CN111450561A - Energy-saving carrier gas stripping system and stripping process - Google Patents
Energy-saving carrier gas stripping system and stripping process Download PDFInfo
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- CN111450561A CN111450561A CN202010297307.8A CN202010297307A CN111450561A CN 111450561 A CN111450561 A CN 111450561A CN 202010297307 A CN202010297307 A CN 202010297307A CN 111450561 A CN111450561 A CN 111450561A
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- 239000012159 carrier gas Substances 0.000 title claims abstract description 205
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 103
- 239000007789 gas Substances 0.000 claims abstract description 77
- 239000002994 raw material Substances 0.000 claims abstract description 58
- 239000000945 filler Substances 0.000 claims abstract description 14
- 238000001816 cooling Methods 0.000 claims description 69
- 238000009835 boiling Methods 0.000 claims description 39
- 238000010992 reflux Methods 0.000 claims description 19
- 238000007599 discharging Methods 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 4
- 239000000126 substance Substances 0.000 abstract description 19
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 230000000630 rising effect Effects 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000004821 distillation Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012847 fine chemical Substances 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 206010057040 Temperature intolerance Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000008543 heat sensitivity Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000000199 molecular distillation Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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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
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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
- B01D3/10—Vacuum distillation
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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
- B01D3/14—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
-
- 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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- 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
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
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Abstract
The invention belongs to the technical field of stripping separation, and relates to an energy-saving carrier gas stripping system and a stripping process, which comprises a stripping tower, a separation tank, a raw material heater, a carrier gas heater and a gas circulating heat exchanger; the top in the stripping tower is provided with a heat and mass transfer section, and the stripping tower, the gas circulating heat exchanger and the heat and mass transfer section are sequentially communicated through a pipeline; the gas circulation heat exchanger, the separating tank and the stripping tower are communicated in sequence through pipelines; the raw material heater is communicated with the stripping tower; the heat exchange mass transfer section, the carrier gas heater and the gas stripping tower are sequentially communicated through a pipeline; the heat exchange mass transfer section comprises a heat exchange tube and a filler, and the heat exchange tube is a tube type heat exchange tube or a coil type heat exchange tube. The invention has low separation temperature, adopts different carrier gas heating modes for heat exchange and mass transfer, realizes enrichment separation of one or more substances through stripping and rectification, has good separation effect, recycles the heat of the system, reduces the heat consumption and the cold consumption of the separation and saves the energy consumption by 30-50%.
Description
Technical Field
The invention belongs to the technical field of stripping separation, and relates to an energy-saving carrier gas stripping system and a stripping process.
Background
In chemical production, for the separation of high-viscosity media of some high-boiling media, the separation can not be finished by adopting conventional rectification; a part of thermal sensitive medium, a solid particle-containing system and a colloid system are separated, and the separation cannot be realized by the traditional technology; the medium separation has the problems of high separation temperature, high medium viscosity, poor separation effect of the traditional separation technology, poor fractionation precision, high investment and energy consumption, large occupied area, high operation and maintenance cost and the like due to the adoption of molecular distillation, short-range distillation or thin film distillation and the like.
Disclosure of Invention
The invention provides an energy-saving carrier gas stripping system and a stripping process, aiming at the technical problems of high separation temperature, poor fractionation precision and high energy consumption in the existing stripping separation.
In order to achieve the purpose, the invention adopts the technical scheme that:
an energy-saving carrier gas stripping system comprises a gas stripping tower, a separation tank, a raw material heater, a carrier gas heater and a gas circulating heat exchanger;
a heat exchange mass transfer section is arranged in the stripping tower;
the gas stripping tower, the gas circulating heat exchanger and the separating tank are sequentially connected through pipelines; the gas circulation heat exchanger is connected with the heat and mass transfer section through a pipeline; the separation tank is connected with the stripping tower through a pipeline; the raw material heater is connected with the stripping tower through a pipeline; the heat and mass transfer section is sequentially connected with the carrier gas heater and the gas stripping tower through pipelines.
Further, a raw material inlet, a light component reflux inlet, a carrier gas inlet, a light component outlet, a carrier gas circulating inlet and a heavy component discharge outlet are arranged on the stripping tower; the carrier gas inlet and the carrier gas outlet are both arranged on the heat exchange mass transfer section;
the separation tank is provided with a separation tank inlet, a separation tank top outlet and a separation tank bottom outlet;
the gas circulation heat exchanger is provided with a heat exchanger top inlet, a heat exchanger gas outlet, a heat exchanger bottom outlet and a heat exchanger gas inlet;
the raw material heater is connected with the raw material inlet through a pipeline; the carrier gas outlet is sequentially connected with the carrier gas heater and the carrier gas circulating inlet through a pipeline; the light component outlet is sequentially connected with the top inlet of the heat exchanger, the gas outlet of the heat exchanger and the carrier gas inlet through pipelines;
the light component outlet is sequentially connected with the top inlet of the heat exchanger, the bottom outlet of the heat exchanger and the inlet of the separation tank through pipelines; an outlet at the bottom of the separation tank is connected with a light component reflux inlet through a pipeline; and the gas inlet of the heat exchanger is connected with the outlet at the top of the separation tank through a pipeline.
Furthermore, a first valve is arranged on a pipeline between an outlet at the bottom of the separation tank and the light component backflow inlet.
Further, the heat and mass transfer section comprises a heat exchange tube and a filler, and the heat exchange tube is a tube type heat exchange tube or a coil type heat exchange tube; the filler is arranged inside or outside the heat exchange tube.
Furthermore, the separating tank is also provided with a separating tank light component return opening connected with the outlet at the bottom of the separating tank, and a second valve is arranged on a pipeline between the outlet at the bottom of the separating tank and the separating tank light component return opening.
Further, the carrier gas heater is a direct heater or an indirect heater.
An energy-saving carrier gas stripping process comprises the following steps:
1) after the raw material is preheated and subjected to heat carrier gas mass transfer, heavy components in the raw material are discharged; after the light component is rectified and separated by the heat exchange and mass transfer section along with the carrier gas, the separated condensed component is taken as a product to be extracted; discharging the light components and the carrier gas which are not condensed and have reduced temperature;
2) the discharged carrier gas and light components are subjected to heat exchange and cooling to obtain cooling carrier gas and condensate, and the cooling carrier gas is sent to heat exchange and mass transfer; further cooling and separating the condensate to obtain a low-boiling product and carrier gas, and extracting or partially recycling the low-boiling product; after the carrier gas is subjected to heat exchange and cooling, the cooled carrier gas is sent to heat exchange and mass transfer;
3) and (3) after the cooling carrier gas sent to the heat exchange mass transfer in the step 2) exchanges heat and mass transfer with the carrier gas and the light components in the step 1), the cooling carrier gas recovers part of heat and performs mass transfer with the raw material after heat compensation.
Further, the specific implementation process of the step 1) is that the raw material is heated by a raw material heater and then enters a gas stripping tower, hot light components rise after mass transfer through gas stripping, and heavy components fall and are discharged from a heavy component discharge port through a pump; when the hot light component rises to the top of the stripping tower, the hot light component exchanges heat with cooling carrier gas of a heat exchange mass transfer section, is cooled and is condensed and refluxed by the hot light component, and an obtained intermediate boiling product is extracted from the middle part of the stripping tower, so that purification, rectification and separation are realized; the light component and the carrier gas, the temperature of which is lowered, are discharged from the light component outlet.
Further, the specific implementation process of the step 2) is that the light component and the carrier gas coming out of the light component outlet enter the gas circulation heat exchanger from the top inlet of the heat exchanger for heat exchange and cooling to obtain cooling carrier gas and condensate, the cooling carrier gas comes out of the gas outlet of the heat exchanger and returns to the top of the stripper through the carrier gas inlet to exchange heat with the light component flowing upwards for cooling, the temperature of the light component flowing out of the top of the stripper is reduced, and meanwhile, a medium-boiling product is obtained;
the condensate flows out from an outlet at the bottom of the heat exchanger and enters a separating tank from an inlet of the separating tank to be cooled and separated to obtain a low-boiling product and a small part of carrier gas; a small part of carrier gas is cooled by heat exchange in a gas circulation heat exchanger and then returns to the top of the stripping tower, and a medium boiling product is obtained while the temperature of light components flowing out of the top of the stripping tower is reduced; the low-boiling product is directly recovered after coming out from an outlet at the bottom of the separation tank, or returns to a light component reflux inlet through a first valve; or returned to the light component return port of the separation tank through a second valve.
Further, the specific implementation process of the step 3) is that cooling carrier gas returns to the heat exchange mass transfer section in the stripper from the carrier gas inlet, the cooling carrier gas exchanges heat with the carrier gas and light components which rise continuously in the stripper, and the cooling carrier gas takes away part of heat; and the cooling carrier gas with heat is supplemented by a carrier gas heat exchanger, and then returns to the bottom of the stripping tower to carry out mass transfer with the raw material entering the stripping tower.
The invention has the beneficial effects that:
1. in the invention, waste heat carried out at the top of the stripping tower is recovered through the heat exchange mass transfer section arranged in the stripping tower, the heat of light components discharged from the top of the stripping tower is reduced, the separation temperature can be lower than the normal bubble point temperature, the separation temperature is low, meanwhile, the rectification separation is realized through the heat exchange mass transfer section, the enrichment separation of different substances such as medium-boiling products, low-boiling products and the like is realized, the separation precision is high, and the heat consumption and the cold consumption of the system are reduced.
2. In the invention, the heat exchange mass transfer section comprises a heat exchange tube and a filler, integrates heat exchange, strengthens mass transfer, improves the separation precision of separated objects through stripping and rectification, and realizes enrichment separation of different substances; meanwhile, the temperature of light components at the top of the stripping tower is reduced through the heat exchange tubes, heat can be recycled, 30-50 energy consumption can be saved, and the purpose of energy conservation is achieved.
3. In the invention, the bubble point of the separated substance is reduced through the combined action of the carrier gas and the negative pressure, so that the separated substance can be extracted and separated at the temperature lower than the normal bubble point, and the requirement on the grade of the consumed heat can be further reduced.
4. In the invention, the heat exchange tube in the gas stripping tower is a tube type heat exchange tube or a coil type heat exchange tube, the carrier gas heater is a direct heater or an indirect heater, two heat transfer modes and heat exchange modes are adopted, the process operation and maintenance are simple, the equipment occupies small area, and the device is suitable for separating high-boiling point, heat-sensitive and easily-oxidized substances, and is more suitable for various processes such as extraction, recovery and the like in the food grade medicine fine chemical industry.
Drawings
FIG. 1 is a first carrier gas stripping column separation device provided by the present invention;
FIG. 2 is a second carrier gas stripping column separation device provided by the present invention;
wherein:
1-a stripper column; 11-feedstock inlet; 12-light component reflux inlet; 13-carrier gas inlet; 14-light fraction outlet; 15-carrier gas outlet; 16-carrier gas circulation inlet; 17-heavy component discharge port; 2-a separation tank; 21-inlet of the separation tank; 22-outlet at the top of the separation tank; 23-outlet at bottom of separation tank; 24-a light component reflux opening of the separation tank; 3-raw material reciprocating pump; 4-a raw material heater; 5-carrier gas heater; 6-gas circulation heat exchanger; 61-heat exchanger top inlet; 62-heat exchanger gas outlet; 63-outlet at the bottom of the heat exchanger; 64-heat exchanger gas inlet; 7, a fan; 8-a vacuum pump; 9-pump.
Detailed Description
The invention will now be further elucidated with reference to the drawings and the embodiments.
Example 1
Referring to fig. 1, an energy-saving carrier gas stripping system comprises a stripping tower 1 and a separation tank 2; a raw material heater 4; a carrier gas heater 5 and a gas circulation heat exchanger 6;
a heat and mass exchange section is arranged in the gas stripping tower 1; specifically, a heat and mass transfer section is arranged at the top in the stripping tower 1, so that the light component upwards along with the carrier gas is subjected to heat exchange and cooling through the heat and mass transfer section, and the temperature of the light component is reduced.
The gas stripping tower 1, the gas circulation heat exchanger 6 and the separating tank 2 are connected in sequence through pipelines; the gas circulation heat exchanger 6 is connected with the heat and mass transfer section through a pipeline; the separation tank 2 is connected with the stripping tower 1 through a pipeline; the raw material heater 4 is connected with the stripping tower 1 through a pipeline; the heat exchange and mass transfer section is sequentially connected with the carrier gas heater 5 and the gas stripping tower 1 through pipelines.
In this embodiment, the stripper 1 is provided with a raw material inlet 11, a light component reflux inlet 12, a carrier gas inlet 13, a light component outlet 14, a carrier gas outlet 15, a carrier gas circulation inlet 16, and a heavy component discharge outlet 17.
In the embodiment, the top in the stripping tower 1 is provided with a heat and mass transfer section; the heat and mass transfer section comprises a heat exchange tube and a filler, the heat exchange tube is a tube type heat exchange tube, the filler is arranged in the tube type heat exchange tube, and the carrier gas inlet 13 and the carrier gas outlet 15 are both arranged on the side wall of the heat and mass transfer section.
In this embodiment, the separation tank 2 is provided with a separation tank inlet 21, a separation tank top outlet 22 and a separation tank bottom outlet 23; the top of the separation tank 2 is also provided with a circulating water inlet pipeline and a circulating water outlet pipeline.
In this embodiment, the gas circulation heat exchanger 6 is provided with a heat exchanger top inlet 61, a heat exchanger gas outlet 62, a heat exchanger bottom outlet 63, and a heat exchanger gas inlet 64.
Specifically, the raw material heater 4 is connected with the raw material inlet 11 through a pipeline; the carrier gas outlet 15 is sequentially connected with the carrier gas heater 5 and the carrier gas circulating inlet 16 through pipelines; the light component outlet 14 is sequentially connected with the heat exchanger top inlet 61, the heat exchanger gas outlet 62 and the carrier gas inlet 13 through pipelines; the heavy component discharge opening 17 is connected with a discharge pipeline; the light component outlet 14 is sequentially connected with a heat exchanger top inlet 61, a heat exchanger bottom outlet 63 and a separation tank inlet 21 through pipelines; an outlet 23 at the bottom of the separation tank is connected with a light component reflux inlet 12 through a pipeline; the heat exchanger gas inlet 64 is connected by a line to the separator tank top outlet 22. The outlet 23 at the bottom of the separating tank is connected with the light component reflux inlet 12 through a pipeline, and a first valve is arranged on the pipeline.
In this embodiment, the carrier gas heater 5 is a direct heater.
Referring to fig. 1, in this embodiment, a vacuum pump 8 is further included, which is connected to the separator tank top outlet 22 and the heat exchanger gas inlet 64; a fan 7 is arranged on a pipeline connecting the gas inlet 64 of the heat exchanger with the outlet 22 at the top of the separation tank, and a pump 9 is also arranged between the outlet 23 at the bottom of the separation tank and the first valve.
An energy-saving carrier gas stripping process comprises the following steps:
1) after the raw material is preheated and subjected to heat carrier gas mass transfer, heavy components in the raw material are discharged; after the light component is rectified and separated by the heat exchange and mass transfer section along with the carrier gas, the separated condensed component is taken as a product to be extracted; discharging the light components and the carrier gas which are not condensed and have reduced temperature;
2) the discharged carrier gas and light components are subjected to heat exchange and cooling to obtain cooling carrier gas and condensate, and the cooling carrier gas is sent to heat exchange and mass transfer; further cooling and separating the condensate to obtain a low-boiling product and carrier gas, and extracting or partially recycling the low-boiling product; after the carrier gas is subjected to heat exchange and cooling, the cooled carrier gas is sent to heat exchange and mass transfer;
3) and (3) after the cooling carrier gas sent to the heat exchange mass transfer in the step 2) exchanges heat and mass transfer with the carrier gas and the light components in the step 1), the cooling carrier gas recovers part of heat and performs mass transfer with the raw material after heat compensation.
In this embodiment, the vacuum is provided at the top of the separation tank 2 by a vacuum pump 8.
When the carrier gas stripping is carried out by adopting the embodiment, the principle is that any mode can be selected for liquid through carrier gas and negative pressure, so that the bubble point of the separated substance is reduced to be lower than the working condition that the boiling point of the separated substance is about (0-50 ℃), and the separated substance is separated, cooled and recovered.
The specific separation process is as follows:
1) the raw material is heated by a raw material heater 4 by a raw material reciprocating pump 3 and enters a stripping tower 1 from a raw material inlet 11 for stripping; as the raw material is transferred with the hot carrier gas in the gas stripping tower 1 from the lower part upwards, the heavy component in the raw material is discharged from the heavy component discharge port 17 through the reciprocating pump; the hot light components in the raw materials continuously rise along with the carrier gas and are subjected to heat exchange and cooling through a tube type heat exchange tube at the top of the stripper column 1, the hot light components are cooled and are condensed and refluxed, and the condensed components are taken as middle-boiling components and are extracted from an outlet at the middle part of the side of the stripper column 1, so that purification, rectification and separation are realized; noncondensable components and light components with non-reduced temperature, and discharging the cooled light components from a light component outlet 14 at the top of the stripping tower along with the continuous rising of the carrier gas;
2) the noncondensable components from the light component outlet 14 enter the gas circulation heat exchanger 6 from the heat exchanger top inlet 61 to exchange heat and cool to obtain cooling carrier gas and condensate, the cooling carrier gas comes out from the heat exchanger gas outlet 62 and returns to the tubular heat exchange tube at the top of the stripper column 1 through the carrier gas inlet 13 to exchange heat and cool with the light components which rise and flow through the tubular heat exchange tube, the temperature of the light components flowing out of the top of the stripper column 1 is reduced, and meanwhile, a medium boiling product is obtained;
the condensate flows out from an outlet 63 at the bottom of the heat exchanger and enters the separating tank 21 from an inlet 21 of the separating tank, and a low-boiling product and a small part of carrier gas are obtained through further cooling and separation by circulating water; a small part of carrier gas enters the gas circulation heat exchanger 6 from the heat exchanger gas inlet 64 after passing through the fan 7 for heat exchange and cooling, then comes out from the heat exchanger gas outlet 62 and returns to the tubular heat exchange tube at the top of the stripper column 1 through the carrier gas inlet 13, so that the temperature of light components flowing out of the top of the stripper column 1 is reduced, and meanwhile, a medium-boiling product is obtained; the low-boiling product is recovered after coming out from an outlet 23 at the bottom of the separation tank or returns to the light component reflux inlet 12 through a first valve, and during implementation, the recovery or reflux can be selected according to the components of the low-boiling product;
3) cooling carrier gas returns to the heat exchange mass transfer section in the stripping tower from the carrier gas inlet 13, the cooling carrier gas exchanges heat with the carrier gas and the light components which rise continuously in the stripping tower, and the cooling carrier gas takes away part of heat, so that the temperature of the rising carrier gas and the light components is reduced; cooling carrier gas which takes away heat is subjected to heat compensation through a carrier gas heat exchanger 5, returns to the bottom of the stripping tower and is subjected to mass transfer with the raw material entering the stripping tower 1, so that the separation of heavy components and light components in the raw material is realized, the heat consumption and the cold consumption are reduced, and the energy-saving efficiency is 30%; the light components are rectified and separated through the heat exchange tubes and the fillers of the heat exchange mass transfer section at the top of the stripping tower, and the separation precision is improved.
In this embodiment, the vacuum pump 8 can also be used for vacuumizing and negative pressure, so that the cooling of the carrier gas in the tube array heat exchange tube arranged at the top of the gas stripping tower 1 is realized, the temperature of the carrier gas is reduced, when the light component rising along with the carrier gas passes through the tube array heat exchange tube arranged at the upper part of the gas stripping tower 1, the temperature of the light component is reduced to the maximum extent, and meanwhile, the filler in the tube array heat exchange tube strengthens mass transfer, the rectification separation is realized, and the separation precision of the separated substance is improved.
Example 2
Referring to fig. 2, an energy-saving carrier gas stripping system comprises a stripping tower 1 and a separation tank 2; a raw material heater 4; a carrier gas heater 5 and a gas circulation heat exchanger 6;
in this embodiment, the stripper 1 is provided with a raw material inlet 11, a light component reflux inlet 12, a carrier gas inlet 13, a light component outlet 14, a carrier gas outlet 15, a carrier gas circulation inlet 16, and a heavy component discharge outlet 17.
In the embodiment, the top in the stripping tower 1 is provided with a heat and mass transfer section; the heat exchange mass transfer section comprises a heat exchange tube and a filler, the heat exchange tube is a coiled heat exchange tube, and the filler is arranged outside the coiled heat exchange tube.
In this embodiment, the separation tank 2 is provided with a separation tank inlet 21, a separation tank top outlet 22, a separation tank bottom outlet 23, and a separation tank light component return port 24.
In this embodiment, the gas circulation heat exchanger 6 is provided with a heat exchanger top inlet 61, a heat exchanger gas outlet 62, a heat exchanger bottom outlet 63, and a heat exchanger gas inlet 64.
Specifically, the raw material heater 4 is connected with the raw material inlet 11 through a pipeline; the carrier gas outlet 15 is sequentially connected with the carrier gas heater 5 and the carrier gas circulating inlet 16 through pipelines; the light component outlet 14 is sequentially connected with the heat exchanger top inlet 61, the heat exchanger gas outlet 62 and the carrier gas inlet 13 through pipelines; the heavy component discharge opening 17 is connected with a discharge pipeline; the light component outlet 14 is sequentially connected with a heat exchanger top inlet 61, a heat exchanger bottom outlet 63 and a separation tank inlet 21 through pipelines; the outlet 23 at the bottom of the separating tank is respectively connected with the light component reflux inlet 12, the light component reflux port 24 of the separating tank and a low-boiling product pipeline through pipelines; the gas inlet 64 of the heat exchanger is connected with the outlet 22 at the top of the separation tank through a pipeline, the outlet 23 at the bottom of the separation tank is connected with the light component reflux inlet 12 through a pipeline, and a first valve is arranged on the pipeline; a second valve is arranged on a pipeline connected between the outlet 23 at the bottom of the separating tank and the light component return opening 24 of the separating tank.
In the present embodiment, the carrier gas heater 5 is an indirect heater.
Referring to fig. 2, in the present embodiment, a vacuum pump 8 is further included, which is connected to the separator tank top outlet 22 and the heat exchanger gas inlet 64; a fan 7 is arranged on a pipeline connecting the gas inlet 64 of the heat exchanger with the outlet 22 at the top of the separation tank, and a pump 9 is also arranged between the outlet 23 at the bottom of the separation tank and the first valve.
An energy-saving carrier gas stripping process comprises the following steps:
1) after the raw material is preheated and subjected to heat carrier gas mass transfer, heavy components in the raw material are discharged; after the light component is rectified and separated by the heat exchange and mass transfer section along with the carrier gas, the separated condensed component is taken as a product to be extracted; discharging the light components and the carrier gas which are not condensed and have reduced temperature;
2) the discharged carrier gas and light components are subjected to heat exchange and cooling to obtain cooling carrier gas and condensate, and the cooling carrier gas is sent to heat exchange and mass transfer; further cooling and separating the condensate to obtain a low-boiling product and carrier gas, and extracting or partially recycling the low-boiling product; after the carrier gas is subjected to heat exchange and cooling, the cooled carrier gas is sent to heat exchange and mass transfer;
3) and (3) after the cooling carrier gas sent to the heat exchange mass transfer in the step 2) exchanges heat and mass transfer with the carrier gas and the light components in the step 1), the cooling carrier gas recovers part of heat and performs mass transfer with the raw material after heat compensation.
In this embodiment, the vacuum is provided at the top of the separation tank 2 by a vacuum pump 8.
When the carrier gas stripping is carried out by adopting the embodiment, the principle is that the carrier gas and the negative pressure are adopted, and any mode can be selected, so that the bubble point of the separated substance is reduced to be lower than the working condition that the boiling point of the separated substance is about (0-50 ℃), and the separated substance is separated, cooled and recovered.
The specific separation process is as follows:
1) the raw material is heated by a raw material heater 4 by a raw material reciprocating pump 3 and enters a stripping tower 1 from a raw material inlet 11 for stripping; as the raw material is transferred with the hot carrier gas in the gas stripping tower 1 from the lower part upwards, the heavy component in the raw material is discharged from the heavy component discharge port 17 through the reciprocating pump; the hot light components in the raw materials continuously rise along with the carrier gas and are subjected to heat exchange and cooling through a coil type heat exchange tube at the top of the stripper column 1, the hot light components are cooled and are condensed and refluxed, and the condensed components are taken as middle-boiling components and are extracted from an outlet at the middle part of the side of the stripper column 1, so that purification, rectification and separation are realized; noncondensable components and light components with non-reduced temperature, and discharging the cooled light components from a light component outlet 14 at the top of the stripping tower along with the continuous rising of the carrier gas;
2) the noncondensable components from the light component outlet 14 enter the gas circulation heat exchanger 6 from the heat exchanger top inlet 61 to exchange heat and cool to obtain cooling carrier gas and condensate, the cooling carrier gas comes out from the heat exchanger gas outlet 62 and returns to the coil type heat exchange tube at the top of the stripper column 1 through the carrier gas inlet 13 to exchange heat with the light components which rise and flow through the coil type heat exchange tube for cooling, the temperature of the light components flowing out of the top of the stripper column 1 is reduced, and meanwhile, a medium boiling product is obtained;
the condensate flows out from an outlet 63 at the bottom of the heat exchanger and enters the separating tank 21 from an inlet 21 of the separating tank, and a low-boiling product and a small part of carrier gas are obtained through further cooling and separation by circulating water; a small part of carrier gas enters the gas circulation heat exchanger 6 from the gas inlet 64 of the heat exchanger after passing through the fan 7 for heat exchange and cooling, then comes out from the gas outlet 62 of the heat exchanger and returns to the coil type heat exchange tube at the top of the stripper column 1 through the carrier gas inlet 13, so that the temperature of light components flowing out of the top of the stripper column 1 is reduced, and meanwhile, a medium-boiling product is obtained; the low-boiling product is recovered after coming out from an outlet 23 at the bottom of the separation tank, or is returned to the light component reflux inlet 12 through a first valve, or is returned to a light component reflux inlet 24 of the separation tank through a second valve, and during implementation, the recovery or the reflux can be selected according to the components of the low-boiling product, and the control is carried out through the first valve and the second valve;
3) cooling carrier gas returns to a coil type heat exchange tube at the top of the stripping tower from a carrier gas inlet 13, the cooling carrier gas exchanges heat with light components in the stripping tower which continuously rise along with the carrier gas, so that the bubble point temperature of the light components which continuously rise along with the carrier gas is reduced, stripping separation is realized, meanwhile, the cooling carrier gas carries away heat after heat exchange, the cooling carrier gas comes out from a carrier gas outlet 15 after the temperature rises and is supplemented with heat by a carrier gas heater 5, and finally, the cooling carrier gas circularly enters the bottom of the stripping tower 1 from a carrier gas circulating inlet 16 and is subjected to mass transfer with raw materials entering the stripping tower; therefore, the recycling of the heat of the separation system is realized, the heat consumption and the cold consumption of the separation system are reduced, the energy-saving efficiency is 50 percent, and the purpose of saving energy is realized; the light components are rectified and separated through the heat exchange tubes and the fillers of the heat exchange mass transfer section at the top of the stripping tower, and the separation precision is improved.
In this embodiment, the vacuum pump 8 can also be used for vacuumizing and negative pressure to cool the carrier gas in the coil type heat exchange tube at the top of the stripper column 1, so that the temperature of the carrier gas is reduced, when the light component rising along with the carrier gas passes through the coil type heat exchange tube at the top of the stripper column 1, the temperature of the light component is reduced to the maximum extent, the filler outside the coil type heat exchange tube strengthens mass transfer, the separation precision of the separated substance is improved, and meanwhile, a medium boiling product is obtained.
In conclusion, the invention uses cooling carrier gas and negative pressure to reduce the bubble point of the separated substance, so that the separated substance can be extracted at the temperature lower than the normal bubble point to realize separation; integrated heat exchange is realized through the gas stripping tower and the separating tank, mass transfer is strengthened, and the separation precision of the separated substances is improved; meanwhile, the heat of the light component for heat exchange and mass transfer is recycled, so that the heat consumption and the cold consumption of system separation are reduced, the energy-saving efficiency can reach 30-50%, the invention provides two heat exchange modes and a heating mode, the separation temperature is low, the separation precision is high, the separated substances are not polluted, the energy consumption is low, the invention is suitable for the separation of high-boiling point, heat sensitivity and easily-oxidized substances, and the invention is more suitable for various processes of extraction, recovery and the like in the food-grade medicine fine chemical industry.
Claims (10)
1. An energy-saving carrier gas stripping system is characterized in that: the energy-saving carrier gas stripping system comprises a gas stripping tower (1), a separation tank (2), a raw material heater (4), a carrier gas heater (5) and a gas circulating heat exchanger (6);
a heat exchange mass transfer section is arranged in the stripping tower (1);
the gas stripping tower (1), the gas circulation heat exchanger (6) and the separating tank (2) are sequentially connected through pipelines; the gas circulation heat exchanger (6) is connected with the heat and mass transfer section through a pipeline; the separation tank (2) is connected with the stripping tower (1) through a pipeline; the raw material heater (4) is connected with the stripping tower (1) through a pipeline; the heat and mass transfer section is sequentially connected with the carrier gas heater (5) and the gas stripping tower (1) through pipelines.
2. The energy-saving carrier gas stripping system according to claim 1, characterized in that: the gas stripping tower (1) is provided with a raw material inlet (11), a light component reflux inlet (12), a carrier gas inlet (13), a light component outlet (14), a carrier gas outlet (15), a carrier gas circulating inlet (16) and a heavy component discharge outlet (17); the carrier gas inlet (13) and the carrier gas outlet (15) are both arranged on the heat exchange mass transfer section;
the separation tank (2) is provided with a separation tank inlet (21), a separation tank top outlet (22) and a separation tank bottom outlet (23);
the gas circulation heat exchanger (6) is provided with a heat exchanger top inlet (61), a heat exchanger gas outlet (62), a heat exchanger bottom outlet (63) and a heat exchanger gas inlet (64);
the raw material heater (4) is connected with the raw material inlet (11) through a pipeline; the carrier gas outlet (15) is sequentially connected with the carrier gas heater (5) and the carrier gas circulating inlet (16) through pipelines; the light component outlet (14) is sequentially connected with a heat exchanger top inlet (61), a heat exchanger gas outlet (62) and a carrier gas inlet (13) through pipelines;
the light component outlet (14) is sequentially connected with a heat exchanger top inlet (61), a heat exchanger bottom outlet (63) and a separation tank inlet (21) through pipelines; an outlet (23) at the bottom of the separation tank is connected with a light component backflow inlet (12) through a pipeline; and the gas inlet (64) of the heat exchanger is connected with the outlet (22) at the top of the separation tank through a pipeline.
3. The energy-saving carrier gas stripping system according to claim 2, characterized in that: and a first valve is arranged on a pipeline between the outlet (23) at the bottom of the separation tank and the light component backflow inlet (12).
4. The energy-saving carrier gas stripping system according to claim 1 or 2, characterized in that: the heat exchange mass transfer section comprises a heat exchange tube and a filler, and the heat exchange tube is a tube type heat exchange tube or a coil type heat exchange tube; the filler is arranged inside or outside the heat exchange tube.
5. The energy-saving carrier gas stripping system according to claim 1 or 2, characterized in that: the separating tank (2) is also provided with a separating tank light component return opening (24) connected with a separating tank bottom outlet (23), and a second valve is also arranged on a pipeline between the separating tank bottom outlet (23) and the separating tank light component return opening (24).
6. The energy-saving carrier gas stripping system according to claim 1 or 2, characterized in that: the carrier gas heater (5) is a direct heater or an indirect heater.
7. A stripping process based on the energy-saving carrier gas stripping system of any one of claims 1 to 6, which is characterized in that: the energy-saving carrier gas stripping process comprises the following steps:
1) after the raw material is preheated and subjected to heat carrier gas mass transfer, heavy components in the raw material are discharged; after the light component is rectified and separated by the heat exchange and mass transfer section along with the carrier gas, the separated condensed component is taken as a product to be extracted; discharging the light components and the carrier gas which are not condensed and have reduced temperature;
2) the discharged carrier gas and light components are subjected to heat exchange and cooling to obtain cooling carrier gas and condensate, and the cooling carrier gas is sent to heat exchange and mass transfer; further cooling and separating the condensate to obtain a low-boiling product and carrier gas, and extracting or partially recycling the low-boiling product; after the carrier gas is subjected to heat exchange and cooling, the cooled carrier gas is sent to heat exchange and mass transfer;
3) and (3) after the cooling carrier gas sent to the heat exchange mass transfer in the step 2) exchanges heat and mass transfer with the carrier gas and the light components in the step 1), the cooling carrier gas recovers part of heat and performs mass transfer with the raw material after heat compensation.
8. The energy-saving carrier gas stripping process according to claim 7, characterized in that: the specific realization process of the step 1) is that the raw material is heated by a raw material heater (4) and then enters a stripping tower (1), hot light components rise after mass transfer through stripping, and heavy components fall and are discharged from a heavy component discharge port (17) through a pump; when the hot light component rises to the top of the gas stripping tower (1), the heat exchange is carried out with the cooling carrier gas of the heat exchange mass transfer section, the hot light component is cooled and condensed and reflows to obtain a medium boiling product which is extracted from the middle part of the gas stripping tower (1), and the purification, rectification and separation are realized; the light component and the carrier gas having the lowered temperature are discharged from the light component outlet (14).
9. The energy-saving carrier gas stripping process according to claim 7, characterized in that: in the step 2), the light components and the carrier gas from the light component outlet (14) enter the gas circulation heat exchanger (6) from the heat exchanger top inlet (61) for heat exchange and cooling to obtain cooling carrier gas and condensate, the cooling carrier gas comes out from the heat exchanger gas outlet (62) and returns to the top of the stripper column (1) through the carrier gas inlet (13) to exchange heat with the light components flowing upwards for cooling, so that the temperature of the light components flowing out of the top of the stripper column (1) is reduced, and meanwhile, a medium-boiling product is obtained;
the condensate flows out from a bottom outlet (63) of the heat exchanger and enters a separating tank (21) from an inlet (21) of the separating tank to be cooled and separated to obtain a low-boiling product and a small part of carrier gas; a small part of carrier gas is cooled by heat exchange in the gas circulation heat exchanger (6) and then returns to the top of the stripping tower (1), and a medium boiling product is obtained while the temperature of light components flowing out of the top of the stripping tower (1) is reduced; the low-boiling products are directly recycled after coming out of an outlet (23) at the bottom of the separation tank or returned to a light component reflux inlet (12) through a first valve; or returned to the knockout drum light component return opening (24) through a second valve.
10. The energy-saving carrier gas stripping process according to claim 7, characterized in that: in the step 3), the specific implementation process of the step 3) is that the cooling carrier gas returns to the heat exchange mass transfer section in the stripper from the carrier gas inlet (13), the cooling carrier gas exchanges heat with the carrier gas and the light components which rise continuously in the stripper, and the cooling carrier gas takes away part of heat; the cooling carrier gas with heat is supplemented by the carrier gas heat exchanger (5), and then returns to the bottom of the stripping tower to carry out mass transfer with the raw material entering the stripping tower (1).
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| CN202010297307.8A CN111450561B (en) | 2020-04-15 | 2020-04-15 | Energy-saving carrier gas stripping system and stripping process |
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| CN202010297307.8A CN111450561B (en) | 2020-04-15 | 2020-04-15 | Energy-saving carrier gas stripping system and stripping process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113234567A (en) * | 2021-04-08 | 2021-08-10 | 陕西聚能新创煤化科技有限公司 | System and process for preparing wine by stripping and distilling by using carrier gas method |
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| CN111450561B (en) | 2024-04-26 |
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