CN117883803A - Solvent rectification heat energy utilization device and method integrating heat pump rectification and triple-effect rectification - Google Patents
Solvent rectification heat energy utilization device and method integrating heat pump rectification and triple-effect rectification Download PDFInfo
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- CN117883803A CN117883803A CN202410302342.2A CN202410302342A CN117883803A CN 117883803 A CN117883803 A CN 117883803A CN 202410302342 A CN202410302342 A CN 202410302342A CN 117883803 A CN117883803 A CN 117883803A
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- 239000002904 solvent Substances 0.000 title claims abstract description 247
- 238000000034 method Methods 0.000 title claims abstract description 39
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 117
- 230000018044 dehydration Effects 0.000 claims abstract description 113
- 239000007788 liquid Substances 0.000 claims abstract description 67
- 238000010438 heat treatment Methods 0.000 claims abstract description 29
- 239000000463 material Substances 0.000 claims abstract description 16
- 230000000630 rising effect Effects 0.000 claims abstract description 6
- 238000010992 reflux Methods 0.000 claims description 86
- 238000011084 recovery Methods 0.000 claims description 40
- 239000012071 phase Substances 0.000 claims description 28
- 238000007599 discharging Methods 0.000 claims description 16
- 230000008569 process Effects 0.000 claims description 14
- 238000003860 storage Methods 0.000 claims description 13
- 239000012808 vapor phase Substances 0.000 claims description 13
- 238000004821 distillation Methods 0.000 claims description 8
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 230000000694 effects Effects 0.000 abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- 238000000605 extraction Methods 0.000 description 10
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 7
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 230000005611 electricity Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 229920003048 styrene butadiene rubber Polymers 0.000 description 2
- 229920003051 synthetic elastomer Polymers 0.000 description 2
- 239000005061 synthetic rubber Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000010528 free radical solution polymerization reaction Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a solvent rectification heat energy utilization device and a method integrating heat pump rectification and triple effect rectification, wherein the device comprises a solvent dehydration tower, a first weight removal tower, a second weight removal tower, a third weight removal tower, a heat pump set, a heat exchanger group and a material pipeline; the bottom discharge line of the solvent dehydration tower is communicated with the tower body feed inlet of the first heavy removal tower, the bottom discharge line of the first heavy removal tower is communicated with the tower body feed inlet of the second heavy removal tower, and the bottom discharge line of the second heavy removal tower is communicated with the tower body feed inlet of the third heavy removal tower; the solvent dehydration tower and the heavy removal tower comprise low-pressure high-temperature steam heating wires; the tower top steam of the solvent dehydration tower is subjected to pressure boosting and temperature rising through a first heat pump and then exchanges heat with the tower bottom liquid of the solvent dehydration tower; the tower top steam of the heavy-removal third tower exchanges heat with the tower bottom liquid of the heavy-removal second tower to supply heat to the heavy-removal second tower; the tower top steam of the heavy-removal second tower exchanges heat with the tower bottom liquid of the heavy-removal first tower to supply heat to the heavy-removal first tower; and after the pressure and the temperature of the tower top steam of the heavy-removal first tower are increased through the second heat pump, the tower top steam exchanges heat with the tower bottom liquid of the heavy-removal third tower.
Description
Technical Field
The invention relates to the technical field of solvent rectification, in particular to a solvent rectification heat energy utilization device and a method integrating heat pump rectification and triple-effect rectification.
Background
The rectification is a distillation method for separating the liquid mixture with high purity by using reflux, is the liquid mixture separation operation with the widest industrial application, and is widely applied to the departments of petroleum, chemical industry, light industry, food, metallurgy and the like.
In a solvent rectifying system of the synthetic rubber device, the steam consumption of each ton of solvent can reach more than 0.2-0.24t at maximum, the energy utilization rate is often less than 10%, and the method belongs to a high-energy-consumption process. According to the national work requirements of enhancing energy conservation and emission reduction, the implementation of the measures of energy conservation and comprehensive waste utilization of the system is quickened, the energy utilization efficiency is improved, the energy consumption is reduced, and the pollution to the environment caused by the production of synthetic rubber is relieved. The existing technology is mature and relatively old, part of high-temperature rectifying tower top gas phase in the system needs to be cooled, and tower bottom liquid phase needs to be reboiled, so that the energy loss of the whole rectifying system is large, and the steam consumption is large. In the existing solvent rectification process, a large amount of steam is required to provide heat for a solvent dehydration tower and a heavy-duty removal tower reboiler, in addition, the vapor phase temperature of the top of the solvent system dehydration tower and the top of the heavy-duty removal tower is high, circulating water is required to be used as a refrigerant for cooling, and the circulating water after heat exchange is also required to be sent to a cooling tower for cooling. Therefore, the heat waste of the two parts is caused, the steam consumption and the load of the cooling tower are increased, and the production and operation cost is increased.
In order to improve the energy utilization efficiency in a rectification system, the invention CN114949896B discloses a heat energy utilization device and a heat energy utilization method for a solution polymerized styrene-butadiene rubber rectification system, wherein the device comprises the following components: a butadiene rectifying tower, a normal hexane solvent dehydrating tower, a water condensation tank, a solvent reflux tank and a heat exchanger for solution polymerization of styrene butadiene rubber; the tower top extraction line and the tower body lateral extraction line of the solvent dehydration tower respectively transfer heat to low-temperature condensate output by the condensate tank through the heat exchanger to obtain a high Wen Ningshui; the high-pressure high-temperature steam is transferred to a solvent dehydration tower and then is converted into steam condensate; the high Wen Ningshui and steam condensate transfer heat to the butadiene rectifying tower reboiler, so that the rectifying tower reboiler supplies high-temperature steam to the butadiene rectifying tower, and steam condensate in the tower flows back to the rectifying tower reboiler; and cooling and refluxing the high-temperature condensate and the steam condensate into a condensate tank. The device combines the tower top extraction line and the tower body lateral extraction line of the solvent dehydration tower, the high Wen Ningshui and the steam condensate, the heat source energy is extremely poor, and the heat consumption is remarkably reduced.
The invention CN113680088A discloses a multi-effect rectifying method, a rectifying device and application thereof. The multi-effect rectification method comprises the following steps: the gas phase materials at the top of the first-stage to N-1-stage rectifying towers are firstly separated and condensed to obtain condensate and residual gas phase; the separated condensate flows back to the stage rectification tower, the residual gas phase exchanges heat with the tower bottom liquid of the next stage rectification tower to be condensed, the residual gas phase condensate after heat exchange is extracted and/or flows back to the stage rectification tower, and the heated tower bottom liquid returns to the next stage rectification tower; wherein N is more than or equal to 2 and is an integer. The invention uses a dephlegmator to exchange heat between the gas phase material flow at the top of the rectifying tower and the bottom liquid of the next-stage rectifying tower, the gas phase material flow at the top of the rectifying tower is dephlegmated, and the bottom liquid of the next-stage rectifying tower is heated. The heavy components at the tower top can be condensed by utilizing the method of tower top segregation, and the content of the heavy components in the extracted condensate can be ensured to be qualified when the heavy components flow back into the tower, so that the reflux quantity of the tower is reduced, and the energy is saved. The multi-effect rectification is an effective means for improving the rectification quality and reducing the energy consumption at present, but only depends on the design and the process control of a multi-effect rectification device, so that the energy consumption is difficult to be further reduced, and a certain technical bottleneck is formed.
Therefore, how to provide a solvent rectification heat energy utilization device, to effectively utilize the heat of the high-temperature discharge of the multi-effect rectification tower, realize the heat transfer between the multi-towers, further improve the heat utilization efficiency, and reduce the production cost is a problem to be solved by the technicians in the field.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a solvent rectification heat energy utilization device and a solvent rectification heat energy utilization method integrating heat pump rectification and triple-effect rectification, integrates the advantages of the heat pump rectification and the triple-effect rectification technology, and utilizes double heat pumps to promote the further improvement of the system heat utilization efficiency on the basis of integral layout and effective utilization of the heat of high-temperature steam of a rectification tower, thereby effectively reducing the production cost.
In a first aspect, the present invention provides a solvent distillation heat energy utilization device integrating heat pump distillation and triple effect distillation, which is characterized in that: comprises a solvent dehydration tower, a first heavy removal tower, a second heavy removal tower, a third heavy removal tower, a heat pump set, a heat exchanger set and a material pipeline;
The bottom discharge line of the solvent dehydration tower is communicated with the tower body feed inlet of the first heavy removal tower, the bottom discharge line of the first heavy removal tower is communicated with the tower body feed inlet of the second heavy removal tower, and the bottom discharge line of the second heavy removal tower is communicated with the tower body feed inlet of the third heavy removal tower;
The solvent dehydration tower and the heavy removal tower comprise low-pressure high-temperature steam heating wires;
The tower top steam of the solvent dehydration tower is subjected to pressure boosting and temperature rising through a first heat pump and then exchanges heat with the tower bottom liquid of the solvent dehydration tower;
the tower top steam of the heavy-removal third tower exchanges heat with the tower bottom liquid of the heavy-removal second tower to supply heat to the heavy-removal second tower;
the tower top steam of the heavy-removal second tower exchanges heat with the tower bottom liquid of the heavy-removal first tower to supply heat to the heavy-removal first tower;
and after the pressure and the temperature of the tower top steam of the heavy-removal first tower are increased through the second heat pump, the tower top steam exchanges heat with the tower bottom liquid of the heavy-removal third tower.
The invention adopts a three-effect rectification technology, forms a high-quality and high-efficiency rectification system through the connection design of material pipelines, effectively utilizes high-temperature still top steam, realizes heat exchange/heat supply between towers, and is beneficial to reducing the steam consumption. Secondly, by utilizing the boosting and heating effects of the heat pump, the saturated pressure and saturated temperature of the top steam of the tower are improved, the grade of the top steam of the still is further improved, double purposes of reboiling of the tower bottom and condensation of the top of the tower are realized, and especially, the double heat pumps are respectively arranged, so that the heat energy flow in a single tower (in the solvent dehydration tower for internal circulation) and between the towers (between the heavy removal tower and the heavy removal tower) can be controllably completed, the steam and cooling water consumption can be effectively reduced, and the energy consumption of a system is reduced.
Preferably, the tower top steam of the solvent dehydration tower passes through the first heat pump and the first heat exchanger, exchanges heat with the tower bottom liquid of the solvent dehydration tower, and then enters the dehydration tower reflux tank, an oil phase discharge port of the dehydration tower reflux tank is communicated with a dehydration tower reflux line, and the dehydration tower reflux line is sequentially communicated with the solvent preheater and the tower top feed port of the solvent dehydration tower; optionally, upstream of the solvent preheater, a crude solvent supply line communicates with the dehydration column return line.
The solvent dehydration tower adopts an open type heat pump rectification mode of tower top gas, and meanwhile, the heat energy utilization mode of heat exchange is carried out between tower top feeding and the heavy-weight removal tower. The tower top discharging line for solvent dehydration is connected with a first heat pump, the tower top steam is directly compressed, the saturation pressure and the saturation temperature of the tower top steam are improved, the dual purposes of reboiling tower bottom liquid and condensing the tower top steam are realized by utilizing a first heat exchanger, and the steam and cooling water consumption is greatly saved.
Preferably, the tower top steam of the heavy-removal first tower passes through a second heat pump and a fourth heat exchanger, exchanges heat with tower bottom liquid of the heavy-removal third tower, and enters a heavy-removal first tower reflux tank;
the oil phase discharge port of the heavy-removal first-tower reflux tank is communicated with the tower top feed port of the heavy-removal first-tower through a heavy-removal first-tower reflux line;
And a refined solvent discharge port of the heavy-removal one-tower reflux tank is communicated with a refined solvent storage tank.
The heavy-removal tower adopts an open-type heat pump rectification mode of tower top gas, and meanwhile, the heat energy utilization mode of heat exchange is carried out between tower top feeding materials and the heavy-removal tower. The tower top discharging line of the heavy-removal first tower is connected with a second heat pump, the tower top steam is directly compressed, the saturation pressure and the saturation temperature of the tower top steam are improved, the double purposes of reboiling tower bottom liquid of the heavy-removal third tower and condensing the tower top steam of the heavy-removal first tower are realized by utilizing a fourth heat exchanger, and the steam and cooling water consumption are also greatly saved.
Preferably, the tower top steam of the heavy-removal second tower passes through a second heat exchanger, exchanges heat with tower bottom liquid of the heavy-removal first tower, and enters a heavy-removal first tower reflux tank through a heavy-removal second tower solvent vapor phase condensate tank and a solvent preheater;
the tower top steam of the heavy-removal third tower passes through a third heat exchanger, exchanges heat with tower bottom liquid of the heavy-removal second tower, and enters the heavy-removal first tower reflux tank through the heavy-removal third tower solvent vapor phase condensate tank and the solvent preheater.
Through the heat exchange mode, the first heavy-removal tower and the second heavy-removal tower do not need external low-pressure high-temperature steam for heat supply, the rectification requirement can be met by means of the high-temperature tower top steam of the second heavy-removal tower and the high-temperature tower top steam of the third heavy-removal tower respectively, and the crude solvent and the reflux solvent which enter the dehydration tower can be preheated through the solvent preheater by the discharging materials of the solvent gas-phase condensate tank of the second heavy-removal tower and the solvent gas-phase condensate tank of the third heavy-removal tower, so that the energy consumption and the cost of the system are further reduced.
Preferably, at least one additional heat exchanger is arranged on the top discharge line of the heavy-removal three-tower between the heavy-removal three-tower solvent vapor phase condensate tank and the heavy-removal one-tower reflux tank and downstream of the solvent preheater.
Preferably, the solvent rectification heat energy utilization device further comprises a residual liquid recovery tower, wherein a tower top feed inlet of the residual liquid recovery tower is communicated with a tower bottom feed inlet of the heavy removal tower, a tower top feed inlet of the heavy removal tower is communicated with a tower body feed inlet of the heavy removal tower, and a tower bottom feed outlet is communicated with a residual liquid tank. The residual liquid recovery tower can separate the materials finally led out from the heavy-removal three towers again, so that the rectification yield is improved. The residual liquid recovery tower can directly supply heat by utilizing low-pressure high-temperature steam, and can also supply heat by using a reboiler or a heat exchanger.
In a second aspect, the present invention also provides a thermal energy utilization method using the solvent rectification thermal energy utilization device, including:
(1) Heat energy utilization process
Heating the solvent dehydration tower and the heavy removal three towers by adopting low-pressure high-temperature steam;
heating the heavy-removal second tower by adopting the tower top steam of the heavy-removal third tower;
heating the heavy first stripping tower by adopting the tower top steam of the heavy second stripping tower;
after the temperature of the tower top steam of the solvent dehydration tower is increased by the first heat pump, the heat is supplied to the solvent dehydration tower through the first heat exchanger;
the tower top steam of the heavy-removal first tower is boosted and heated through the second heat pump, and then supplies heat to the heavy-removal third tower through the fourth heat exchanger;
(2) Solvent rectification process
The dehydrated solvent of the solvent dehydration tower is discharged from a discharging line at the bottom of the tower and is fed from a feeding hole of a tower body of the weight removal tower; discharging the heavy component-containing solvent of the first heavy component removal tower from a discharging line at the bottom of the tower, and feeding the heavy component-containing solvent from a feeding hole of a tower body of the second heavy component removal tower; heavy component-containing solvent of the second heavy component removal tower is discharged from a discharge line at the bottom of the tower and is fed from a feed inlet of a tower body of the third heavy component removal tower; heavy component-containing solvent of the heavy component removal three towers is discharged from a discharge line at the bottom of the tower and enters a residual liquid recovery tower;
and respectively condensing the tower top steam of the second heavy removal tower and the tower top steam of the third heavy removal tower through heat exchange, flowing into a reflux tank of the first heavy removal tower, separating the refined solvent, and delivering the refined solvent to a refined solvent storage tank.
Preferably, the temperature of the steam at the top of the solvent dehydration tower (C01) is 80 ℃ or higher, and after the temperature is raised by the first heat pump (K01), the steam pressure is raised by 20% or more, preferably 30% or more, and the steam temperature is raised by 20% or more, preferably 25% or more.
Preferably, the temperature of the top steam of the heavy removal one tower (C02) is more than 80 ℃, after the temperature is increased by the second heat pump (K02), the steam pressure is increased to more than 6 times, preferably more than 8 times, of the original top steam pressure, and the steam temperature is increased by more than 50%, preferably more than 60%.
Preferably, the low pressure high temperature steam has a temperature above 220 ℃. Optionally, the low temperature steam formed after the temperature reduction is used to preheat the crude solvent, or other possible heat exchanges.
The invention at least has the following beneficial effects:
(1) The invention adopts three-effect rectification layout and a thermal circulation mode, one tower supplies steam, three towers circulate, rectification is performed simultaneously, high-temperature steam at the top of the tower is utilized for discharging, heat is provided for the other tower through heat exchange, and heat energy can be utilized for multiple times. The heat energy recycling technology can save steam consumption and reduce the consumption of circulating water.
(2) According to the invention, the heat pump rectification layout is adopted, the grade of heat at the top of the tower is respectively improved by utilizing the double heat pumps, and the heat is transferred to the tower kettle for heating, so that the internal thermal circulation of the solvent dehydration tower and the thermal circulation between the heavy removal first tower and the heavy removal third tower are smoothly realized, and the steam and cooling water consumption is greatly saved; and in the step-up and temperature-rise step of the heat pump, the heat exchange/heat supplement requirements are met, and meanwhile, the operation of hot steam in a pipeline is accelerated, and the heat dissipation is reduced.
(3) According to the invention, heat transfer in the tower and among multiple towers is efficiently realized by integrating heat pump rectification and triple-effect rectification, so that the heat energy utilization efficiency of the system is further improved, the steam and circulating water consumption is reduced, and the production cost is reduced.
Drawings
FIG. 1 is a schematic diagram of the connection of a solvent rectification heat energy utilization device integrating heat pump rectification and triple effect rectification according to the present invention;
Reference numerals illustrate: c01-dehydration tower, C02-heavy first-removal tower, C03-heavy second-removal tower, C04-heavy third-removal tower, C05-raffinate recovery tower, E01-dehydration tower heat exchanger, E02-first heat exchanger, E03, E04-additional heat exchanger, E05-preheater, E06-second heat exchanger, E07-third heat exchanger, E08-heavy third-removal tower heat exchanger, E09-fourth heat exchanger, E10-raffinate recovery tower heat exchanger, V01-dehydration tower reflux drum, V02-heavy first-removal tower reflux drum, V03-raffinate drum, V04-heavy second-removal tower vapor phase solvent condensate drum, V05-heavy third-removal tower vapor phase solvent condensate drum, K01-first heat pump, K02-second heat pump.
Detailed Description
In order to better understand the above technical solutions, the following detailed description will be given with reference to the accompanying drawings and specific embodiments. It will be apparent that the described embodiments are only some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The terminology used in the embodiments of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used in this application and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise, the "plurality" generally includes at least two.
It should also be noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a product or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such product or apparatus. Without further limitation, an element defined by the phrase "comprising one … …" does not exclude the presence of other like elements in a commodity or device comprising such elements.
A solvent rectification heat energy utilization device integrating heat pump rectification and triple-effect rectification comprises a solvent dehydration tower (C01), a first de-weight tower (C02), a second de-weight tower (C03), a third de-weight tower (C04), a heat pump group, a heat exchanger group and a material pipeline.
The concrete communication mode of the material pipeline comprises the following steps:
the solvent dehydration tower (C01) is provided with a tower body feeding hole and a tower top feeding hole, on one hand, the tower body feeding hole is communicated with a tower body feeding line, and crude solvent in the tower body feeding line enters the solvent dehydration tower (C01) after being subjected to heat exchange and heating by a dehydration tower heat exchanger (E01); on the other hand, the top feed inlet is communicated with a dehydration tower reflux line, the top steam of the solvent dehydration tower (C01) is boosted and heated through a first heat pump (K01), and enters the dehydration tower reflux tank (V01) after being subjected to heat exchange and temperature reduction with the tower bottom liquid of the solvent dehydration tower (C01) through a first heat exchanger (E02) at the downstream of the top steam, an oil phase discharge port of the dehydration tower reflux tank (V01) is communicated with the dehydration tower reflux line, the dehydration tower reflux line is sequentially communicated with a solvent preheater (E05) and the top feed inlet of the solvent dehydration tower (C01), and a crude solvent supply line is communicated with the dehydration tower reflux line at the upstream of the solvent preheater (E05), and the other part of crude solvent enters the dehydration tower through the top feed inlet in a reflux material following manner.
The tower bottom discharge line of the solvent dehydration tower (C01) is communicated with the tower body feed inlet of the heavy first tower (C02), the tower bottom discharge line of the heavy first tower (C02) is communicated with the tower body feed inlet of the heavy second tower (C03), the tower bottom discharge line of the heavy second tower (C03) is communicated with the tower body feed inlet of the heavy third tower (C04), the tower bottom discharge line of the heavy third tower (C04) is communicated with the tower top feed inlet of the residual liquid recovery tower (C05), the tower top discharge outlet of the residual liquid recovery tower (C05) is communicated with the tower body feed inlet of the heavy first tower (C02), and the tower bottom discharge outlet of the residual liquid recovery tower (C05) is communicated with the residual liquid tank (V03).
The tower top steam of the heavy-removal three-tower (C04) passes through a third heat exchanger (E07), exchanges heat with tower kettle liquid of the heavy-removal two-tower (C03), and enters a heavy-removal one-tower reflux tank (V02) through a heavy-removal three-tower gas-phase solvent condensate tank (V05) and a solvent preheater (E05);
the tower top steam of the second heavy removal tower (C03) passes through a second heat exchanger (E06) and exchanges heat with the tower bottom liquid of the first heavy removal tower (C02), and then enters a first heavy removal tower reflux tank (V02) through a second heavy removal tower solvent vapor phase condensate tank (V04) and a solvent preheater (E05);
The tower top steam of the heavy-removal first tower (C02) passes through a second heat pump (K02) and a fourth heat exchanger (E09) to exchange heat with tower kettle liquid of the heavy-removal third tower (C04), and then enters a heavy-removal first tower reflux tank (V02);
The oil phase discharge port of the heavy-removal one-tower reflux tank (V02) is communicated with the top feed port of the heavy-removal one-tower (C02) through a heavy-removal one-tower reflux line, and the refined solvent discharge port of the heavy-removal one-tower reflux tank (V02) is communicated with the refined solvent storage tank.
The heat circulation/heat exchange circuit specifically comprises:
the solvent dehydration tower (C01), the heavy metal removal tower (C04) and the raffinate recovery tower (C05) comprise low-pressure high-temperature steam heating wires;
the tower top steam of the solvent dehydration tower (C101) is subjected to pressure boosting and temperature rising through a first heat pump (K01) and then exchanges heat with the tower bottom liquid of the solvent dehydration tower (C01);
The tower top steam of the heavy-removal three tower (C04) exchanges heat with the tower bottom liquid of the heavy-removal two tower (C03) to supply heat to the heavy-removal two tower (C03); specifically, the tower top steam of the heavy-removal three-tower (C04) passes through a third heat exchanger (E07), exchanges heat with tower kettle liquid of the heavy-removal two-tower (C03), and enters a heavy-removal one-tower reflux tank (V02) through a heavy-removal three-tower gas phase solvent condensate tank (V05) and a solvent preheater (E05);
The tower top steam of the second heavy removal tower (C03) exchanges heat with the tower bottom liquid of the first heavy removal tower (C02) to supply heat to the first heavy removal tower (C02); specifically, the tower top steam of the second heavy removal tower (C03) passes through a second heat exchanger (E06) and exchanges heat with the tower bottom liquid of the first heavy removal tower (C02), and then enters a first heavy removal tower reflux tank (V02) through a second heavy removal tower solvent vapor phase condensate tank (V04) and a solvent preheater (E05);
the tower top steam of the heavy-removal first tower (C02) is subjected to pressure boosting and temperature rising through the second heat pump (K02) and then exchanges heat with the tower bottom liquid of the heavy-removal third tower (C04). Specifically, the tower top steam of the heavy first-tower (C02) passes through a second heat pump (K02) and a fourth heat exchanger (E09) to exchange heat with tower bottom liquid of the heavy third-tower (C04), and then enters a heavy first-tower reflux tank (V02);
The oil phase discharge port of the heavy-duty one-tower reflux tank (V02) is communicated with the tower top feed port of the heavy-duty one-tower (C02) through a heavy-duty one-tower reflux line; at least one additional heat exchanger (E03, E04) is arranged on the top discharge line of the heavy-removal three-column (C04) between the heavy-removal three-column gas-phase solvent condensate tank (V05) and the heavy-removal one-column reflux tank (V02) downstream of the solvent preheater (E05); and a refined solvent discharge port of the heavy-removal one-tower reflux tank (V02) is communicated with a refined solvent storage tank.
In the circuit, the low-pressure high-temperature steam supply wire supplies heat to the outside of the solvent dehydration tower (C01) through the dehydration tower heat exchanger (E01), and the consumption of the external low-pressure high-temperature steam is adjusted according to the heat exchange condition of the tower top steam of the dehydration tower (C01) and the first heat exchanger (E02) through the first heat pump (K01) boosting and heating heat pump rectifying circuit, so that the energy-saving effect of reducing the consumption of the external steam is achieved. Similarly, the low-pressure high-temperature steam supply line supplies heat to the heavy-removal three-column (C04) through the heavy-removal three-column heat exchanger (E08), and the consumption of the external low-pressure high-temperature steam is adjusted according to the heat exchange condition that the steam at the top of the heavy-removal one-column (C02) passes through the second heat pump (K02) boosting and heating heat pump rectifying circuit and the fourth heat exchanger (E09). The low-pressure high-temperature steam has a temperature of more than 220 ℃, and can be used for preheating crude solvent and other low-requirement heat exchange requirements after heat supply is completed and the temperature is reduced.
The temperature of the top steam of the heavy-removal three-tower (C04) is above 120 ℃, the temperature of the top steam of the heavy-removal two-tower (C03) is above 100 ℃, and the temperature of the top steam of the heavy-removal one-tower (C02) is above 85 ℃. The temperature of the vapor at the top of the solvent dehydration tower (C01) is above 80 ℃. After the first heat pump (K01) is used for boosting and heating, the steam pressure is increased by more than 20%, preferably more than 30%, and the steam temperature is increased by more than 20%, preferably more than 25%. The temperature of the top steam of the heavy-removal one-tower (C02) is more than 80 ℃, after the pressure and the temperature of the top steam are raised through the second heat pump (K02), the pressure of the steam is raised to more than 6 times, preferably more than 8 times, of the original top steam pressure, and the temperature of the steam is raised to more than 50%, preferably more than 60%.
In addition, when the boosting heating power of the first heat pump (K01) and the second heat pump (K02) is higher, the heat exchanger (E01) of the dehydration tower and the heat exchanger (E08) of the heavy-duty three tower can be used as a preheater only.
The heat energy utilization method based on the solvent rectification heat energy utilization device comprises the following steps:
(1) Heat energy utilization process
Heating the solvent dehydration tower (C01) and the heavy-removal three tower (C04) by adopting low-pressure high-temperature steam; the temperature of the low-pressure high-temperature steam is above 220 ℃, preferably above 230 ℃, and the low-temperature steam is cooled to low-temperature steam after heat supply is finished, and can be used for preheating the crude solvent;
heating the heavy-removal second tower (C03) by adopting the tower top steam of the heavy-removal third tower (C04); the temperature of the top steam of the heavy-removal three-column (C04) is above 120 ℃;
Heating the first heavy removal tower (C02) by adopting the tower top steam of the second heavy removal tower (C03); the temperature of the top steam of the heavy-removal second tower (C03) is above 100 ℃;
The tower top steam of the solvent dehydration tower (C01) is boosted and heated through a first heat pump (K01), and then supplies heat to the solvent dehydration tower (C01) through a first heat exchanger (E02); the temperature of the steam at the top of the solvent dehydration tower (C01) is above 80 ℃, the steam pressure is raised by above 20%, preferably by above 30%, and the steam temperature is raised by above 20%, preferably by above 25% through the first heat pump (K01);
the tower top steam of the heavy-removal first tower (C02) is boosted and heated through the second heat pump (K02), and then supplies heat to the heavy-removal third tower (C04) through the fourth heat exchanger (E09); the temperature of the top steam of the heavy-removal one tower (C02) is above 80 ℃, after the steam passes through the second heat pump (K02), the pressure of the steam is raised to be above 6 times, preferably above 8 times, the pressure of the original top steam, and the temperature of the steam is raised by above 50%, preferably above 60%;
(2) Solvent rectification process
The dehydrated solvent of the solvent dehydration tower (C01) is discharged from a discharging line at the bottom of the tower and is fed from a feeding hole of the tower body of the heavy-removal tower (C02); the heavy component-containing solvent of the first heavy component removal tower (C02) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the second heavy component removal tower (C03); heavy component-containing solvent of the second heavy component removal tower (C03) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the third heavy component removal tower (C04); discharging heavy component-containing solvent from a discharging line at the bottom of the heavy component-removing three towers (C04), and feeding the heavy component-containing solvent into a raffinate recovery tower (C05);
And respectively condensing the tower top steam of the second heavy removal tower (C03) and the third heavy removal tower (C06) through heat exchange, flowing into a first heavy removal tower reflux tank (V02), separating the refined solvent, and delivering the refined solvent to a refined solvent storage tank.
By the solvent rectification heat energy utilization device integrating heat pump rectification and triple effect rectification and the heat energy utilization method thereof, on the basis of opening circulation of a double heat pump system, the steam and circulating water are obviously saved, the steam saving amount is about 8-15t/h, and the circulating water saving amount is about 50-70t/h.
Example 1
The utility model provides a solvent rectification heat energy utilization device of integrated heat pump rectification and triple effect rectification, includes solvent dehydration tower unit, the first tower unit of weightlessness, the second tower unit of weightlessness, the third tower unit of weightlessness and raffinate recovery unit that connects gradually, wherein:
(1) The solvent dehydration column unit includes at least: a solvent dehydration tower (C01), a first heat pump (K01), a first heat exchanger (E02), a dehydration tower reflux tank (V01), a preheater (E05) and an external low-pressure high-temperature steam source dehydration tower heat exchanger (E01) are communicated;
(2) The solvent stripping one-column unit comprises: a de-weight one-tower (C02), a second heat pump (K02), a second heat exchanger (E06), a de-weight one-tower reflux drum (V02);
(3) The solvent heavy-removal two-column unit comprises: a second heavy removal tower (C03), a third heat exchanger (E07), and a second heavy removal tower vapor phase solvent condensate tank (V04);
(4) The solvent heavy-removal three-column unit comprises: a heavy-removal three-tower (C04), a fourth heat exchanger (E09), a heavy-removal three-tower gas-phase solvent condensate tank (V05) and an external low-pressure high-temperature steam source heavy-removal three-tower heat exchanger (E08) are communicated;
(5) The raffinate recovery unit includes: a raffinate recovery tower (C05), a raffinate tank (V03), and a raffinate recovery tower heat exchanger (E10).
The device completes heat energy utilization by the following method:
(1) Heat energy utilization process
Heating a solvent dehydration tower (C01), a heavy removal three tower (C04) and a residual liquid recovery tower (C05) by using low-pressure high-temperature steam at 230+/-5 ℃, cooling the heated materials to low-temperature steam, and using the low-temperature steam for preheating a crude solvent;
heating the heavy-removal second tower (C03) by adopting tower top steam with the temperature of 140+/-5 ℃ of the heavy-removal third tower (C04);
heating the first heavy removal tower (C02) by adopting tower top steam with the temperature of 110+/-5 ℃ of the second heavy removal tower (C03);
Wherein, the temperature of the tower bottom of the solvent dehydration tower (C01) is about 95+/-2 ℃, the pressure is about 150+/-5 KPaA, the temperature of the vapor at the top of the extracted tower is about 85+/-2 ℃, the pressure is 120+/-5 KPaA, the flow is about 8000-12000kg/h, after the temperature is raised by the first heat pump (K01), the vapor temperature is raised to about 110+/-5 ℃, the pressure is raised to about 160KPaA, and the heat is exchanged with the tower bottom liquid by the first heat exchanger (E02), thereby supplying heat to the solvent dehydration tower (C01); the first heat pump (K01) increases the steam pressure by about 33% and the steam temperature by about 30%;
the temperature of the tower bottom of the heavy-removal first tower (C02) is about 90+/-2 ℃, the pressure is about 160-190KPaA, the temperature of the vapor at the top of the extracted tower is about 85+/-2 ℃, the pressure is 130+/-5 KPaA, the flow is about 30000-35000kg/h, after the pressure is increased and the temperature is raised through a second heat pump (K02), the vapor temperature is increased to 138+/-2 ℃, the pressure is increased to about 1100KPaA, and the heat is supplied to the heavy-removal third tower (C04) through a fourth heat exchanger (E09); the second heat pump (K02) increases the steam pressure to about 8.5 times the original overhead steam pressure, and increases the steam temperature by about 62%.
After the heat supply is completed, the reflux and weight-removing one-tower reflux tank (V02) is arranged, an oil phase discharge port of the weight-removing one-tower reflux tank (V02) is communicated with a tower top feed port of the weight-removing one-tower (C02) through a weight-removing one-tower reflux line, the energy saving purpose of condensation reflux is achieved, and a refined solvent discharge port of the weight-removing one-tower reflux tank (V02) is communicated with a refined solvent storage tank.
(2) Solvent rectification process
The dehydrated solvent of the solvent dehydration tower (C01) is discharged from a discharge line at the bottom of the tower, the extraction flow is about 90000-120000kg/h, and the dehydrated solvent is fed from a tower body feed inlet of the weight-removing tower (C02);
the heavy component-containing solvent of the first heavy component removal tower (C02) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the second heavy component removal tower (C03);
Heavy component-containing solvent of the second heavy component removal tower (C03) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the third heavy component removal tower (C04);
The heavy component-containing solvent in the tower of the heavy component removal three towers (C04) is discharged from a discharging line at the bottom of the tower, and enters the residual liquid recovery tower (C05) from a feeding port at the top of the residual liquid recovery tower (C05).
The bottom extraction flow rates of the first heavy-removal tower (C02), the second heavy-removal tower (C03) and the third heavy-removal tower (04) are respectively about 400-800kg/h.
The tower top steam of the second heavy-removal tower (C03) and the third heavy-removal tower (C06) flows into a first heavy-removal tower reflux tank (V02) after heat exchange and condensation, and the refined solvent is separated and sent to a refined solvent storage tank.
The top discharge port of the residual liquid recovery tower (C05) is communicated with the tower body feed port of the heavy-removal first tower (C02), and the bottom discharge port is communicated with the residual liquid tank (V03).
By the solvent rectification heat energy utilization device integrating heat pump rectification and triple-effect rectification and the heat energy utilization method thereof, on the basis of opening circulation of a double heat pump system, the steam and circulating water are obviously saved, and the main consumption is electric consumption. Compared with a three-effect rectifying device which supplies heat to each tower through external steam, the total steam saving amount is about 9.8t/h, the circulating water saving amount is about 62.5t/h, the electricity price is 0.7 yuan/kW.h, the steam price is 220 yuan/ton, the circulating water price is 0.18 yuan/ton, the annual running time is 8000 hours, and after the power consumption is deducted, the total energy saving benefit is about 1300 yuan/h, and the annual balance is about 1000 ten thousands yuan.
Comparative example 1
The comparative example is a solvent rectification heat energy utilization device integrating heat pump rectification and triple effect rectification, and the main difference from the embodiment 1 is that only the first heat pump (K01) is started, the top steam of the heavy removal one tower (C01) is used for preheating a crude solvent and then flows back to the heavy removal one tower reflux tank (V02), and the heat is not supplemented to the heavy removal three towers (C04).
The device of this comparative example specifically includes a solvent dehydration column unit, a first-column-for-weight removal unit, a second-column-for-weight removal unit, a third-column-for-weight removal unit, and a raffinate recovery unit, which are connected in sequence, wherein:
(1) The solvent dehydration column unit includes at least: a solvent dehydration tower (C01), a first heat pump (K01), a first heat exchanger (E02), a dehydration tower reflux tank (V01), a preheater (E05) and an external low-pressure high-temperature steam source dehydration tower heat exchanger (E01) are communicated;
(2) The solvent stripping one-column unit comprises: a first heavy removal tower (C02), a second heat exchanger (E06), and a first heavy removal tower reflux drum (V02);
(3) The solvent heavy-removal two-column unit comprises: a second heavy removal tower (C03), a third heat exchanger (E07), and a second heavy removal tower vapor phase solvent condensate tank (V04);
(4) The solvent heavy-removal three-column unit comprises: a three-tower heavy-removal tower (C04), a three-tower heavy-removal tower vapor phase solvent condensate tank (V05) and an external low-pressure high-temperature steam source three-tower heavy-removal heat exchanger (E08) are communicated;
(5) The raffinate recovery unit includes: a raffinate recovery tower (C05), a raffinate tank (V03), and a raffinate recovery tower heat exchanger (E10).
The device completes heat energy utilization by the following method:
(1) Heat energy utilization process
Heating a solvent dehydration tower (C01), a heavy removal three tower (C04) and a residual liquid recovery tower (C05) by using low-pressure high-temperature steam at 230+/-5 ℃, cooling the heated materials to low-temperature steam, and using the low-temperature steam for preheating a crude solvent;
heating the heavy-removal second tower (C03) by adopting tower top steam with the temperature of 140+/-5 ℃ of the heavy-removal third tower (C04);
heating the first heavy removal tower (C02) by adopting tower top steam with the temperature of 115+/-5 ℃ of the second heavy removal tower (C03);
Wherein, the temperature of the tower bottom of the solvent dehydration tower (C01) is about 95+/-2 ℃, the pressure is about 160+/-5 KPaA, the temperature of the vapor at the top of the extracted tower is about 82+/-2 ℃, the pressure is 130+/-5 KPaA, the flow is about 8000-12000kg/h, after the temperature is raised by the first heat pump (K01), the vapor temperature is raised to about 110+/-5 ℃, the pressure is raised to about 160KPaA, and the heat is exchanged with the tower bottom liquid by the first heat exchanger (E02), thereby supplying heat to the solvent dehydration tower (C01); the first heat pump (K01) increases the steam pressure by about 23% and the steam temperature by about 34%;
The temperature of the vapor at the top of the stripping tower (C02) is about 88+/-2 ℃, the pressure is 115+/-5 KPaA, the flow is about 10000-15000kg/h, after the crude solvent is preheated, the crude solvent flows into the stripping tower reflux tank (V02), the oil phase discharge port of the stripping tower reflux tank (V02) is communicated with the top feed port of the stripping tower (C02) through the stripping tower reflux line, the energy saving purpose of condensation reflux is achieved, and the refined solvent discharge port of the stripping tower reflux tank (V02) is communicated with the refined solvent storage tank.
(2) Solvent rectification process
The dehydrated solvent of the solvent dehydration tower (C01) is discharged from a discharge line at the bottom of the tower, the extraction flow is about 90000-120000kg/h, and the dehydrated solvent is fed from a tower body feed inlet of the weight-removing tower (C02);
the heavy component-containing solvent of the first heavy component removal tower (C02) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the second heavy component removal tower (C03);
Heavy component-containing solvent of the second heavy component removal tower (C03) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the third heavy component removal tower (C04);
The heavy component-containing solvent in the tower of the heavy component removal three towers (C04) is discharged from a discharging line at the bottom of the tower, and enters the residual liquid recovery tower (C05) from a feeding port at the top of the residual liquid recovery tower (C05).
The top discharge port of the residual liquid recovery tower (C05) is communicated with the tower body feed port of the heavy-removal first tower (C02), and the bottom discharge port is communicated with the residual liquid tank (V03).
The bottom extraction flow rates of the first heavy-removal tower (C02), the second heavy-removal tower (C03) and the third heavy-removal tower (04) are respectively about 400-800kg/h.
The tower top steam of the first heavy removal tower (C02), the second heavy removal tower (C03) and the third heavy removal tower (C06) flows into a first heavy removal tower reflux tank (V02) after heat exchange condensation, the refined solvent is separated, the refined solvent is discharged from a discharge port and is sent to a refined solvent storage tank, and an oil phase discharge port is communicated with a tower top feed port of the first heavy removal tower (C02) through a first heavy removal tower reflux line, so that the energy saving purpose of condensation reflux is achieved.
According to the solvent rectification heat energy utilization device and the heat energy utilization method for integrating heat pump rectification and triple effect rectification in the comparison example, on the basis of the opening cycle of the first heat pump, the consumption of steam and circulating water is saved to a certain extent compared with the triple effect rectification device which supplies heat to each tower respectively only through external steam. The steam saving amount is about 1.8t/h, the circulating water saving amount is about 14.5t/h, the electricity price is 0.7 yuan/kW.h, the steam price is 220 yuan/ton, the circulating water price is 0.18 yuan/ton, the annual running time is estimated according to 8000 hours, after the power consumption is deducted, the total energy saving benefit is about 320 yuan/h, and the annual balance is about 257 ten thousands.
Comparative example 2
The present comparative example is also a solvent distillation heat energy utilization device integrating heat pump distillation and triple effect distillation, and the main difference from the embodiment 1 is that only the second heat pump (K02) is started, and the solvent dehydration tower (C01) only relies on external low pressure high temperature steam for heat supply.
The device specifically comprises a solvent dehydration tower unit, a weight-removing first tower unit, a weight-removing second tower unit, a weight-removing third tower unit and a residual liquid recovery unit which are connected in sequence, wherein:
(1) The solvent dehydration column unit includes at least: a solvent dehydration tower (C01), a dehydration tower reflux tank (V01), a preheater (E05) and an external low-pressure high-temperature steam source dehydration tower heat exchanger (E01);
(2) The solvent stripping one-column unit comprises: a de-weight one-tower (C02), a second heat pump (K02), a second heat exchanger (E06), a de-weight one-tower reflux drum (V02);
(3) The solvent heavy-removal two-column unit comprises: a second heavy removal tower (C03), a third heat exchanger (E07), and a second heavy removal tower vapor phase solvent condensate tank (V04);
(4) The solvent heavy-removal three-column unit comprises: a heavy-removal three-tower (C04), a fourth heat exchanger (E09), a heavy-removal three-tower gas-phase solvent condensate tank (V05) and an external low-pressure high-temperature steam source heavy-removal three-tower heat exchanger (E08) are communicated;
(5) The raffinate recovery unit includes: a raffinate recovery tower (C05), a raffinate tank (V03), and a raffinate recovery tower heat exchanger (E10).
The device completes heat energy utilization by the following method:
(1) Heat energy utilization process
Heating a solvent dehydration tower (C01), a heavy removal three tower (C04) and a residual liquid recovery tower (C05) by using low-pressure high-temperature steam at 230+/-5 ℃, cooling the heated materials to low-temperature steam, and using the low-temperature steam for preheating a crude solvent;
heating the heavy-removal second tower (C03) by adopting tower top steam with the temperature of 140+/-5 ℃ of the heavy-removal third tower (C04);
heating the first heavy removal tower (C02) by adopting tower top steam with the temperature of 110+/-5 ℃ of the second heavy removal tower (C03);
The method comprises the steps that after the raw solvent raw material is heated by an E01-dehydration tower heat exchanger, the raw solvent raw material is fed through a tower body feed inlet of a solvent dehydration tower (C01), the temperature of a tower kettle of the solvent dehydration tower (C01) is about 95+/-2 ℃, the pressure is about 150+/-5 KPa, the temperature of extracted tower top steam is about 85+/-2 ℃, the pressure is about 130+/-5 KPa, the flow is about 8000-12000kg/h, the tower top steam enters a dehydration tower reflux tank (V01), an oil phase discharge port of the dehydration tower reflux tank (V01) is communicated with a dehydration tower reflux line, the dehydration tower reflux line is sequentially communicated with a solvent preheater (E05) and a tower top feed inlet of the solvent dehydration tower (C01), and a crude solvent supply line is communicated with the dehydration tower reflux line at the upstream of the solvent preheater (E05);
The temperature of the tower bottom of the heavy-removal first tower (C02) is about 135+/-2 ℃, the pressure is about 160-190KPaA, the temperature of the vapor at the top of the extracted tower is about 85+/-2 ℃, the pressure is 115+/-5 KPaA, the flow is about 30000-35000kg/h, after the pressure is increased and the temperature is raised through a second heat pump (K02), the vapor temperature is increased to 150+/-2 ℃, the pressure is increased to about 1100KPaA, and the heat is supplied to the heavy-removal third tower (C04) through a fourth heat exchanger (E09); the second heat pump (K02) increases the steam pressure to about 9.6 times the original overhead steam pressure, and increases the steam temperature by about 76%.
After the heat supply is completed, the reflux and weight-removing one-tower reflux tank (V02) is arranged, an oil phase discharge port of the weight-removing one-tower reflux tank (V02) is communicated with a tower top feed port of the weight-removing one-tower (C02) through a weight-removing one-tower reflux line, the energy saving purpose of condensation reflux is achieved, and a refined solvent discharge port of the weight-removing one-tower reflux tank (V02) is communicated with a refined solvent storage tank.
(2) Solvent rectification process
The dehydrated solvent of the solvent dehydration tower (C01) is discharged from a discharge line at the bottom of the tower, the extraction flow is about 90000-120000kg/h, and the dehydrated solvent is fed from a tower body feed inlet of the weight-removing tower (C02);
the heavy component-containing solvent of the first heavy component removal tower (C02) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the second heavy component removal tower (C03);
Heavy component-containing solvent of the second heavy component removal tower (C03) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the third heavy component removal tower (C04);
The heavy component-containing solvent in the tower of the heavy component removal three towers (C04) is discharged from a discharging line at the bottom of the tower, and enters the residual liquid recovery tower (C05) from a feeding port at the top of the residual liquid recovery tower (C05).
The bottom extraction flow rates of the first heavy-removal tower (C02), the second heavy-removal tower (C03) and the third heavy-removal tower (04) are respectively about 400-800kg/h.
The tower top steam of the second heavy-removal tower (C03) and the third heavy-removal tower (C06) flows into a first heavy-removal tower reflux tank (V02) after heat exchange and condensation, and the refined solvent is separated and sent to a refined solvent storage tank.
The top discharge port of the residual liquid recovery tower (C05) is communicated with the tower body feed port of the heavy-removal first tower (C02), and the bottom discharge port is communicated with the residual liquid tank (V03).
According to the solvent rectification heat energy utilization device and the heat energy utilization method for integrating heat pump rectification and triple effect rectification in the comparison example, on the basis of opening circulation of the second heat pump (K02), the consumption of steam and circulating water is saved to a certain extent compared with the triple effect rectification device which supplies heat to each tower through external steam. The steam saving amount is about 7.5t/h, the circulating water saving amount is about 45.2t/h, the electricity price is 0.7 yuan/kW.h, the steam price is 220 yuan/ton, the circulating water price is 0.18 yuan/ton, the annual running time is estimated according to 8000 hours, after the power consumption is deducted, the total energy saving benefit is about 840 yuan/h, and the annual balance is about 670 ten thousand.
Compared with a three-effect rectifying device which supplies heat to each tower respectively through external steam, the embodiment and the comparative example have the advantages of saving steam and circulating water and integrally showing the combination of heat pump rectification and multi-effect rectification. Compared with the steam saving amount and the circulating water saving amount of the two comparative examples, the embodiment has more obvious advantages, is higher than the simple superposition of the two, mainly has more effective and convenient cooperative allocation and use of heat and cold after the whole system is designed and laid out, improves the energy utilization rate, and further shows the remarkable advantages of the synergy between the heat pump rectification technology adopting the double heat pump and the triple-effect rectification energy-saving technology.
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. Therefore, the present invention includes the preferred embodiments and all the variations and modifications associated therewith. It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit and scope of the invention, and it is intended that the invention encompass such modifications and variations as fall within the scope of the invention and its equivalents.
Claims (10)
1. A solvent rectification heat energy utilization device integrating heat pump rectification and triple-effect rectification is characterized in that: comprises a solvent dehydration tower (C01), a first heavy-removal tower (C02), a second heavy-removal tower (C03), a third heavy-removal tower (C04), a heat pump set, a heat exchanger set and a material pipeline;
the bottom discharge line of the solvent dehydration tower (C01) is communicated with the tower body feed inlet of the first heavy removal tower (C02), the bottom discharge line of the first heavy removal tower (C02) is communicated with the tower body feed inlet of the second heavy removal tower (C03), and the bottom discharge line of the second heavy removal tower (C03) is communicated with the tower body feed inlet of the third heavy removal tower (C04);
the solvent dehydration tower (C01) and the heavy-removal three tower (C04) comprise low-pressure high-temperature steam heating wires;
the tower top steam of the solvent dehydration tower (C101) is subjected to pressure boosting and temperature rising through a first heat pump (K01) and then exchanges heat with the tower bottom liquid of the solvent dehydration tower (C01);
The tower top steam of the heavy-removal three tower (C04) exchanges heat with the tower bottom liquid of the heavy-removal two tower (C03) to supply heat to the heavy-removal two tower (C03);
The tower top steam of the second heavy removal tower (C03) exchanges heat with the tower bottom liquid of the first heavy removal tower (C02) to supply heat to the first heavy removal tower (C02);
The tower top steam of the heavy-removal first tower (C02) is subjected to pressure boosting and temperature rising through the second heat pump (K02) and then exchanges heat with the tower bottom liquid of the heavy-removal third tower (C04).
2. The solvent rectification heat energy utilization device as claimed in claim 1, wherein the top steam of the solvent dehydration tower (C01) passes through the first heat pump (K01) and the first heat exchanger (E02), exchanges heat with the tower bottom liquid of the solvent dehydration tower (C01), and then enters the dehydration tower reflux tank (V01), an oil phase discharge port of the dehydration tower reflux tank (V01) is communicated with a dehydration tower reflux line, and the dehydration tower reflux line is sequentially communicated with the solvent preheater (E05) and a top feed port of the solvent dehydration tower (C01);
optionally, upstream of the solvent preheater (E05), a crude solvent supply line communicates with the dehydration column return line.
3. The solvent rectification heat energy utilization device as claimed in claim 2, wherein the top steam of the first heavy removal tower (C02) passes through a second heat pump (K02) and a fourth heat exchanger (E09), exchanges heat with the tower bottom liquid of the third heavy removal tower (C04), and enters a first heavy removal tower reflux tank (V02);
the oil phase discharge port of the heavy-duty one-tower reflux tank (V02) is communicated with the tower top feed port of the heavy-duty one-tower (C02) through a heavy-duty one-tower reflux line;
and a refined solvent discharge port of the heavy-removal one-tower reflux tank (V02) is communicated with a refined solvent storage tank.
4. A solvent rectification heat energy utilization device as claimed in claim 3, wherein the top steam of the second de-weight tower (C03) passes through a second heat exchanger (E06) to exchange heat with the tower bottom liquid of the first de-weight tower (C02), and then enters the first de-weight tower reflux tank (V02) through a second de-weight tower gas-phase solvent condensate tank (V04) and a solvent preheater (E05);
The tower top steam of the heavy-removal three-tower (C04) passes through a third heat exchanger (E07), exchanges heat with tower kettle liquid of the heavy-removal two-tower (C03), and enters the heavy-removal one-tower reflux tank (V02) through the heavy-removal three-tower gas phase solvent condensate tank (V05) and the solvent preheater (E05).
5. The apparatus according to claim 4, wherein at least one additional heat exchanger (E03, E04) is further provided on the top discharge line of the three-heavy-removal column (C04) downstream of the solvent preheater (E05) between the three-heavy-removal column vapor phase solvent condensate tank (V05) and the one-heavy-removal column reflux tank (V02).
6. The heat energy utilization device for solvent distillation according to any one of claims 1 to 5, further comprising a raffinate recovery column (C05), wherein a top feed port of the raffinate recovery column (C05) is connected to a bottom discharge line of the heavy-removal three column (C04), wherein a top discharge port of the raffinate recovery column is connected to a column body feed port of the heavy-removal one column (C02), and wherein a bottom discharge port of the raffinate tank (V03).
7. A heat energy utilization method employing the solvent rectification heat energy utilization device of any one of claims 1 to 6, comprising:
(1) Heat energy utilization process
Heating the solvent dehydration tower (C01) and the heavy-removal three tower (C04) by adopting low-pressure high-temperature steam;
heating the heavy-removal second tower (C03) by adopting the tower top steam of the heavy-removal third tower (C04);
Heating the first heavy removal tower (C02) by adopting the tower top steam of the second heavy removal tower (C03);
the tower top steam of the solvent dehydration tower (C01) is boosted and heated through a first heat pump (K01), and then supplies heat to the solvent dehydration tower (C01) through a first heat exchanger (E02);
The tower top steam of the heavy-removal first tower (C02) is boosted and heated through the second heat pump (K02), and then supplies heat to the heavy-removal third tower (C04) through the fourth heat exchanger (E09);
(2) Solvent rectification process
The dehydrated solvent of the solvent dehydration tower (C01) is discharged from a discharging line at the bottom of the tower and is fed from a feeding hole of the tower body of the heavy-removal tower (C02); the heavy component-containing solvent of the first heavy component removal tower (C02) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the second heavy component removal tower (C03); heavy component-containing solvent of the second heavy component removal tower (C03) is discharged from a discharge line at the bottom of the tower and is fed from a tower body feed inlet of the third heavy component removal tower (C04); discharging heavy component-containing solvent from a discharging line at the bottom of the heavy component-removing three towers (C04), and feeding the heavy component-containing solvent into a raffinate recovery tower (C05);
And respectively condensing the tower top steam of the second heavy removal tower (C03) and the third heavy removal tower (C06) through heat exchange, flowing into a first heavy removal tower reflux tank (V02), separating the refined solvent, and delivering the refined solvent to a refined solvent storage tank.
8. The heat energy utilization method according to claim 7, wherein the temperature of the top steam of the solvent dehydration column (C01) is 80 ℃ or higher, the pressure of the steam is raised by 20% or more and the temperature of the steam is raised by 20% or more after the temperature is raised by the first heat pump (K01).
9. The heat energy utilization method according to claim 7, wherein the temperature of the top steam of the heavy-removal one column (C02) is more than 80 ℃, the pressure of the steam is increased to more than 6 times of the original top steam pressure after the temperature is increased by the second heat pump (K02), and the steam temperature is increased by more than 50%.
10. The heat energy utilization method according to claim 7 or 8, wherein the temperature of the low-pressure high-temperature steam is 220 ℃ or higher.
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