " two series connection, the condensers/intermediate reboiler Thermal-mechanical Coupling of pressing of double tower " technology and " additive regulating reboiler " technology of not using.
Summary of the invention:
The objective of the invention is to design a kind of two rectifying separating technologies of pressing series connection, condenser, intermediate reboiler Thermal-mechanical Coupling and additive regulating reboiler equipment of double tower that include, both brought into play the advantage that " Thermal-mechanical Coupling " is energy-conservation, save operating cost, overcome effectively again, cause " Thermal-mechanical Coupling " can be brought the shortcoming of flexibility variation to operation, makes " Thermal-mechanical Coupling " operation more be tending towards perfect.
The objective of the invention is to realize by following process program:
It is to be made of A and two rectifying columns of B, the bottom of A tower is connected with a reboiler, the extraction mouth is adopted to enter the mouth with the B tower and is connected at the bottom of the tower, the top extraction mouth of A tower is connected with intermediate reboiler, intermediate reboiler is connected with return tank, return tank is connected with the top inlet of A tower by reflux pump, intermediate reboiler is connected with B tower bottom, adjusting reboiler one end is connected with the B tower bottom, one end flows out pipeline with the still liquid of B tower bottom and is connected, B top of tower extraction mouth is connected with return tank by condenser, is being connected with the B top of tower by reflux pump.
All raw material enters the A tower by inlet, this tower is provided with conventional reboiler, enter the B tower of series connection by tower still extraction mouth, the part light product is under the lower rate of recovery requires, steam from cat head, and the cat head that makes the A tower is removed the thermal loads of hot condensation heat load as the intermediate reboiler of the B tower of series connection, thereby reaching two pressure of double tower connects, condenser, intermediate reboiler Thermal-mechanical Coupling purpose, promptly realized removing the Thermal-mechanical Coupling of reheater condenser thermic load and heat supply intermediate reboiler thermic load, this way has not only been saved the hot thermic load of removing of condenser but also saved two parts of thermic loads of intermediate reboiler heating, therefore can reach and reduce comprehensive energy consumption and product cost purpose.Because the A tower is crude separation, so the reboiler thermic load can reach and reduce reboiler thermic load purpose far below the thermic load of original single tower, the liquid of this column overhead condensation, and partial reflux is gone into tower, and remainder is used as the product extraction.At the B tower, the part light-end products steams from cat head in addition, through condenser condenses, partial reflux is gone into tower, and remainder also is used as the product extraction, this tower is mainly by condenser and intermediate reboiler heat supply, this tower also is provided with conventional condenser, but is lower than original single tower because this tower is handled load, so the condensation heat load also significantly reduces, for easy to operate, this tower also is provided with the very little additive regulating reboiler of thermic load.
For the single tower distillation tower, the present invention is owing to adopted the rough segmentation measure to the A tower, the yield that promptly requires light component is only for about below 50%, so this tower number of plates, capacity of returns and inlet amount ratio, also can reduce half (concrete data depend on the influence to relative volatility of pressure, component) in principle than B tower, therefore the operation of A tower is easier than B tower, and the operation of B tower does not almost change, and has just increased condenser and intermediate reboiler.
Two tower rectifying situations to series connection, need not increase new tower, and just change the operating parameter of original two towers, to charging when the A tower or to charging during at the B tower, either way be to utilize the thermal loads of the overhead condensation thermic load of A tower as the intermediate reboiler of the B tower of another one series connection, thereby reaching two pressure of double tower connects, condenser and intermediate reboiler Thermal-mechanical Coupling purpose, promptly realized the Thermal-mechanical Coupling of condenser heat load and intermediate reboiler thermic load, again at the B tower, additive regulating reboiler and overhead condenser are set, satisfy the separation requirement of B tower, the separation requirement of each tower of two towers of connecting does not change fully with original requirement.
In addition, to single tower distillation, the present invention is not only applicable to newly design occasion, and is specially adapted to existing apparatus is extended occasion on a large scale, and can utilize on the basis of original single tower this moment, only need the A tower of the crude separation of new series connection another one, good operation, just can accomplish, enlarge the output purpose, both save equipment investment thereby reach, the effect of operating cost can be saved again, therefore product cost can be reduced effectively.
Two tower rectifying for series connection: the present invention both had been applicable to new design occasion, was applicable to more that also existing two tower rectifying transform occasion, only need to adjust this moment higher pressure column device security, suitably change equipment, just can easily form new technological process.
Therefore the present invention is specially adapted to the two devices of series connection condenser and reboiler Thermal-mechanical Coupling technology of pressing of original double tower are improved for example methanol rectifying system of occasion owing to adopt additive regulating reboiler technology, and the device operation after the improvement can be convenient.
For single tower distillation, be applicable to the dense occasion of light component in the charging (generally suitable more than 70%).The present invention has only used the less reboiler thermic load of A tower and less condenser heat load and " additive regulating reboiler " thermic load of B tower, has therefore saved comprehensive energy consumption, has reduced running cost.The use of " additive regulating reboiler " makes the operation of " Thermal-mechanical Coupling " more flexible, makes things convenient for.Crude separation measure, the number of plates because of the A tower is few in addition, processing ease.Though cost of equipment needs to increase, fixed cost also needs to increase, and total production cost reduces.
For two tower rectifying of series connection, only used reboiler thermic load and less condenser heat load and " additive regulating reboiler " thermic load of B tower of A tower, therefore saved comprehensive energy consumption, reduce running cost.Cost of equipment changes not quite in principle, so total production cost also reduces.
The present invention is suitable for various single towers and separates occasion, and just the light component concentration in the charging should just have better economic benefit greater than 70%.
The present invention is suitable for two tower rectifying of series connection, to former two tower thermic loads more near the time suitable more, energy-saving effect is obvious more.
Description of drawings
Fig. 1 single tower distillation tower schematic flow diagram.
Two tower rectifying column schematic flow diagrams of Fig. 2 series connection.
Fig. 3 single tower distillation tower changes " two series connection, the intermediate reboiler Thermal-mechanical Coupling of pressing of double tower " into and reaches " additive regulating reboiler " schematic flow sheet.
Fig. 4 two-tower rectification tower changes " two series connection, the intermediate reboiler Thermal-mechanical Coupling of pressing of double tower " into and reaches " additive regulating reboiler " schematic flow sheet.
Fig. 5 two-tower rectification tower changes " two series connection, the intermediate reboiler Thermal-mechanical Coupling of pressing of double tower " into and reaches " additive regulating reboiler " schematic flow sheet.
Wherein: 1A tower 2B tower 3 reboilers 4 intermediate reboilers 5 additive regulating reboilers
6 reflux pumps, 7 condensers, 8 return tanks, 9 reflux pumps, 10 return tanks
Specific embodiments
Present embodiment is to change the single tower distillation tower into double tower two series connection, condenser and intermediate reboiler Thermal-mechanical Coupling and additive regulating reboilers of pressing, and schematic flow sheet is seen accompanying drawing 3.
Constitute by A and two rectifying columns of B, the bottom of A tower (1) is connected with a reboiler (3), the extraction mouth is adopted to enter the mouth with B tower (2) and is connected at the bottom of the tower, the top extraction mouth of A tower is connected with intermediate reboiler (4), intermediate reboiler is connected with a return tank (8), return tank is connected with the top inlet of A tower by reflux pump (6), intermediate reboiler is connected with B tower bottom, adjusting reboiler (5) one ends are connected with the B tower bottom, the other end flows out pipeline with the still liquid of B tower bottom and is connected, B top of tower extraction mouth is connected with return tank (10) by condenser (7), is connected with the B top of tower by reflux pump (9) again.
Fresh feed at first enters the correct position of A tower, this tower only is provided with reboiler, adopt low product recovery rate, thereby overcome the unfavorable factor that improves the relative volatility minimizing that brings because of pressure, cat head steams the part light product, removes heat through the condenser and the intermediate reboiler of B tower, condensation enters the return tank buffering, partial reflux returns cat head, remainder is done the product extraction, and this tower bottoms extraction enters the B tower, the B tower keeps the separation requirement identical with former knockout tower, steam the part light-end products from cat head, remove heat through common condenser, condensation enters the return tank buffering, partial reflux returns cat head, remainder is also done the product extraction, in order to increase operation, the flexibility of regulating is set up the additive regulating reboiler at B Tata still, be used to guarantee product quality, adapt to the fluctuation of changing factor.
Present embodiment is to change the two-tower rectification tower into double tower two the pressure to connect, condenser and intermediate reboiler Thermal-mechanical Coupling and additive regulating reboiler, to charging when the A tower, schematic flow sheet is seen accompanying drawing 4, technological process such as embodiment 1, fresh feed at first enters the A tower, and cat head steams product I, removes heat through the condenser and the intermediate reboiler of B tower, condensation, enter the return tank buffering, partial reflux returns cat head, and remainder is done the product I extraction, and this tower is provided with typical reboiler, the extraction of still liquid, enter the B tower, the B tower steams light product II from cat head, and classic condenser removes heat, condensation, enter the return tank buffering, partial reflux returns cat head, and remainder is also done product I I extraction, sets up the additive regulating reboiler at B Tata still, be used to guarantee the normal running of B tower, from tower still extraction still liquid product.
Present embodiment is to change the two-tower rectification tower into double tower two the pressure to connect, condenser and intermediate reboiler Thermal-mechanical Coupling and additive regulating reboiler technology, process equipment is identical with embodiment 1, charging is when the B tower, referring to accompanying drawing 5, fresh feed at first enters the B tower, and cat head steams product I, removes heat through B tower typical case condenser, condensation, enter the return tank buffering, partial reflux returns cat head, and remainder is done the product I extraction, sets up the additive regulating reboiler at the tower still, be used to guarantee the normal running of B tower, this tower bottoms extraction enters the A tower, and the A tower steams light product II from cat head, condenser and intermediate reboiler through the B tower are removed heat, condensation, enter the return tank buffering, partial reflux returns cat head, and remainder is also done product I I extraction, this tower is provided with typical reboiler, from tower still extraction still liquid product.
Embodiment 4
Carry out ethylene distillation with embodiment 1 process equipment
Ethylene rectifying column calculated data table
For certain ethylene separation tower, the cold of the cat head of B tower-40 ℃ can save 42% approximately, the reboiler thermic load of A tower (deduction B tower additive regulating reboiler thermic load) can save 57% approximately, for no other reason than that this tower still temperature is about 0 ℃, so reboiler thermic load essence is 18 ℃ of refrigerating capacitys, therefore to save reboiler thermic load essence be negative effect, offset the positive-effect of the cold of saving cat head-40 ℃.The two pressure of double tower connected in addition, and the tower expense can increase (wherein increase the A tower newly, but reduce B tower treating capacity), the instrument expense can increase, so fixed cost can increase slightly, but the positive-effect of the cold of the cat head of saving-40 ℃ is far longer than the fixed cost of increase, and pure cost can be saved.
Carry out propylene rectifying with the process equipment identical with embodiment 1
Propylene rectification tower calculated data table
For certain propylene knockout tower, the refrigeration duty of the cat head recirculated water of B tower can save 42% approximately; The reboiler thermic load of A tower (deduction B tower additive regulating reboiler thermic load) can save 38% approximately.The two pressure of double tower connected in addition, the tower expense can increase and (wherein increases the A tower newly, but reduce B tower treating capacity), the instrument expense can increase, so fixed cost can increase slightly, but the refrigeration duty of the recirculated water of the cat head of saving and the positive-effect of the reboiler thermic load of relative high pressure column are far longer than the fixed cost of increase, and pure cost can be saved.
With the process equipment identical with embodiment 1 carry out benzene, toluene separates
Benzene, toluene separating rectification tower calculated data table
For certain benzene, toluene pre-separation tower, the refrigeration duty of overhead condenser recirculated water can save 34% approximately; Tower still reboiler thermic load (deduction B tower additive regulating reboiler thermic load) can save 31% approximately.The two pressure of double tower connected in addition, the tower expense can increase and (wherein increases the A tower newly, but reduce B tower treating capacity), the instrument expense can increase, so fixed cost can increase slightly, but the positive-effect of the reboiler thermic load of the refrigeration duty of the recirculated water of the cat head of saving and relative high pressure column is much larger than the fixed cost of increase, and pure cost can be saved.
Carry out benzene, toluene pre-separation with the process equipment identical with embodiment 1
Benzene, toluene pre-separation rectifying column calculated data table
For certain benzene, toluene knockout tower, the refrigeration duty of overhead condenser recirculated water can save 40% approximately; Tower still reboiler thermic load (deduction B tower additive regulating reboiler thermic load) can save 31% approximately.The two pressure of double tower connected in addition, the tower expense can increase and (wherein increases the A tower newly, but reduce B tower treating capacity), the instrument expense can increase, so fixed cost can increase slightly, but the positive-effect of the reboiler thermic load of the refrigeration duty of the recirculated water of the cat head of saving and relative high pressure column is much larger than the fixed cost of increase, and pure cost can be saved.
Carrying out ortho-xylene with the process equipment identical with embodiment 1 separates
Ortho-xylene separating rectification tower calculated data table
For certain ortho-xylene knockout tower, the refrigeration duty of overhead condenser recirculated water can save 44% approximately; Tower still reboiler thermic load (deduction B tower additive regulating reboiler thermic load) can save 42% approximately.The two pressure of double tower connected in addition, the tower expense can increase and (wherein increases the A tower newly, but reduce B tower treating capacity), the instrument expense can increase, so fixed cost can increase slightly, but the positive-effect of the reboiler thermic load of the refrigeration duty of the recirculated water of the cat head of saving and relative high pressure column is much larger than the fixed cost of increase, and pure cost can be saved.
Carry out the two tower rectifying of 1-butylene with the process equipment identical with embodiment 1
1-butylene rectifying column calculated data table
*Thermal-mechanical Coupling
To certain 1-butylene knockout tower, the refrigeration duty of overhead condenser recirculated water can save 35% approximately; Tower still reboiler thermic load can save 33% approximately, and the fixed cost change is little, and 1-butylene pure cost can be saved.
Carry out pseudocumene two tower rectifying with the process equipment identical with embodiment 1
Certain pseudocumene rectifying column calculated data table
*Thermal-mechanical Coupling
For certain pseudocumene knockout tower, the refrigeration duty of overhead condenser recirculated water can save 27% approximately; Tower still reboiler thermic load can save 24% approximately, and by constant, can save temporarily by the pseudocumene pure cost for fixed cost.
For single tower, can save the reboiler thermic load of making an appointment with half, the condenser heat load of half than original flow process in theory, in fact, can lack because reasons such as " additive regulating reboilers " is set.
For single tower, (for example 〉=70%) occasion all is suitable for charging light component concentration height, and light component concentration is high more, and energy-saving effect is good more in principle.As ethylene separation tower; The propylene knockout tower; Benzene, toluene knockout tower; Benzene, toluene pre-separation tower; Ortho-xylene column; Methanol rectifying tower; Most heavy ends are few takes off heavies column; The many cut light tower of most light components.
To the series connection two tower rectifying, to former two tower thermic loads more near the time suitable more, energy-saving effect is obvious more.As 1-butylene knockout tower; The pseudocumene knockout tower; In most two tower rectifying, two tower rectifying of the series connection that thermic load is approaching or more approaching.
Claims (2)
1. energy-saving rectifying separation equipment, it is characterized in that: it is to be made of A and two rectifying columns of B, the bottom of A tower is connected with a reboiler, the extraction mouth is adopted to enter the mouth with the B tower and is connected at the bottom of the tower, the top extraction mouth of A tower is connected with intermediate reboiler, intermediate reboiler is connected with return tank A, return tank A is connected with the top inlet of A tower by reflux pump A, intermediate reboiler is connected with B tower bottom, adjusting reboiler one end is connected with the B tower bottom, one end flows out pipeline with the still liquid of B tower bottom and is connected, B top of tower extraction mouth is connected with return tank B by condenser, is connected with the B top of tower by reflux pump B again.
2. energy-saving rectifying separation method, it is characterized in that: separate with the described equipment rectifying of claim 1, all raw material enters the A tower from inlet, and the A tower only is provided with reboiler, enters the B tower of series connection by tower extraction mouth, yield is 50% part light product, steam from the A cat head, as the thermal loads of intermediate reboiler of the B tower of series connection, the liquid of condensation, a part passes back into tower, and a part is as the product extraction; At the B tower, the part light product steams from cat head in addition, and through condenser condenses, partial reflux is gone into tower, and remainder is as the product extraction, and this tower is by condenser and intermediate reboiler heat supply, and the very little adjusting reboiler of parasitic thermal load.
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| CNB2006100900034A CN100486662C (en) | 2006-06-23 | 2006-06-23 | Energy saving method and equipment for rectification separation |
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| CNB2006100900034A CN100486662C (en) | 2006-06-23 | 2006-06-23 | Energy saving method and equipment for rectification separation |
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| CN101091836A CN101091836A (en) | 2007-12-26 |
| CN100486662C true CN100486662C (en) | 2009-05-13 |
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| CN102260593B (en) * | 2011-07-11 | 2012-12-05 | 云南绿宝香精香料股份有限公司 | Device for extracting iris root oil by virtue of dynamic circulation type steam vacuum distillation |
| CN102641604B (en) * | 2012-04-01 | 2016-12-14 | 中国石油化工股份有限公司 | A kind of process of multicomponent side line thermal coupling rectification |
| CN102921183A (en) * | 2012-11-07 | 2013-02-13 | 浙江大学 | Rectification device and process for purifying ethyl difluoroacetate efficiently |
| CN107434783A (en) * | 2016-05-25 | 2017-12-05 | 天津大学 | A kind of power-economizing method and device of caprolactam system |
| CN106966875B (en) * | 2017-03-31 | 2020-09-08 | 四川达兴能源股份有限公司 | Anti-blocking device of polymethoxy dibutyl ether rectification system and refining method |
| CN107603659A (en) * | 2017-08-16 | 2018-01-19 | 中石化广州工程有限公司 | One kind alkylation fractional method |
| CN107523323A (en) * | 2017-08-16 | 2017-12-29 | 中石化广州工程有限公司 | One kind alkylation fractionation process |
| CN108273279B (en) * | 2017-11-28 | 2021-04-02 | 聊城市鲁西化工工程设计有限责任公司 | High-efficiency low-consumption hydrogen chloride separation method |
| CN108704330B (en) * | 2018-06-15 | 2019-11-26 | 武汉理工大学 | A kind of low energy consumption variable-pressure rectification system |
| CN110980648A (en) * | 2019-12-31 | 2020-04-10 | 中船重工（邯郸）派瑞特种气体有限公司 | Hydrogen bromide purification device and method |
| CN114534771B (en) * | 2022-03-03 | 2022-09-16 | 大庆亿鑫化工股份有限公司 | Isomerization catalyst for mixed xylene and separation method of o-xylene |
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